Revised list of TBCs

author: kinitrupti 2017-05-12 18:40:35 +0530
committer: kinitrupti 2017-05-12 18:40:35 +0530
commit: d36fc3b8f88cc3108ffff6151e376b619b9abb01 (patch)
tree: 9806b0d68a708d2cfc4efc8ae3751423c56b7721 /Process_Heat_Transfer_by_D._Q._Kern
parent: 1b1bb67e9ea912be5c8591523c8b328766e3680f (diff)
download: Python-Textbook-Companions-d36fc3b8f88cc3108ffff6151e376b619b9abb01.tar.gz
Python-Textbook-Companions-d36fc3b8f88cc3108ffff6151e376b619b9abb01.tar.bz2
Python-Textbook-Companions-d36fc3b8f88cc3108ffff6151e376b619b9abb01.zip
68 files changed, 0 insertions, 48804 deletions
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection.ipynb
deleted file mode 100755
index d735fd25..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection.ipynb
+++ /dev/null
@@ -1,580 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 10 :Stream Line Flow and Heat Convection"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.1 pgno:203"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for crude \t\n",
-      "\t total heat required for crude is :  Btu/hr \t388000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t387655.0\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.381317817\n",
-      "\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \n",
-      "\n",
-      "\t caloric temperature of cold fluid is :  F \t110.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude \t\n",
-      "\t flow area is : ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t918.009849613\n",
-      "\t reynolds number is :  \t564.193553408\n",
-      "\t prandelt number is :  \t72.6936774194\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1.98827586207\n",
-      "\t phyt is :  \t1.2141948844\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t2.41415438049\n",
-      "\t tp is :  F \t249.775040982\n",
-      "\t delt is :  F \t139.775040982\n",
-      "\t total surface area is :  ft**2 \t117.6\n",
-      "\t delt3 is :  F \t5.1\n",
-      "\t ti is :  F \t100.1\n",
-      "The oil now enters the second pass at given 126.9 f\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=410.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for crude \\t\"\n",
-    "c=0.485; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "\n",
-    "print\"\\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \\n\"\n",
-    "ti=125; # F\n",
-    "tc=((t1)+(ti))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.95*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=4.8*2.42; # at 110F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "c=0.485; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.0775; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu3)/k); # prandelt number\n",
-    "print\"\\t prandelt number is :  \\t\",Pr\n",
-    "Hi=((1.86)*(k/D)*((Ret2*(D/L)*Pr)**(1/3))); # using eq.6.1,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "muw=1.2*2.42; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hi=(Hi)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "tp=(tc)+(((ho)/(hi+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tp is :  F \\t\",tp\n",
-    "delt=tp-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Ai1=0.228 # internal surface per foot of length,ft\n",
-    "Ai=(Nt*L*Ai1/2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",round(Ai,1)\n",
-    "delt3=((hi*Ai*delt)/(W*c)); # delt3=ti-t1, F\n",
-    "print\"\\t delt3 is :  F \\t\",round(delt3,1)\n",
-    "ti=t1+delt3; # F\n",
-    "print\"\\t ti is :  F \\t\",round(ti,1)\n",
-    "print\"The oil now enters the second pass at given 126.9 f\"\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## EXAMPLE 10.2 pgno:207"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for kerosene \t\n",
-      "\t total heat required for kerosene is :  Btu/hr \t400000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t399946.5\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.525612445\n",
-      "\t caloric temperature of cold fluid is :  F \t120.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,kerosene \t\n",
-      "\t flow area is :  ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t1991.27136497\n",
-      "\t reynolds number is :  \t1547.50231792\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t10.2620689655\n",
-      "\t Hio is :  Btu/(hr)*(ft**2)*(F) \t8.928\n",
-      "\t tw is :  F \t249.23081817\n",
-      "\t phyt is :  \t1.16189787585\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t10.3734242356\n",
-      "\t delt is :  F \t129.23081817\n",
-      "\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \t\n",
-      "\t beta is :  /F \t0.000449494949495\n",
-      "\t G is :   \t1289776.29615\n",
-      "\t psy is :   \t0.712464789946\n",
-      "\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \t7.39069951902\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t14.7\n",
-      "\t total surface area is :  ft**2 \t270.1776\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t11.5\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#gien\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=423.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for kerosene \\t\"\n",
-    "c=0.5; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,kerosene \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.36*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=1.75*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "Z1=331; # Z1=(L*n/D)\n",
-    "jH=3.1; # from fig 24\n",
-    "mu4=1.75; # cp and 40 API\n",
-    "Z2=0.24; # Z2=((k)*(c*mu4/k)**(1/3)), from fig 16\n",
-    "Hi=((jH)*(1/D)*(Z2)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=(Hi*(ID/OD)); #Btu/(hr)*(ft**2)*(F), from eq.6.5\n",
-    "print\"\\t Hio is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "tw=(tc)+(((ho)/(Hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=1.45; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "delt=tw-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \\t\"\n",
-    "s=0.8;\n",
-    "row=50; # lb/ft**3, from fig 6\n",
-    "s1=0.810; # at 95F\n",
-    "s2=0.792; # at 145F\n",
-    "bita=((s1**2-s2**2)/(2*(t2-t1)*s1*s2)); # /F\n",
-    "print\"\\t beta is :  /F \\t\",bita\n",
-    "G=((D**3)*(row**2)*(bita)*(delt)*(4.18*10**8)/(mu3**2));\n",
-    "print\"\\t G is :   \\t\",G\n",
-    "psy=((2.25)*(1+(0.01*G**(1/3)))/(log10(Ret2)));\n",
-    "print\"\\t psy is :   \\t\",psy\n",
-    "hio1=(hio*psy);\n",
-    "print\"\\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=2*((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(UD,1)\n",
-    "Rd=-0.407*((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.3 pgno:211"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas oil \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t587500.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t588101.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t120.0\n",
-      "\t LMTD is : F \t132.254461931\n",
-      "\t caloric temperature of cold fluid is : %.1f F \t117.5\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.317708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19577.704918\n",
-      "\t reynolds number is :  \t37409.6272319\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t at1 is :  in**2 \t0.3979165\n",
-      "\t flow area is :  ft**2 \t0.118822288194\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t420796.474801\n",
-      "\t De is :  ft \t0.0485536398467\n",
-      "\t reynolds number is :  \t1223.42517882\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t22.3464194121\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t19.4413848885\n",
-      "\t phyt is :  \t1.18932885404\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t23.1222000104\n",
-      "\t tw is :  F \t247.988545173\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7711867211\n",
-      "\t total surface area is :  ft**2 \t270\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.4694016372\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0168035136331\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t9\n",
-      "\t delPs is :  psi \t1.19559186672\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t dt is :  ft \t0.0308333333333\n",
-      "\t Ret2 is :  \t776.919639103\n",
-      "\t phyt is :  \t1.35\n",
-      "\t delPt is :  psi \t2.0\n",
-      "\t delPr is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=105.; # inlet cold fluid,F\n",
-    "t2=130.; # outlet cold fluid,F\n",
-    "w=50000.; # lb/hr\n",
-    "W=622.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas oil \\t\"\n",
-    "c=0.47; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : %.1f F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=15; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2, eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(6220/As); # mass velocity,lb/(hr)*(ft**2), calculation mistake\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0314; # at 250F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.060; # from fig.29,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number, calculation mistake\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "ho=1500; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "d1=0.5; # in\n",
-    "d2=0.87; # in\n",
-    "at1=((3.14*(d2**2-d1**2))/4);\n",
-    "print\"\\t at1 is :  in**2 \\t\",at1\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "De=(d2**2-d1**2)/(12*d2);\n",
-    "print\"\\t De is :  ft \\t\",De\n",
-    "mu2=16.7; # at 117F,lb/(ft)*(hr)\n",
-    "Ret=((De)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=3.1; # from fig.24\n",
-    "Z=0.35; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=6.9cp and 28 API\n",
-    "Hi=((jH)*(1/De)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "muw=4.84; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A=270; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0016; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.00116; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(19600**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "dt=(d2-d1)/(12); # ft\n",
-    "print\"\\t dt is :  ft \\t\",dt\n",
-    "Ret2=(dt*Gt/mu2);\n",
-    "print\"\\t Ret2 is :  \\t\",Ret2\n",
-    "f=0.00066; # friction factor for reynolds number 8220, using fig.26\n",
-    "phyt=1.35; # fig 6\n",
-    "print\"\\t phyt is :  \\t\",phyt\n",
-    "s=0.85;\n",
-    "delPt=((f*(420000**2)*(L)*(n))/(5.22*(10**10)*(0.0309)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.4 pgno:217"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t delt is : F \t100\n",
-      "\t convection loss is :  Btu/(hr)(ft**2)(F) \t0.948683298051\n",
-      "\t radiation loss is :  Btu/(hr)(ft**2)(F) \t0.510696\n",
-      "\t combined loss is :  Btu/(hr)(ft**2)(F) \t1.45937929805\n",
-      "\t total tank area is :  ft**2 \t227.65\n",
-      "\t total heat loss :  Btu/hr \t33222.7697201\n",
-      "\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \t\n",
-      "\t X is :  \t75.7575757576\n",
-      "\t tf is :  F \t156\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t23.9583333333\n",
-      "\t total surface is :  ft**2 \t12.3811564174\n",
-      "\t number of pipes are :  \t7.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "t1=100; # F\n",
-    "t2=0; # F\n",
-    "T1abs=100+460; # R\n",
-    "T2abs=460; #R\n",
-    "#solution\n",
-    "delt=t1-t2;\n",
-    "from math import ceil\n",
-    "print\"\\t delt is : F \\t\",delt\n",
-    "hc=0.3*(delt**0.25); # convection loss, Btu/(hr)*(ft**2)*( degree F)\n",
-    "print\"\\t convection loss is :  Btu/(hr)(ft**2)(F) \\t\",hc\n",
-    "e=0.8; # emissivity\n",
-    "hr=((0.173*e*((T1abs/100)**4-(T2abs/100)**4))/(T1abs-T2abs)); # radiation rate, from 4.32, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t radiation loss is :  Btu/(hr)(ft**2)(F) \\t\",hr\n",
-    "hl=hc+hr; # combined loss, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t combined loss is :  Btu/(hr)(ft**2)(F) \\t\",hl\n",
-    "D=5; # ft\n",
-    "L=12; # ft\n",
-    "A1=((2*3.14*D**2)/(4))+(3.14*D*L); # total tank area\n",
-    "print\"\\t total tank area is :  ft**2 \\t\",A1\n",
-    "Q=(hl*A1*delt); # total heat loss\n",
-    "print\"\\t total heat loss :  Btu/hr \\t\",Q\n",
-    "print\"\\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \\t\"\n",
-    "d0=1.32;\n",
-    "X=(delt/d0);\n",
-    "tf=((t1+212)/2); # F\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "hio=48; # from fig 10.4, Btu/(hr)(ft**2)(F)\n",
-    "ho=1500; # condensation of steam,Btu/(hr)(ft**2)(F)\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.02; # dirt factor, (hr)(ft**2)(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A2=((Q)/((UD)*(212-100))); # total surface,ft**2\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A2\n",
-    "A3=2.06; # area/pipe\n",
-    "N=(A2/A3);\n",
-    "print\"\\t number of pipes are :  \\t\",ceil(N)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_1.ipynb
deleted file mode 100755
index 8e712245..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_1.ipynb
+++ /dev/null
@@ -1,562 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 10 :Stream Line Flow and Heat Convection"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.1 pgno:203"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for crude \t\n",
-      "\t total heat required for crude is :  Btu/hr \t388000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t387655.0\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.381317817\n",
-      "\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \n",
-      "\n",
-      "\t caloric temperature of cold fluid is :  F \t110.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude \t\n",
-      "\t flow area is : ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t918.009849613\n",
-      "\t reynolds number is :  \t564.193553408\n",
-      "\t prandelt number is :  \t72.6936774194\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1.98827586207\n",
-      "\t phyt is :  \t1.2141948844\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t2.41415438049\n",
-      "\t tp is :  F \t249.775040982\n",
-      "\t delt is :  F \t139.775040982\n",
-      "\t total surface area is :  ft**2 \t117.6\n",
-      "\t delt3 is :  F \t5.1\n",
-      "\t ti is :  F \t100.1\n",
-      "The oil now enters the second pass at given 126.9 f\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=410.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for crude \\t\"\n",
-    "c=0.485; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "\n",
-    "print\"\\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \\n\"\n",
-    "ti=125; # F\n",
-    "tc=((t1)+(ti))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.95*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=4.8*2.42; # at 110F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "c=0.485; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.0775; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu3)/k); # prandelt number\n",
-    "print\"\\t prandelt number is :  \\t\",Pr\n",
-    "Hi=((1.86)*(k/D)*((Ret2*(D/L)*Pr)**(1/3))); # using eq.6.1,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "muw=1.2*2.42; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hi=(Hi)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "tp=(tc)+(((ho)/(hi+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tp is :  F \\t\",tp\n",
-    "delt=tp-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Ai1=0.228 # internal surface per foot of length,ft\n",
-    "Ai=(Nt*L*Ai1/2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",round(Ai,1)\n",
-    "delt3=((hi*Ai*delt)/(W*c)); # delt3=ti-t1, F\n",
-    "print\"\\t delt3 is :  F \\t\",round(delt3,1)\n",
-    "ti=t1+delt3; # F\n",
-    "print\"\\t ti is :  F \\t\",round(ti,1)\n",
-    "print\"The oil now enters the second pass at given 126.9 f\"\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## EXAMPLE 10.2 pgno:207"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for kerosene \t\n",
-      "\t total heat required for kerosene is :  Btu/hr \t400000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t399946.5\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.525612445\n",
-      "\t caloric temperature of cold fluid is :  F \t120.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,kerosene \t\n",
-      "\t flow area is :  ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t1991.27136497\n",
-      "\t reynolds number is :  \t1547.50231792\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t10.2620689655\n",
-      "\t Hio is :  Btu/(hr)*(ft**2)*(F) \t8.928\n",
-      "\t tw is :  F \t249.23081817\n",
-      "\t phyt is :  \t1.16189787585\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t10.3734242356\n",
-      "\t delt is :  F \t129.23081817\n",
-      "\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \t\n",
-      "\t beta is :  /F \t0.000449494949495\n",
-      "\t G is :   \t1289776.29615\n",
-      "\t psy is :   \t0.712464789946\n",
-      "\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \t7.39069951902\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t14.7\n",
-      "\t total surface area is :  ft**2 \t270.1776\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t11.5\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#gien\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=423.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for kerosene \\t\"\n",
-    "c=0.5; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,kerosene \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.36*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=1.75*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "Z1=331; # Z1=(L*n/D)\n",
-    "jH=3.1; # from fig 24\n",
-    "mu4=1.75; # cp and 40 API\n",
-    "Z2=0.24; # Z2=((k)*(c*mu4/k)**(1/3)), from fig 16\n",
-    "Hi=((jH)*(1/D)*(Z2)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=(Hi*(ID/OD)); #Btu/(hr)*(ft**2)*(F), from eq.6.5\n",
-    "print\"\\t Hio is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "tw=(tc)+(((ho)/(Hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=1.45; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "delt=tw-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \\t\"\n",
-    "s=0.8;\n",
-    "row=50; # lb/ft**3, from fig 6\n",
-    "s1=0.810; # at 95F\n",
-    "s2=0.792; # at 145F\n",
-    "bita=((s1**2-s2**2)/(2*(t2-t1)*s1*s2)); # /F\n",
-    "print\"\\t beta is :  /F \\t\",bita\n",
-    "G=((D**3)*(row**2)*(bita)*(delt)*(4.18*10**8)/(mu3**2));\n",
-    "print\"\\t G is :   \\t\",G\n",
-    "psy=((2.25)*(1+(0.01*G**(1/3)))/(log10(Ret2)));\n",
-    "print\"\\t psy is :   \\t\",psy\n",
-    "hio1=(hio*psy);\n",
-    "print\"\\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=2*((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(UD,1)\n",
-    "Rd=-0.407*((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.3 pgno:211"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas oil \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t587500.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t588101.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t120.0\n",
-      "\t LMTD is : F \t132.254461931\n",
-      "\t caloric temperature of cold fluid is : %.1f F \t117.5\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.317708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19577.704918\n",
-      "\t reynolds number is :  \t37409.6272319\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t at1 is :  in**2 \t0.3979165\n",
-      "\t flow area is :  ft**2 \t0.118822288194\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t420796.474801\n",
-      "\t De is :  ft \t0.0485536398467\n",
-      "\t reynolds number is :  \t1223.42517882\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t22.3464194121\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t19.4413848885\n",
-      "\t phyt is :  \t1.18932885404\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t23.1222000104\n",
-      "\t tw is :  F \t247.988545173\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7711867211\n",
-      "\t total surface area is :  ft**2 \t270\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.4694016372\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0168035136331\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t9\n",
-      "\t delPs is :  psi \t1.19559186672\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t dt is :  ft \t0.0308333333333\n",
-      "\t Ret2 is :  \t776.919639103\n",
-      "\t phyt is :  \t1.35\n",
-      "\t delPt is :  psi \t2.0\n",
-      "\t delPr is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=105.; # inlet cold fluid,F\n",
-    "t2=130.; # outlet cold fluid,F\n",
-    "w=50000.; # lb/hr\n",
-    "W=622.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas oil \\t\"\n",
-    "c=0.47; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : %.1f F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=15; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2, eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(6220/As); # mass velocity,lb/(hr)*(ft**2), calculation mistake\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0314; # at 250F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.060; # from fig.29,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number, calculation mistake\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "ho=1500; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "d1=0.5; # in\n",
-    "d2=0.87; # in\n",
-    "at1=((3.14*(d2**2-d1**2))/4);\n",
-    "print\"\\t at1 is :  in**2 \\t\",at1\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "De=(d2**2-d1**2)/(12*d2);\n",
-    "print\"\\t De is :  ft \\t\",De\n",
-    "mu2=16.7; # at 117F,lb/(ft)*(hr)\n",
-    "Ret=((De)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=3.1; # from fig.24\n",
-    "Z=0.35; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=6.9cp and 28 API\n",
-    "Hi=((jH)*(1/De)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "muw=4.84; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A=270; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0016; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.00116; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(19600**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "dt=(d2-d1)/(12); # ft\n",
-    "print\"\\t dt is :  ft \\t\",dt\n",
-    "Ret2=(dt*Gt/mu2);\n",
-    "print\"\\t Ret2 is :  \\t\",Ret2\n",
-    "f=0.00066; # friction factor for reynolds number 8220, using fig.26\n",
-    "phyt=1.35; # fig 6\n",
-    "print\"\\t phyt is :  \\t\",phyt\n",
-    "s=0.85;\n",
-    "delPt=((f*(420000**2)*(L)*(n))/(5.22*(10**10)*(0.0309)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.4 pgno:217"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t delt is : F \t100\n",
-      "\t convection loss is :  Btu/(hr)(ft**2)(F) \t0.948683298051\n",
-      "\t radiation loss is :  Btu/(hr)(ft**2)(F) \t0.510696\n",
-      "\t combined loss is :  Btu/(hr)(ft**2)(F) \t1.45937929805\n",
-      "\t total tank area is :  ft**2 \t227.65\n",
-      "\t total heat loss :  Btu/hr \t33222.7697201\n",
-      "\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \t\n",
-      "\t X is :  \t75.7575757576\n",
-      "\t tf is :  F \t156\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t23.9583333333\n",
-      "\t total surface is :  ft**2 \t12.3811564174\n",
-      "\t number of pipes are :  \t7.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "t1=100; # F\n",
-    "t2=0; # F\n",
-    "T1abs=100+460; # R\n",
-    "T2abs=460; #R\n",
-    "#solution\n",
-    "delt=t1-t2;\n",
-    "from math import ceil\n",
-    "print\"\\t delt is : F \\t\",delt\n",
-    "hc=0.3*(delt**0.25); # convection loss, Btu/(hr)*(ft**2)*( degree F)\n",
-    "print\"\\t convection loss is :  Btu/(hr)(ft**2)(F) \\t\",hc\n",
-    "e=0.8; # emissivity\n",
-    "hr=((0.173*e*((T1abs/100)**4-(T2abs/100)**4))/(T1abs-T2abs)); # radiation rate, from 4.32, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t radiation loss is :  Btu/(hr)(ft**2)(F) \\t\",hr\n",
-    "hl=hc+hr; # combined loss, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t combined loss is :  Btu/(hr)(ft**2)(F) \\t\",hl\n",
-    "D=5; # ft\n",
-    "L=12; # ft\n",
-    "A1=((2*3.14*D**2)/(4))+(3.14*D*L); # total tank area\n",
-    "print\"\\t total tank area is :  ft**2 \\t\",A1\n",
-    "Q=(hl*A1*delt); # total heat loss\n",
-    "print\"\\t total heat loss :  Btu/hr \\t\",Q\n",
-    "print\"\\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \\t\"\n",
-    "d0=1.32;\n",
-    "X=(delt/d0);\n",
-    "tf=((t1+212)/2); # F\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "hio=48; # from fig 10.4, Btu/(hr)(ft**2)(F)\n",
-    "ho=1500; # condensation of steam,Btu/(hr)(ft**2)(F)\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.02; # dirt factor, (hr)(ft**2)(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A2=((Q)/((UD)*(212-100))); # total surface,ft**2\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A2\n",
-    "A3=2.06; # area/pipe\n",
-    "N=(A2/A3);\n",
-    "print\"\\t number of pipes are :  \\t\",ceil(N)\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_2.ipynb
deleted file mode 100755
index 8e712245..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_2.ipynb
+++ /dev/null
@@ -1,562 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 10 :Stream Line Flow and Heat Convection"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.1 pgno:203"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for crude \t\n",
-      "\t total heat required for crude is :  Btu/hr \t388000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t387655.0\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.381317817\n",
-      "\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \n",
-      "\n",
-      "\t caloric temperature of cold fluid is :  F \t110.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude \t\n",
-      "\t flow area is : ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t918.009849613\n",
-      "\t reynolds number is :  \t564.193553408\n",
-      "\t prandelt number is :  \t72.6936774194\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1.98827586207\n",
-      "\t phyt is :  \t1.2141948844\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t2.41415438049\n",
-      "\t tp is :  F \t249.775040982\n",
-      "\t delt is :  F \t139.775040982\n",
-      "\t total surface area is :  ft**2 \t117.6\n",
-      "\t delt3 is :  F \t5.1\n",
-      "\t ti is :  F \t100.1\n",
-      "The oil now enters the second pass at given 126.9 f\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=410.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for crude \\t\"\n",
-    "c=0.485; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "\n",
-    "print\"\\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \\n\"\n",
-    "ti=125; # F\n",
-    "tc=((t1)+(ti))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.95*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=4.8*2.42; # at 110F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "c=0.485; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.0775; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu3)/k); # prandelt number\n",
-    "print\"\\t prandelt number is :  \\t\",Pr\n",
-    "Hi=((1.86)*(k/D)*((Ret2*(D/L)*Pr)**(1/3))); # using eq.6.1,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "muw=1.2*2.42; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hi=(Hi)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "tp=(tc)+(((ho)/(hi+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tp is :  F \\t\",tp\n",
-    "delt=tp-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Ai1=0.228 # internal surface per foot of length,ft\n",
-    "Ai=(Nt*L*Ai1/2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",round(Ai,1)\n",
-    "delt3=((hi*Ai*delt)/(W*c)); # delt3=ti-t1, F\n",
-    "print\"\\t delt3 is :  F \\t\",round(delt3,1)\n",
-    "ti=t1+delt3; # F\n",
-    "print\"\\t ti is :  F \\t\",round(ti,1)\n",
-    "print\"The oil now enters the second pass at given 126.9 f\"\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## EXAMPLE 10.2 pgno:207"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for kerosene \t\n",
-      "\t total heat required for kerosene is :  Btu/hr \t400000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t399946.5\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.525612445\n",
-      "\t caloric temperature of cold fluid is :  F \t120.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,kerosene \t\n",
-      "\t flow area is :  ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t1991.27136497\n",
-      "\t reynolds number is :  \t1547.50231792\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t10.2620689655\n",
-      "\t Hio is :  Btu/(hr)*(ft**2)*(F) \t8.928\n",
-      "\t tw is :  F \t249.23081817\n",
-      "\t phyt is :  \t1.16189787585\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t10.3734242356\n",
-      "\t delt is :  F \t129.23081817\n",
-      "\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \t\n",
-      "\t beta is :  /F \t0.000449494949495\n",
-      "\t G is :   \t1289776.29615\n",
-      "\t psy is :   \t0.712464789946\n",
-      "\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \t7.39069951902\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t14.7\n",
-      "\t total surface area is :  ft**2 \t270.1776\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t11.5\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#gien\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=423.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for kerosene \\t\"\n",
-    "c=0.5; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,kerosene \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.36*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=1.75*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "Z1=331; # Z1=(L*n/D)\n",
-    "jH=3.1; # from fig 24\n",
-    "mu4=1.75; # cp and 40 API\n",
-    "Z2=0.24; # Z2=((k)*(c*mu4/k)**(1/3)), from fig 16\n",
-    "Hi=((jH)*(1/D)*(Z2)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=(Hi*(ID/OD)); #Btu/(hr)*(ft**2)*(F), from eq.6.5\n",
-    "print\"\\t Hio is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "tw=(tc)+(((ho)/(Hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=1.45; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "delt=tw-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \\t\"\n",
-    "s=0.8;\n",
-    "row=50; # lb/ft**3, from fig 6\n",
-    "s1=0.810; # at 95F\n",
-    "s2=0.792; # at 145F\n",
-    "bita=((s1**2-s2**2)/(2*(t2-t1)*s1*s2)); # /F\n",
-    "print\"\\t beta is :  /F \\t\",bita\n",
-    "G=((D**3)*(row**2)*(bita)*(delt)*(4.18*10**8)/(mu3**2));\n",
-    "print\"\\t G is :   \\t\",G\n",
-    "psy=((2.25)*(1+(0.01*G**(1/3)))/(log10(Ret2)));\n",
-    "print\"\\t psy is :   \\t\",psy\n",
-    "hio1=(hio*psy);\n",
-    "print\"\\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=2*((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(UD,1)\n",
-    "Rd=-0.407*((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.3 pgno:211"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas oil \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t587500.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t588101.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t120.0\n",
-      "\t LMTD is : F \t132.254461931\n",
-      "\t caloric temperature of cold fluid is : %.1f F \t117.5\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.317708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19577.704918\n",
-      "\t reynolds number is :  \t37409.6272319\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t at1 is :  in**2 \t0.3979165\n",
-      "\t flow area is :  ft**2 \t0.118822288194\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t420796.474801\n",
-      "\t De is :  ft \t0.0485536398467\n",
-      "\t reynolds number is :  \t1223.42517882\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t22.3464194121\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t19.4413848885\n",
-      "\t phyt is :  \t1.18932885404\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t23.1222000104\n",
-      "\t tw is :  F \t247.988545173\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7711867211\n",
-      "\t total surface area is :  ft**2 \t270\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.4694016372\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0168035136331\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t9\n",
-      "\t delPs is :  psi \t1.19559186672\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t dt is :  ft \t0.0308333333333\n",
-      "\t Ret2 is :  \t776.919639103\n",
-      "\t phyt is :  \t1.35\n",
-      "\t delPt is :  psi \t2.0\n",
-      "\t delPr is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=105.; # inlet cold fluid,F\n",
-    "t2=130.; # outlet cold fluid,F\n",
-    "w=50000.; # lb/hr\n",
-    "W=622.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas oil \\t\"\n",
-    "c=0.47; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : %.1f F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=15; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2, eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(6220/As); # mass velocity,lb/(hr)*(ft**2), calculation mistake\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0314; # at 250F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.060; # from fig.29,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number, calculation mistake\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "ho=1500; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "d1=0.5; # in\n",
-    "d2=0.87; # in\n",
-    "at1=((3.14*(d2**2-d1**2))/4);\n",
-    "print\"\\t at1 is :  in**2 \\t\",at1\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "De=(d2**2-d1**2)/(12*d2);\n",
-    "print\"\\t De is :  ft \\t\",De\n",
-    "mu2=16.7; # at 117F,lb/(ft)*(hr)\n",
-    "Ret=((De)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=3.1; # from fig.24\n",
-    "Z=0.35; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=6.9cp and 28 API\n",
-    "Hi=((jH)*(1/De)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "muw=4.84; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A=270; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0016; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.00116; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(19600**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "dt=(d2-d1)/(12); # ft\n",
-    "print\"\\t dt is :  ft \\t\",dt\n",
-    "Ret2=(dt*Gt/mu2);\n",
-    "print\"\\t Ret2 is :  \\t\",Ret2\n",
-    "f=0.00066; # friction factor for reynolds number 8220, using fig.26\n",
-    "phyt=1.35; # fig 6\n",
-    "print\"\\t phyt is :  \\t\",phyt\n",
-    "s=0.85;\n",
-    "delPt=((f*(420000**2)*(L)*(n))/(5.22*(10**10)*(0.0309)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.4 pgno:217"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t delt is : F \t100\n",
-      "\t convection loss is :  Btu/(hr)(ft**2)(F) \t0.948683298051\n",
-      "\t radiation loss is :  Btu/(hr)(ft**2)(F) \t0.510696\n",
-      "\t combined loss is :  Btu/(hr)(ft**2)(F) \t1.45937929805\n",
-      "\t total tank area is :  ft**2 \t227.65\n",
-      "\t total heat loss :  Btu/hr \t33222.7697201\n",
-      "\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \t\n",
-      "\t X is :  \t75.7575757576\n",
-      "\t tf is :  F \t156\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t23.9583333333\n",
-      "\t total surface is :  ft**2 \t12.3811564174\n",
-      "\t number of pipes are :  \t7.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "t1=100; # F\n",
-    "t2=0; # F\n",
-    "T1abs=100+460; # R\n",
-    "T2abs=460; #R\n",
-    "#solution\n",
-    "delt=t1-t2;\n",
-    "from math import ceil\n",
-    "print\"\\t delt is : F \\t\",delt\n",
-    "hc=0.3*(delt**0.25); # convection loss, Btu/(hr)*(ft**2)*( degree F)\n",
-    "print\"\\t convection loss is :  Btu/(hr)(ft**2)(F) \\t\",hc\n",
-    "e=0.8; # emissivity\n",
-    "hr=((0.173*e*((T1abs/100)**4-(T2abs/100)**4))/(T1abs-T2abs)); # radiation rate, from 4.32, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t radiation loss is :  Btu/(hr)(ft**2)(F) \\t\",hr\n",
-    "hl=hc+hr; # combined loss, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t combined loss is :  Btu/(hr)(ft**2)(F) \\t\",hl\n",
-    "D=5; # ft\n",
-    "L=12; # ft\n",
-    "A1=((2*3.14*D**2)/(4))+(3.14*D*L); # total tank area\n",
-    "print\"\\t total tank area is :  ft**2 \\t\",A1\n",
-    "Q=(hl*A1*delt); # total heat loss\n",
-    "print\"\\t total heat loss :  Btu/hr \\t\",Q\n",
-    "print\"\\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \\t\"\n",
-    "d0=1.32;\n",
-    "X=(delt/d0);\n",
-    "tf=((t1+212)/2); # F\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "hio=48; # from fig 10.4, Btu/(hr)(ft**2)(F)\n",
-    "ho=1500; # condensation of steam,Btu/(hr)(ft**2)(F)\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.02; # dirt factor, (hr)(ft**2)(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A2=((Q)/((UD)*(212-100))); # total surface,ft**2\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A2\n",
-    "A3=2.06; # area/pipe\n",
-    "N=(A2/A3);\n",
-    "print\"\\t number of pipes are :  \\t\",ceil(N)\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_3.ipynb
deleted file mode 100755
index 8e712245..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_10_Stream_Line_Flow_and_Heat_Convection_3.ipynb
+++ /dev/null
@@ -1,562 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 10 :Stream Line Flow and Heat Convection"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.1 pgno:203"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for crude \t\n",
-      "\t total heat required for crude is :  Btu/hr \t388000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t387655.0\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.381317817\n",
-      "\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \n",
-      "\n",
-      "\t caloric temperature of cold fluid is :  F \t110.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude \t\n",
-      "\t flow area is : ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t918.009849613\n",
-      "\t reynolds number is :  \t564.193553408\n",
-      "\t prandelt number is :  \t72.6936774194\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1.98827586207\n",
-      "\t phyt is :  \t1.2141948844\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t2.41415438049\n",
-      "\t tp is :  F \t249.775040982\n",
-      "\t delt is :  F \t139.775040982\n",
-      "\t total surface area is :  ft**2 \t117.6\n",
-      "\t delt3 is :  F \t5.1\n",
-      "\t ti is :  F \t100.1\n",
-      "The oil now enters the second pass at given 126.9 f\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=410.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for crude \\t\"\n",
-    "c=0.485; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "\n",
-    "print\"\\t On the assumption that the fluids are mixed between passes each pass must be solved independently Since only two passes are present in this exchanger it is simply a matter of assuming the temp at the end of the first pass More than half the heat load must be transferred in the first pass therefore assume ti at the end of the first pass is 125 degres f \\n\"\n",
-    "ti=125; # F\n",
-    "tc=((t1)+(ti))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.95*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=4.8*2.42; # at 110F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "c=0.485; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.0775; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu3)/k); # prandelt number\n",
-    "print\"\\t prandelt number is :  \\t\",Pr\n",
-    "Hi=((1.86)*(k/D)*((Ret2*(D/L)*Pr)**(1/3))); # using eq.6.1,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "muw=1.2*2.42; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hi=(Hi)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "tp=(tc)+(((ho)/(hi+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tp is :  F \\t\",tp\n",
-    "delt=tp-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Ai1=0.228 # internal surface per foot of length,ft\n",
-    "Ai=(Nt*L*Ai1/2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",round(Ai,1)\n",
-    "delt3=((hi*Ai*delt)/(W*c)); # delt3=ti-t1, F\n",
-    "print\"\\t delt3 is :  F \\t\",round(delt3,1)\n",
-    "ti=t1+delt3; # F\n",
-    "print\"\\t ti is :  F \\t\",round(ti,1)\n",
-    "print\"The oil now enters the second pass at given 126.9 f\"\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## EXAMPLE 10.2 pgno:207"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for kerosene \t\n",
-      "\t total heat required for kerosene is :  Btu/hr \t400000.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t399946.5\n",
-      "\t delt1 is :  F \t155.0\n",
-      "\t delt2 is :  F \t105.0\n",
-      "\t LMTD is : F \t128.525612445\n",
-      "\t caloric temperature of cold fluid is :  F \t120.0\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,kerosene \t\n",
-      "\t flow area is :  ft**2 \t0.177375\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t90395.480226\n",
-      "\t reynolds number is :  \t1991.27136497\n",
-      "\t reynolds number is :  \t1547.50231792\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t10.2620689655\n",
-      "\t Hio is :  Btu/(hr)*(ft**2)*(F) \t8.928\n",
-      "\t tw is :  F \t249.23081817\n",
-      "\t phyt is :  \t1.16189787585\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t10.3734242356\n",
-      "\t delt is :  F \t129.23081817\n",
-      "\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \t\n",
-      "\t beta is :  /F \t0.000449494949495\n",
-      "\t G is :   \t1289776.29615\n",
-      "\t psy is :   \t0.712464789946\n",
-      "\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \t7.39069951902\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t14.7\n",
-      "\t total surface area is :  ft**2 \t270.1776\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t11.5\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#gien\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=95.; # inlet cold fluid,F\n",
-    "t2=145.; # outlet cold fluid,F\n",
-    "W=16000.; # lb/hr\n",
-    "w=423.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for kerosene \\t\"\n",
-    "c=0.5; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ho=(1500); # condensation of steam Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,kerosene \\t\"\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.594; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(.177)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.36*2.42; # at 145F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret1=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret1\n",
-    "mu3=1.75*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.87/12); # ft\n",
-    "Ret2=((D)*(Gt)/mu3); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret2\n",
-    "Z1=331; # Z1=(L*n/D)\n",
-    "jH=3.1; # from fig 24\n",
-    "mu4=1.75; # cp and 40 API\n",
-    "Z2=0.24; # Z2=((k)*(c*mu4/k)**(1/3)), from fig 16\n",
-    "Hi=((jH)*(1/D)*(Z2)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=(Hi*(ID/OD)); #Btu/(hr)*(ft**2)*(F), from eq.6.5\n",
-    "print\"\\t Hio is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "tw=(tc)+(((ho)/(Hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=1.45; # lb/(ft)*(hr),at 249F from fig.14\n",
-    "phyt=(mu3/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "delt=tw-tc; #F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t Since the kerosene has a viscosity of only 1.75 cp at the caloric temperature and delt=129F, free convection should be investigated. \\t\"\n",
-    "s=0.8;\n",
-    "row=50; # lb/ft**3, from fig 6\n",
-    "s1=0.810; # at 95F\n",
-    "s2=0.792; # at 145F\n",
-    "bita=((s1**2-s2**2)/(2*(t2-t1)*s1*s2)); # /F\n",
-    "print\"\\t beta is :  /F \\t\",bita\n",
-    "G=((D**3)*(row**2)*(bita)*(delt)*(4.18*10**8)/(mu3**2));\n",
-    "print\"\\t G is :   \\t\",G\n",
-    "psy=((2.25)*(1+(0.01*G**(1/3)))/(log10(Ret2)));\n",
-    "print\"\\t psy is :   \\t\",psy\n",
-    "hio1=(hio*psy);\n",
-    "print\"\\t corrected hio1 is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=2*((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(UD,1)\n",
-    "Rd=-0.407*((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.3 pgno:211"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas oil \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t587500.0\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t588101.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t120.0\n",
-      "\t LMTD is : F \t132.254461931\n",
-      "\t caloric temperature of cold fluid is : %.1f F \t117.5\n",
-      "\t hot fluid:shell side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.317708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19577.704918\n",
-      "\t reynolds number is :  \t37409.6272319\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t at1 is :  in**2 \t0.3979165\n",
-      "\t flow area is :  ft**2 \t0.118822288194\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t420796.474801\n",
-      "\t De is :  ft \t0.0485536398467\n",
-      "\t reynolds number is :  \t1223.42517882\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t22.3464194121\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t19.4413848885\n",
-      "\t phyt is :  \t1.18932885404\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t23.1222000104\n",
-      "\t tw is :  F \t247.988545173\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7711867211\n",
-      "\t total surface area is :  ft**2 \t270\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.4694016372\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0168035136331\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t9\n",
-      "\t delPs is :  psi \t1.19559186672\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t dt is :  ft \t0.0308333333333\n",
-      "\t Ret2 is :  \t776.919639103\n",
-      "\t phyt is :  \t1.35\n",
-      "\t delPt is :  psi \t2.0\n",
-      "\t delPr is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=250.; # outlet hot fluid,F\n",
-    "t1=105.; # inlet cold fluid,F\n",
-    "t2=130.; # outlet cold fluid,F\n",
-    "w=50000.; # lb/hr\n",
-    "W=622.; # lb/hr\n",
-    "#solution\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas oil \\t\"\n",
-    "c=0.47; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=945.5; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : %.1f F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,steam \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=15; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2, eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(6220/As); # mass velocity,lb/(hr)*(ft**2), calculation mistake\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0314; # at 250F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.060; # from fig.29,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number, calculation mistake\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "ho=1500; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "d1=0.5; # in\n",
-    "d2=0.87; # in\n",
-    "at1=((3.14*(d2**2-d1**2))/4);\n",
-    "print\"\\t at1 is :  in**2 \\t\",at1\n",
-    "Nt=86;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "De=(d2**2-d1**2)/(12*d2);\n",
-    "print\"\\t De is :  ft \\t\",De\n",
-    "mu2=16.7; # at 117F,lb/(ft)*(hr)\n",
-    "Ret=((De)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=3.1; # from fig.24\n",
-    "Z=0.35; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=6.9cp and 28 API\n",
-    "Hi=((jH)*(1/De)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.87; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "muw=4.84; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is :  \\t\",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(T1-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A=270; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0016; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.00116; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(19600**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "dt=(d2-d1)/(12); # ft\n",
-    "print\"\\t dt is :  ft \\t\",dt\n",
-    "Ret2=(dt*Gt/mu2);\n",
-    "print\"\\t Ret2 is :  \\t\",Ret2\n",
-    "f=0.00066; # friction factor for reynolds number 8220, using fig.26\n",
-    "phyt=1.35; # fig 6\n",
-    "print\"\\t phyt is :  \\t\",phyt\n",
-    "s=0.85;\n",
-    "delPt=((f*(420000**2)*(L)*(n))/(5.22*(10**10)*(0.0309)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 10.4 pgno:217"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 10.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t delt is : F \t100\n",
-      "\t convection loss is :  Btu/(hr)(ft**2)(F) \t0.948683298051\n",
-      "\t radiation loss is :  Btu/(hr)(ft**2)(F) \t0.510696\n",
-      "\t combined loss is :  Btu/(hr)(ft**2)(F) \t1.45937929805\n",
-      "\t total tank area is :  ft**2 \t227.65\n",
-      "\t total heat loss :  Btu/hr \t33222.7697201\n",
-      "\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \t\n",
-      "\t X is :  \t75.7575757576\n",
-      "\t tf is :  F \t156\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t23.9583333333\n",
-      "\t total surface is :  ft**2 \t12.3811564174\n",
-      "\t number of pipes are :  \t7.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 10.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "t1=100; # F\n",
-    "t2=0; # F\n",
-    "T1abs=100+460; # R\n",
-    "T2abs=460; #R\n",
-    "#solution\n",
-    "delt=t1-t2;\n",
-    "from math import ceil\n",
-    "print\"\\t delt is : F \\t\",delt\n",
-    "hc=0.3*(delt**0.25); # convection loss, Btu/(hr)*(ft**2)*( degree F)\n",
-    "print\"\\t convection loss is :  Btu/(hr)(ft**2)(F) \\t\",hc\n",
-    "e=0.8; # emissivity\n",
-    "hr=((0.173*e*((T1abs/100)**4-(T2abs/100)**4))/(T1abs-T2abs)); # radiation rate, from 4.32, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t radiation loss is :  Btu/(hr)(ft**2)(F) \\t\",hr\n",
-    "hl=hc+hr; # combined loss, Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t combined loss is :  Btu/(hr)(ft**2)(F) \\t\",hl\n",
-    "D=5; # ft\n",
-    "L=12; # ft\n",
-    "A1=((2*3.14*D**2)/(4))+(3.14*D*L); # total tank area\n",
-    "print\"\\t total tank area is :  ft**2 \\t\",A1\n",
-    "Q=(hl*A1*delt); # total heat loss\n",
-    "print\"\\t total heat loss :  Btu/hr \\t\",Q\n",
-    "print\"\\t This heat must be supplied by the pipe bundle,Assuming exhaust steam to be at 212 degree F \\t\"\n",
-    "d0=1.32;\n",
-    "X=(delt/d0);\n",
-    "tf=((t1+212)/2); # F\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "hio=48; # from fig 10.4, Btu/(hr)(ft**2)(F)\n",
-    "ho=1500; # condensation of steam,Btu/(hr)(ft**2)(F)\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.02; # dirt factor, (hr)(ft**2)(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A2=((Q)/((UD)*(212-100))); # total surface,ft**2\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A2\n",
-    "A3=2.06; # area/pipe\n",
-    "N=(A2/A3);\n",
-    "print\"\\t number of pipes are :  \\t\",ceil(N)\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions.ipynb
deleted file mode 100755
index c318815e..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions.ipynb
+++ /dev/null
@@ -1,1053 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 11 Calculations for Process Heat Conditions"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example11.1 pgno:231"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for straw oil \t\n",
-      "\t total heat required for straw oil is :  Btu/hr \t1728400.0\n",
-      "\t for naphtha \t\n",
-      "\t total heat required for naphtha is :  Btu/hr \t1730400.0\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t110.0\n",
-      "\t LMTD is  F \t69.2750233163\n",
-      "\t R is :  \t3.33333333333\n",
-      "\t S is :  \t0.214285714286\n",
-      "\t FT is 0.885 \t\n",
-      "\t delt is :  F \t61.3083956349\n",
-      "\t ratio of two local temperature difference is :  \t0.363636363636\n",
-      "\t caloric temperature of hot fluid is :  F \t280.5\n",
-      "\t caloric temperature of cold fluid is :  F \t212.15\n",
-      "\t A1 is :  ft**2 \t403.207419539\n",
-      "\t number of tubes are :\t128.37729863\n",
-      "\t total surface area is :  ft**2 \t389.4592\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.4710556785\n",
-      "\t hot fluid:shell side,straw oil \t\n",
-      "\t flow area is :  ft**2 \t0.0926649305556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t321588.758782\n",
-      "\t reynolds number is :  \t7013.52894497\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t130.155789474\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t130.155789474\n",
-      "\t cold fluid:inner tube side,naphtha \t\n",
-      "\t flow area is :  ft**2 \t0.130027777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t792138.431959\n",
-      "\t reynolds number is :  \t31262.2572002\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t329.477756286\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t272.36827853\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t272.36827853\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t54.8571428571\n",
-      "\t delPs is :  psi \t5.1651098751\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.06675311157\n",
-      "\t clean overall coefficient is : %.1f Btu/(hr)*(ft**2)*(F) \t88.0700339124\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00244401237634\n",
-      "\t The first trial is disqualified because of failure to meet the required dirt factor \t\n",
-      "\t Proceeding as above and carrying the viscosity correction and pressure drops to completion the new summary is given using a 17.25in. ID shell with 166 tubes on two passes and a 3.5in. baffle space \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t74.8\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t54.2\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t delPs is :  psi \t4.7\n",
-      "\t delPt is :  psi \t2.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=340.; # inlet hot fluid,F\n",
-    "T2=240.; # outlet hot fluid,F\n",
-    "t1=200.; # inlet cold fluid,F\n",
-    "t2=230.; # outlet cold fluid,F\n",
-    "W=29800; # lb/hr\n",
-    "w=103000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for straw oil \\t\"\n",
-    "c=0.58; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for straw oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for naphtha \\t\"\n",
-    "c=0.56; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt1=40.;\n",
-    "delt2=T1-t2; # F\n",
-    "delt2=110.\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.885 \\t\" # from fig 18\n",
-    "delt=(0.885*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "L=16;\n",
-    "Fc=0.405; # from fig.17\n",
-    "Kc=0.23; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8a\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(16*a1));\n",
-    "print\"\\t number of tubes are :\\t\",N1\n",
-    "N2=124; # assuming two tube passes, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,straw oil \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=3.5; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=3.63; # at 280.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46; # from fig.28\n",
-    "Z=0.224; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=1.5cp and 35 API\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,naphtha \\t\"\n",
-    "Nt=124;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.31; # at 212F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=102; # from fig.24\n",
-    "Z=0.167; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu4=0.54cp and 48 API\n",
-    "Hi=((jH)*(1/D)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "phyt=1;\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00225; # friction factor for reynolds number 7000, using fig.29\n",
-    "s=0.76; # for reynolds number 7000,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 31300, using fig.26\n",
-    "s=0.72;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : %.1f Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t The first trial is disqualified because of failure to meet the required dirt factor \\t\"\n",
-    "print\"\\t Proceeding as above and carrying the viscosity correction and pressure drops to completion the new summary is given using a 17.25in. ID shell with 166 tubes on two passes and a 3.5in. baffle space \\t\"\n",
-    "UD1=60; # assumption for 2 tube passes,3.5 baffle spacing and 17.25in ID\n",
-    "UC1=74.8;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=54.2;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.005; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "delPs1=4.7;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPt1=2.1;\n",
-    "print\"\\t delPt is :  psi \\t\",delPt1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.2 pgno:235"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lean oil \t\n",
-      "\t total heat required for lean oil is :  Btu/hr \t8984203.2\n",
-      "\t for rich oil \t\n",
-      "\t total heat required for rich oil is :  Btu/hr \t8924995.95\n",
-      "\t Q is :  V \t8954599.575\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t55.0\n",
-      "\t LMTD is : F \t57.5283364148\n",
-      "\t R is :  \t0.974358974359\n",
-      "\t S is :  \t0.78\n",
-      "\t FT is 0.875 \t\n",
-      "\t delt is :  F \t50.337294363\n",
-      "\t ratio of two local temperature difference is :  \t1.09090909091\n",
-      "\t caloric temperature of hot fluid is :  F \t251.2\n",
-      "\t caloric temperature of cold fluid is :  \t193.6\n",
-      "\t A1 is :  ft**2 \t3557.83904889\n",
-      "\t number of tubes are :  \t566.390577064\n",
-      "\t total surface area is :  ft**2 \t3643.328\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t48.8267738849\n",
-      "\t hot fluid:inner tube side,lean oil \t\n",
-      "\t flow area is :  ft**2 \t0.202731481481\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t416501.667047\n",
-      "\t reynolds number is :  \t10109.4536086\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t130.609284333\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t107.970341715\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t107.970341715\n",
-      "\t cold fluid:shell side,rich oil \t\n",
-      "\t flow area is :  ft**2 \t0.322916666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t267428.129032\n",
-      "\t reynolds number is :  \t6721.07731695\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t121.073684211\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t121.073684211\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.32759598913\n",
-      "\t delPr is :  psi \t1.4961038961\n",
-      "\t delPT is :  psi \t5.82369988524\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t64\n",
-      "\t delPs is :  psi \t6.44657740525\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.073599733\n",
-      "\t actual Rd is : %.4f (hr)*(ft**2)*(F)/Btu \t0.00295933089476\n",
-      "\t The initial assumptions have provided an exchanger which very nearly meets all the requirements. Eight-pass units would meet the heat-transfer requirement but would give a tube-side pressure drop of 14 psi. The trial exchanger will be somewhat less suitable when the value of Q, is also taken into account. If the minimum dirt factor of 0.0040 is to be taken literally, it will be necessary to try the next size shell \t\n",
-      "\t Assume a 33 in. ID shell with six1 tube passes and baffies spaced 12-in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t52.3\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0047\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.004\n",
-      "\t delPs is :  psi \t4.4\n",
-      "\t delPt is :  psi \t7.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"   \n",
-    "T1=350.; # inlet hot fluid,F\n",
-    "T2=160.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=295.; # outlet cold fluid,F\n",
-    "W=84438; # lb/hr\n",
-    "w=86357; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lean oil \\t\"\n",
-    "c=0.56; # Btu/(lb)*(F)\n",
-    "Qh=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lean oil is :  Btu/hr \\t\",Qh\n",
-    "print\"\\t for rich oil \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Qc=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for rich oil is :  Btu/hr \\t\",Qc\n",
-    "Q=(Qh+Qc)/(2);\n",
-    "print\"\\t Q is :  V \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.875 \\t\"# for 4-8 exchanger,from fig 21\n",
-    "delt=(0.875*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.48; # from fig.17\n",
-    "Kc=0.32; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "UD1=50; # assume, from table 8a\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(16*a1*2)); # 2-4 exchanger in series\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=580; # assuming six tube passes,31in ID, from table 9\n",
-    "A2=(N2*16*a1*2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:inner tube side,lean oil \\t\"\n",
-    "Nt=580;\n",
-    "n=6; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.13; # at 212F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=36.5; # from fig.24\n",
-    "Z=0.185; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu4=0.88cp and 35 API\n",
-    "Hi=((jH)*(1/D)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "phyt=1;\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,rich oil \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT))/(2); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=3.15; # at 193.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=45; # from fig.28\n",
-    "Z=0.213; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=1.3cp and 35 API\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00027; # friction factor for reynolds number 10100, using fig.26\n",
-    "s=0.77;\n",
-    "delPt=((2*f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.024; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*2*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0023; # friction factor for reynolds number 6720, using fig.29\n",
-    "s=0.79; # for reynolds number 6720,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "De=0.0792;\n",
-    "N=(4*12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : %.4f (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t The initial assumptions have provided an exchanger which very nearly meets all the requirements. Eight-pass units would meet the heat-transfer requirement but would give a tube-side pressure drop of 14 psi. The trial exchanger will be somewhat less suitable when the value of Q, is also taken into account. If the minimum dirt factor of 0.0040 is to be taken literally, it will be necessary to try the next size shell \\t\"\n",
-    "print\"\\t Assume a 33 in. ID shell with six1 tube passes and baffies spaced 12-in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \\t\"\n",
-    "UC1=52.3;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=42;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0047; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.004; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=4.4;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=7.9;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.3 pgno:238"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for caustic \t\n",
-      "\t total heat required for caustic is :  Btu/hr \t6160000.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t6160000.0\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t70.0\n",
-      "\t LMTD is : F \t53.6684619193\n",
-      "\t R is :  \t1.75\n",
-      "\t S is :  \t0.363636363636\n",
-      "\t FT is 0.815 \t\n",
-      "\t delt is :  F \t43.7397964643\n",
-      "\t caloric temperature of hot fluid is :  F \t155.0\n",
-      "\t caloric temperature of cold fluid is :  \t100.0\n",
-      "\t A1 is :  ft**2 \t563.331382215\n",
-      "\t number of tubes are :  \t134.485146633\n",
-      "\t total surface area is :  ft**2 \t586.432\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t240.152047558\n",
-      "\t hot fluid:shell side,caustic \t\n",
-      "\t flow area is :  ft**2 \t0.187152777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t534322.820037\n",
-      "\t reynolds number is :  \t17423.5702186\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t718.75\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t718.75\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.132708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1160439.56044\n",
-      "\t V is  fps \t5.15750915751\n",
-      "\t reynolds number is :  \t46350.8904888\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1165.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t972.1104\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are : %.0f \t28\n",
-      "\t delPs is :  psi \t6.97705175383\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.27604456957\n",
-      "\t delPr is :  psi \t2.88\n",
-      "\t delPT is :  psi \t7.15604456957\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t413.224149078\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00174403453004\n",
-      "\t Adjustment of the baffie space to use the full 10 psi will still not permit the exchanger to make the 0.002 dirt factor. The value of UD has been assumed too high \t\n",
-      "\t Try a 21.25 in ID shell with four tube passes and a 6 in baffie space This corresponds to 170 tubes \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t39\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t200\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0024\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.002\n",
-      "\t delPs is :  psi \t9.8\n",
-      "\t delPt is :  psi \t4.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=190.; # inlet hot fluid,F\n",
-    "T2=120.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=154000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for caustic \\t\"\n",
-    "c=0.88; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for caustic is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.815 \\t\" # for 4-8 exchanger,from fig 21\n",
-    "delt=(0.815*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "UD1=250; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(16*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=140; # assuming four tube passes,19.25in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,caustic \\t\"\n",
-    "ID=19.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.84; # at 155F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.72/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=75; # from fig.28\n",
-    "Z=0.575; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1; # low viscosity\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=140;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=Gt/(3600*62.5);\n",
-    "print\"\\t V is  fps \\t\",V\n",
-    "mu2=1.74; # at 100F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1240*0.94; # from fig 25\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.834; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0019; # friction factor for reynolds number 17400, using fig.29\n",
-    "s=1.115; # for reynolds number 17400,using fig.6\n",
-    "Ds=19.25/12; # ft\n",
-    "De=0.06;\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : %.0f \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00018; # friction factor for reynolds number 46300, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.18; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t Adjustment of the baffie space to use the full 10 psi will still not permit the exchanger to make the 0.002 dirt factor. The value of UD has been assumed too high \\t\"\n",
-    "print\"\\t Try a 21.25 in ID shell with four tube passes and a 6 in baffie space This corresponds to 170 tubes \\t\"\n",
-    "UC1=39\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=200;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0024; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.002; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=9.8;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=4.9;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.4 pgno:241"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9956700\n",
-      "\t for alcohol \t\n",
-      "\t total heat required for alcohol is :  Btu/hr \t9936000.0\n",
-      "\t Q is :  V \t9946350.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t25.0\n",
-      "\t LMTD is : F \t68.3416294443\n",
-      "\t caloric temperature of hot fluid is :  F \t450.0\n",
-      "\t caloric temperature of cold fluid is :  \t280.0\n",
-      "\t A1 is :f ft**2 \t727.693360612\n",
-      "\t number of tubes are :  \t231.631449138\n",
-      "\t total surface area is :  ft**2 \t728.8512\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t199.68228374\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.439833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t23531.640773\n",
-      "\t reynolds number is :  \t52084.3641314\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,alcohol \t\n",
-      "\t flow area is :  ft**2 \t0.226041666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t508755.760369\n",
-      "\t reynolds number is :  \t21051.962498\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t269.75\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t269.75\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.421749731499\n",
-      "\t delPr is negligible \t\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t20\n",
-      "\t delPs is :  psi \t7.39957120534\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t228.633987851\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.000634152640616\n",
-      "\t This is clearly an instance in which UD was assumed too high.It is now a question of how much too high. With the aid of the summary it is apparent thatin a larger shell a clean overall coefficient of about 200 may be expected \t\n",
-      "\t Assume a 27in. ID shell with 2 tube passes,334 tubes and baffies spaced 7in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t214\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t138.5\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.002\n",
-      "\t delPs is :  psi \t0.23\n",
-      "\t delPt is :  psi \t7.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=225.; # inlet hot fluid,F\n",
-    "T2=225.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=200.; # outlet cold fluid,F\n",
-    "W=10350; # lb/hr\n",
-    "w=115000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=962; # Btu/(lb)\n",
-    "Qh=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Qh\n",
-    "print\"\\t for alcohol \\t\"\n",
-    "c=0.72; # Btu/(lb)*(F)\n",
-    "Qc=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for alcohol is :  Btu/hr \\t\",Qc\n",
-    "Q=(Qh+Qc)/(2);\n",
-    "print\"\\t Q is :  V \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1)); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2)); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "L=12;\n",
-    "UD1=200; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :f ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=232; # assuming two tube passes,23.25in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=232;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.0314; # at 225F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,alcohol \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.45; # at 193.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.72/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=83; # from fig.28\n",
-    "Z=0.195; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000175; # friction factor for reynolds number 52000, using fig.26\n",
-    "s=0.00076;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(1)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0018; # friction factor for reynolds number 21000, using fig.29\n",
-    "s=0.78; # for reynolds number 21000,using fig.6\n",
-    "Ds=1.94; # ft\n",
-    "De=0.06;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t This is clearly an instance in which UD was assumed too high.It is now a question of how much too high. With the aid of the summary it is apparent thatin a larger shell a clean overall coefficient of about 200 may be expected \\t\"\n",
-    "print\"\\t Assume a 27in. ID shell with 2 tube passes,334 tubes and baffies spaced 7in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \\t\"\n",
-    "UC1=214;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=138.5;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0025; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.002; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=0.23;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=7.1;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.5 pgno:246"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas \t\n",
-      "\t total heat required for gas is :  Btu/hr \t1290625.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t1290000.0\n",
-      "\t delt1 is :  F \t45.0\n",
-      "\t delt2 is :  F \t150.0\n",
-      "\t LMTD is : F \t87.3092936462\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.117647058824\n",
-      "\t FT is 0.935 \t\n",
-      "\t delt is :  F \t81.6341895592\n",
-      "\t caloric temperature of hot fluid is :  F \t187.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t A1 is :  ft**2 \t1067.71638982\n",
-      "\t number of tubes are :  \t339.863887771\n",
-      "\t total surface area is :  ft**2 \t1124.6928\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14.0502389358\n",
-      "\t When solved in a manner identical with the preceding examples and using the smallest integral number of bundle crosses (five) corresponding to a 28.8 in spacing \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.027\n",
-      "\t required Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t delPs is :  psi \t5.2\n",
-      "\t delPt is :  psi \t1.0\n",
-      "\t The first trial is disqualified because of failure to meet the required dirt factor and the the pressure drop is five times greater than the allowable \t\n",
-      "\t This would be unsatisfactory, since gases require large inlet connections and the flow distribution on the first and third bundle crosses would be poor and the conditions of allowable pressure drop would still not be met \t\n",
-      "\t A1 is :  ft**2 \t1053.48017129\n",
-      "\t number of tubes are : %. \t335.332369267\n",
-      "\t total surface area is :  ft**2 \t1068.144\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14.7940751147\n",
-      "\t hot fluid:shell side,gas \t\n",
-      "\t flow area is :  ft**2 \t1.03333333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19983.8709677\n",
-      "\t reynolds number is :  \t32973.3870968\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t17.9454545455\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t17.9454545455\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.107430555556\n",
-      "\t mass velocity is : %lb/(hr)*(ft**2) \t600387.847447\n",
-      "\t V is :  fps \t2.6683904331\n",
-      "\t reynolds number is :  \t21289.2629579\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t667\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t553.61\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.788231357313\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.14770229996\n",
-      "\t delPr is :  psi \t2.496\n",
-      "\t delPT is :  psi \t5.64370229996\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t17.4\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0099\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=41300.; # lb/hr\n",
-    "w=64500.; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas \\t\"\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.935 \\t\" # from fig 18\n",
-    "delt=(0.935*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=14.8; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=358; # assuming 12 tube passes, from table 9\n",
-    "L=12;\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t When solved in a manner identical with the preceding examples and using the smallest integral number of bundle crosses (five) corresponding to a 28.8 in spacing \\t\"\n",
-    "UC1=22.7;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=14;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.027; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd1=0.005; \n",
-    "print\"\\t required Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "delPs1=5.2;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPt1=1.0;\n",
-    "print\"\\t delPt is :  psi \\t\",delPt1\n",
-    "print\"\\t The first trial is disqualified because of failure to meet the required dirt factor and the the pressure drop is five times greater than the allowable \\t\"\n",
-    "print\"\\t This would be unsatisfactory, since gases require large inlet connections and the flow distribution on the first and third bundle crosses would be poor and the conditions of allowable pressure drop would still not be met \\t\"\n",
-    "UD1=15; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are : %. \\t\",N1\n",
-    "N2=340; # assuming eight tube passes, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,gas \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.25; # clearance\n",
-    "B=24; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As)/(2); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.050; # at 187.5F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=105; # from fig.28\n",
-    "k=0.015; # Btu/(hr)(ft**2)( degree F/ft)\n",
-    "Z=0.94; # Z=((c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "Nt=340;\n",
-    "n=12; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : %lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.96; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=667; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.83; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "phyt=1;\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 33000, using fig.29\n",
-    "s=0.0012; # for reynolds number 33000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 21300, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.052; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=-1*(((Uc-UD)/((UD)*(Uc)))-0.02); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions_1.ipynb
deleted file mode 100755
index c318815e..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions_1.ipynb
+++ /dev/null
@@ -1,1053 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 11 Calculations for Process Heat Conditions"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example11.1 pgno:231"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for straw oil \t\n",
-      "\t total heat required for straw oil is :  Btu/hr \t1728400.0\n",
-      "\t for naphtha \t\n",
-      "\t total heat required for naphtha is :  Btu/hr \t1730400.0\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t110.0\n",
-      "\t LMTD is  F \t69.2750233163\n",
-      "\t R is :  \t3.33333333333\n",
-      "\t S is :  \t0.214285714286\n",
-      "\t FT is 0.885 \t\n",
-      "\t delt is :  F \t61.3083956349\n",
-      "\t ratio of two local temperature difference is :  \t0.363636363636\n",
-      "\t caloric temperature of hot fluid is :  F \t280.5\n",
-      "\t caloric temperature of cold fluid is :  F \t212.15\n",
-      "\t A1 is :  ft**2 \t403.207419539\n",
-      "\t number of tubes are :\t128.37729863\n",
-      "\t total surface area is :  ft**2 \t389.4592\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.4710556785\n",
-      "\t hot fluid:shell side,straw oil \t\n",
-      "\t flow area is :  ft**2 \t0.0926649305556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t321588.758782\n",
-      "\t reynolds number is :  \t7013.52894497\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t130.155789474\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t130.155789474\n",
-      "\t cold fluid:inner tube side,naphtha \t\n",
-      "\t flow area is :  ft**2 \t0.130027777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t792138.431959\n",
-      "\t reynolds number is :  \t31262.2572002\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t329.477756286\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t272.36827853\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t272.36827853\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t54.8571428571\n",
-      "\t delPs is :  psi \t5.1651098751\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.06675311157\n",
-      "\t clean overall coefficient is : %.1f Btu/(hr)*(ft**2)*(F) \t88.0700339124\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00244401237634\n",
-      "\t The first trial is disqualified because of failure to meet the required dirt factor \t\n",
-      "\t Proceeding as above and carrying the viscosity correction and pressure drops to completion the new summary is given using a 17.25in. ID shell with 166 tubes on two passes and a 3.5in. baffle space \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t74.8\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t54.2\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t delPs is :  psi \t4.7\n",
-      "\t delPt is :  psi \t2.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=340.; # inlet hot fluid,F\n",
-    "T2=240.; # outlet hot fluid,F\n",
-    "t1=200.; # inlet cold fluid,F\n",
-    "t2=230.; # outlet cold fluid,F\n",
-    "W=29800; # lb/hr\n",
-    "w=103000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for straw oil \\t\"\n",
-    "c=0.58; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for straw oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for naphtha \\t\"\n",
-    "c=0.56; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt1=40.;\n",
-    "delt2=T1-t2; # F\n",
-    "delt2=110.\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.885 \\t\" # from fig 18\n",
-    "delt=(0.885*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "L=16;\n",
-    "Fc=0.405; # from fig.17\n",
-    "Kc=0.23; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8a\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(16*a1));\n",
-    "print\"\\t number of tubes are :\\t\",N1\n",
-    "N2=124; # assuming two tube passes, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,straw oil \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=3.5; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=3.63; # at 280.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46; # from fig.28\n",
-    "Z=0.224; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=1.5cp and 35 API\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,naphtha \\t\"\n",
-    "Nt=124;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.31; # at 212F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=102; # from fig.24\n",
-    "Z=0.167; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu4=0.54cp and 48 API\n",
-    "Hi=((jH)*(1/D)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "phyt=1;\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00225; # friction factor for reynolds number 7000, using fig.29\n",
-    "s=0.76; # for reynolds number 7000,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 31300, using fig.26\n",
-    "s=0.72;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : %.1f Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t The first trial is disqualified because of failure to meet the required dirt factor \\t\"\n",
-    "print\"\\t Proceeding as above and carrying the viscosity correction and pressure drops to completion the new summary is given using a 17.25in. ID shell with 166 tubes on two passes and a 3.5in. baffle space \\t\"\n",
-    "UD1=60; # assumption for 2 tube passes,3.5 baffle spacing and 17.25in ID\n",
-    "UC1=74.8;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=54.2;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.005; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "delPs1=4.7;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPt1=2.1;\n",
-    "print\"\\t delPt is :  psi \\t\",delPt1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.2 pgno:235"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lean oil \t\n",
-      "\t total heat required for lean oil is :  Btu/hr \t8984203.2\n",
-      "\t for rich oil \t\n",
-      "\t total heat required for rich oil is :  Btu/hr \t8924995.95\n",
-      "\t Q is :  V \t8954599.575\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t55.0\n",
-      "\t LMTD is : F \t57.5283364148\n",
-      "\t R is :  \t0.974358974359\n",
-      "\t S is :  \t0.78\n",
-      "\t FT is 0.875 \t\n",
-      "\t delt is :  F \t50.337294363\n",
-      "\t ratio of two local temperature difference is :  \t1.09090909091\n",
-      "\t caloric temperature of hot fluid is :  F \t251.2\n",
-      "\t caloric temperature of cold fluid is :  \t193.6\n",
-      "\t A1 is :  ft**2 \t3557.83904889\n",
-      "\t number of tubes are :  \t566.390577064\n",
-      "\t total surface area is :  ft**2 \t3643.328\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t48.8267738849\n",
-      "\t hot fluid:inner tube side,lean oil \t\n",
-      "\t flow area is :  ft**2 \t0.202731481481\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t416501.667047\n",
-      "\t reynolds number is :  \t10109.4536086\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t130.609284333\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t107.970341715\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t107.970341715\n",
-      "\t cold fluid:shell side,rich oil \t\n",
-      "\t flow area is :  ft**2 \t0.322916666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t267428.129032\n",
-      "\t reynolds number is :  \t6721.07731695\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t121.073684211\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t121.073684211\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.32759598913\n",
-      "\t delPr is :  psi \t1.4961038961\n",
-      "\t delPT is :  psi \t5.82369988524\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t64\n",
-      "\t delPs is :  psi \t6.44657740525\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.073599733\n",
-      "\t actual Rd is : %.4f (hr)*(ft**2)*(F)/Btu \t0.00295933089476\n",
-      "\t The initial assumptions have provided an exchanger which very nearly meets all the requirements. Eight-pass units would meet the heat-transfer requirement but would give a tube-side pressure drop of 14 psi. The trial exchanger will be somewhat less suitable when the value of Q, is also taken into account. If the minimum dirt factor of 0.0040 is to be taken literally, it will be necessary to try the next size shell \t\n",
-      "\t Assume a 33 in. ID shell with six1 tube passes and baffies spaced 12-in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t52.3\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0047\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.004\n",
-      "\t delPs is :  psi \t4.4\n",
-      "\t delPt is :  psi \t7.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"   \n",
-    "T1=350.; # inlet hot fluid,F\n",
-    "T2=160.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=295.; # outlet cold fluid,F\n",
-    "W=84438; # lb/hr\n",
-    "w=86357; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lean oil \\t\"\n",
-    "c=0.56; # Btu/(lb)*(F)\n",
-    "Qh=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lean oil is :  Btu/hr \\t\",Qh\n",
-    "print\"\\t for rich oil \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Qc=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for rich oil is :  Btu/hr \\t\",Qc\n",
-    "Q=(Qh+Qc)/(2);\n",
-    "print\"\\t Q is :  V \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.875 \\t\"# for 4-8 exchanger,from fig 21\n",
-    "delt=(0.875*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.48; # from fig.17\n",
-    "Kc=0.32; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "UD1=50; # assume, from table 8a\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(16*a1*2)); # 2-4 exchanger in series\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=580; # assuming six tube passes,31in ID, from table 9\n",
-    "A2=(N2*16*a1*2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:inner tube side,lean oil \\t\"\n",
-    "Nt=580;\n",
-    "n=6; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.13; # at 212F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=36.5; # from fig.24\n",
-    "Z=0.185; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu4=0.88cp and 35 API\n",
-    "Hi=((jH)*(1/D)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "phyt=1;\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,rich oil \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT))/(2); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=3.15; # at 193.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=45; # from fig.28\n",
-    "Z=0.213; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=1.3cp and 35 API\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00027; # friction factor for reynolds number 10100, using fig.26\n",
-    "s=0.77;\n",
-    "delPt=((2*f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.024; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*2*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0023; # friction factor for reynolds number 6720, using fig.29\n",
-    "s=0.79; # for reynolds number 6720,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "De=0.0792;\n",
-    "N=(4*12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : %.4f (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t The initial assumptions have provided an exchanger which very nearly meets all the requirements. Eight-pass units would meet the heat-transfer requirement but would give a tube-side pressure drop of 14 psi. The trial exchanger will be somewhat less suitable when the value of Q, is also taken into account. If the minimum dirt factor of 0.0040 is to be taken literally, it will be necessary to try the next size shell \\t\"\n",
-    "print\"\\t Assume a 33 in. ID shell with six1 tube passes and baffies spaced 12-in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \\t\"\n",
-    "UC1=52.3;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=42;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0047; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.004; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=4.4;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=7.9;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.3 pgno:238"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for caustic \t\n",
-      "\t total heat required for caustic is :  Btu/hr \t6160000.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t6160000.0\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t70.0\n",
-      "\t LMTD is : F \t53.6684619193\n",
-      "\t R is :  \t1.75\n",
-      "\t S is :  \t0.363636363636\n",
-      "\t FT is 0.815 \t\n",
-      "\t delt is :  F \t43.7397964643\n",
-      "\t caloric temperature of hot fluid is :  F \t155.0\n",
-      "\t caloric temperature of cold fluid is :  \t100.0\n",
-      "\t A1 is :  ft**2 \t563.331382215\n",
-      "\t number of tubes are :  \t134.485146633\n",
-      "\t total surface area is :  ft**2 \t586.432\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t240.152047558\n",
-      "\t hot fluid:shell side,caustic \t\n",
-      "\t flow area is :  ft**2 \t0.187152777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t534322.820037\n",
-      "\t reynolds number is :  \t17423.5702186\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t718.75\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t718.75\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.132708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1160439.56044\n",
-      "\t V is  fps \t5.15750915751\n",
-      "\t reynolds number is :  \t46350.8904888\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1165.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t972.1104\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are : %.0f \t28\n",
-      "\t delPs is :  psi \t6.97705175383\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.27604456957\n",
-      "\t delPr is :  psi \t2.88\n",
-      "\t delPT is :  psi \t7.15604456957\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t413.224149078\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00174403453004\n",
-      "\t Adjustment of the baffie space to use the full 10 psi will still not permit the exchanger to make the 0.002 dirt factor. The value of UD has been assumed too high \t\n",
-      "\t Try a 21.25 in ID shell with four tube passes and a 6 in baffie space This corresponds to 170 tubes \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t39\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t200\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0024\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.002\n",
-      "\t delPs is :  psi \t9.8\n",
-      "\t delPt is :  psi \t4.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=190.; # inlet hot fluid,F\n",
-    "T2=120.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=154000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for caustic \\t\"\n",
-    "c=0.88; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for caustic is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.815 \\t\" # for 4-8 exchanger,from fig 21\n",
-    "delt=(0.815*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "UD1=250; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(16*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=140; # assuming four tube passes,19.25in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,caustic \\t\"\n",
-    "ID=19.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.84; # at 155F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.72/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=75; # from fig.28\n",
-    "Z=0.575; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1; # low viscosity\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=140;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=Gt/(3600*62.5);\n",
-    "print\"\\t V is  fps \\t\",V\n",
-    "mu2=1.74; # at 100F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1240*0.94; # from fig 25\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.834; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0019; # friction factor for reynolds number 17400, using fig.29\n",
-    "s=1.115; # for reynolds number 17400,using fig.6\n",
-    "Ds=19.25/12; # ft\n",
-    "De=0.06;\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : %.0f \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00018; # friction factor for reynolds number 46300, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.18; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t Adjustment of the baffie space to use the full 10 psi will still not permit the exchanger to make the 0.002 dirt factor. The value of UD has been assumed too high \\t\"\n",
-    "print\"\\t Try a 21.25 in ID shell with four tube passes and a 6 in baffie space This corresponds to 170 tubes \\t\"\n",
-    "UC1=39\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=200;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0024; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.002; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=9.8;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=4.9;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.4 pgno:241"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9956700\n",
-      "\t for alcohol \t\n",
-      "\t total heat required for alcohol is :  Btu/hr \t9936000.0\n",
-      "\t Q is :  V \t9946350.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t25.0\n",
-      "\t LMTD is : F \t68.3416294443\n",
-      "\t caloric temperature of hot fluid is :  F \t450.0\n",
-      "\t caloric temperature of cold fluid is :  \t280.0\n",
-      "\t A1 is :f ft**2 \t727.693360612\n",
-      "\t number of tubes are :  \t231.631449138\n",
-      "\t total surface area is :  ft**2 \t728.8512\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t199.68228374\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.439833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t23531.640773\n",
-      "\t reynolds number is :  \t52084.3641314\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,alcohol \t\n",
-      "\t flow area is :  ft**2 \t0.226041666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t508755.760369\n",
-      "\t reynolds number is :  \t21051.962498\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t269.75\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t269.75\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.421749731499\n",
-      "\t delPr is negligible \t\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t20\n",
-      "\t delPs is :  psi \t7.39957120534\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t228.633987851\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.000634152640616\n",
-      "\t This is clearly an instance in which UD was assumed too high.It is now a question of how much too high. With the aid of the summary it is apparent thatin a larger shell a clean overall coefficient of about 200 may be expected \t\n",
-      "\t Assume a 27in. ID shell with 2 tube passes,334 tubes and baffies spaced 7in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t214\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t138.5\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.002\n",
-      "\t delPs is :  psi \t0.23\n",
-      "\t delPt is :  psi \t7.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=225.; # inlet hot fluid,F\n",
-    "T2=225.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=200.; # outlet cold fluid,F\n",
-    "W=10350; # lb/hr\n",
-    "w=115000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=962; # Btu/(lb)\n",
-    "Qh=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Qh\n",
-    "print\"\\t for alcohol \\t\"\n",
-    "c=0.72; # Btu/(lb)*(F)\n",
-    "Qc=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for alcohol is :  Btu/hr \\t\",Qc\n",
-    "Q=(Qh+Qc)/(2);\n",
-    "print\"\\t Q is :  V \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1)); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2)); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "L=12;\n",
-    "UD1=200; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :f ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=232; # assuming two tube passes,23.25in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=232;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.0314; # at 225F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,alcohol \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.45; # at 193.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.72/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=83; # from fig.28\n",
-    "Z=0.195; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000175; # friction factor for reynolds number 52000, using fig.26\n",
-    "s=0.00076;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(1)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0018; # friction factor for reynolds number 21000, using fig.29\n",
-    "s=0.78; # for reynolds number 21000,using fig.6\n",
-    "Ds=1.94; # ft\n",
-    "De=0.06;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t This is clearly an instance in which UD was assumed too high.It is now a question of how much too high. With the aid of the summary it is apparent thatin a larger shell a clean overall coefficient of about 200 may be expected \\t\"\n",
-    "print\"\\t Assume a 27in. ID shell with 2 tube passes,334 tubes and baffies spaced 7in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \\t\"\n",
-    "UC1=214;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=138.5;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0025; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.002; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=0.23;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=7.1;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.5 pgno:246"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas \t\n",
-      "\t total heat required for gas is :  Btu/hr \t1290625.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t1290000.0\n",
-      "\t delt1 is :  F \t45.0\n",
-      "\t delt2 is :  F \t150.0\n",
-      "\t LMTD is : F \t87.3092936462\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.117647058824\n",
-      "\t FT is 0.935 \t\n",
-      "\t delt is :  F \t81.6341895592\n",
-      "\t caloric temperature of hot fluid is :  F \t187.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t A1 is :  ft**2 \t1067.71638982\n",
-      "\t number of tubes are :  \t339.863887771\n",
-      "\t total surface area is :  ft**2 \t1124.6928\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14.0502389358\n",
-      "\t When solved in a manner identical with the preceding examples and using the smallest integral number of bundle crosses (five) corresponding to a 28.8 in spacing \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.027\n",
-      "\t required Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t delPs is :  psi \t5.2\n",
-      "\t delPt is :  psi \t1.0\n",
-      "\t The first trial is disqualified because of failure to meet the required dirt factor and the the pressure drop is five times greater than the allowable \t\n",
-      "\t This would be unsatisfactory, since gases require large inlet connections and the flow distribution on the first and third bundle crosses would be poor and the conditions of allowable pressure drop would still not be met \t\n",
-      "\t A1 is :  ft**2 \t1053.48017129\n",
-      "\t number of tubes are : %. \t335.332369267\n",
-      "\t total surface area is :  ft**2 \t1068.144\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14.7940751147\n",
-      "\t hot fluid:shell side,gas \t\n",
-      "\t flow area is :  ft**2 \t1.03333333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19983.8709677\n",
-      "\t reynolds number is :  \t32973.3870968\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t17.9454545455\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t17.9454545455\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.107430555556\n",
-      "\t mass velocity is : %lb/(hr)*(ft**2) \t600387.847447\n",
-      "\t V is :  fps \t2.6683904331\n",
-      "\t reynolds number is :  \t21289.2629579\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t667\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t553.61\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.788231357313\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.14770229996\n",
-      "\t delPr is :  psi \t2.496\n",
-      "\t delPT is :  psi \t5.64370229996\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t17.4\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0099\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=41300.; # lb/hr\n",
-    "w=64500.; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas \\t\"\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.935 \\t\" # from fig 18\n",
-    "delt=(0.935*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=14.8; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=358; # assuming 12 tube passes, from table 9\n",
-    "L=12;\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t When solved in a manner identical with the preceding examples and using the smallest integral number of bundle crosses (five) corresponding to a 28.8 in spacing \\t\"\n",
-    "UC1=22.7;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=14;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.027; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd1=0.005; \n",
-    "print\"\\t required Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "delPs1=5.2;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPt1=1.0;\n",
-    "print\"\\t delPt is :  psi \\t\",delPt1\n",
-    "print\"\\t The first trial is disqualified because of failure to meet the required dirt factor and the the pressure drop is five times greater than the allowable \\t\"\n",
-    "print\"\\t This would be unsatisfactory, since gases require large inlet connections and the flow distribution on the first and third bundle crosses would be poor and the conditions of allowable pressure drop would still not be met \\t\"\n",
-    "UD1=15; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are : %. \\t\",N1\n",
-    "N2=340; # assuming eight tube passes, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,gas \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.25; # clearance\n",
-    "B=24; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As)/(2); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.050; # at 187.5F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=105; # from fig.28\n",
-    "k=0.015; # Btu/(hr)(ft**2)( degree F/ft)\n",
-    "Z=0.94; # Z=((c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "Nt=340;\n",
-    "n=12; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : %lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.96; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=667; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.83; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "phyt=1;\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 33000, using fig.29\n",
-    "s=0.0012; # for reynolds number 33000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 21300, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.052; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=-1*(((Uc-UD)/((UD)*(Uc)))-0.02); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions_2.ipynb
deleted file mode 100755
index c318815e..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Calculations_for_Process_Heat_Conditions_2.ipynb
+++ /dev/null
@@ -1,1053 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 11 Calculations for Process Heat Conditions"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example11.1 pgno:231"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for straw oil \t\n",
-      "\t total heat required for straw oil is :  Btu/hr \t1728400.0\n",
-      "\t for naphtha \t\n",
-      "\t total heat required for naphtha is :  Btu/hr \t1730400.0\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t110.0\n",
-      "\t LMTD is  F \t69.2750233163\n",
-      "\t R is :  \t3.33333333333\n",
-      "\t S is :  \t0.214285714286\n",
-      "\t FT is 0.885 \t\n",
-      "\t delt is :  F \t61.3083956349\n",
-      "\t ratio of two local temperature difference is :  \t0.363636363636\n",
-      "\t caloric temperature of hot fluid is :  F \t280.5\n",
-      "\t caloric temperature of cold fluid is :  F \t212.15\n",
-      "\t A1 is :  ft**2 \t403.207419539\n",
-      "\t number of tubes are :\t128.37729863\n",
-      "\t total surface area is :  ft**2 \t389.4592\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.4710556785\n",
-      "\t hot fluid:shell side,straw oil \t\n",
-      "\t flow area is :  ft**2 \t0.0926649305556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t321588.758782\n",
-      "\t reynolds number is :  \t7013.52894497\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t130.155789474\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t130.155789474\n",
-      "\t cold fluid:inner tube side,naphtha \t\n",
-      "\t flow area is :  ft**2 \t0.130027777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t792138.431959\n",
-      "\t reynolds number is :  \t31262.2572002\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t329.477756286\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t272.36827853\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t272.36827853\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t54.8571428571\n",
-      "\t delPs is :  psi \t5.1651098751\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.06675311157\n",
-      "\t clean overall coefficient is : %.1f Btu/(hr)*(ft**2)*(F) \t88.0700339124\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00244401237634\n",
-      "\t The first trial is disqualified because of failure to meet the required dirt factor \t\n",
-      "\t Proceeding as above and carrying the viscosity correction and pressure drops to completion the new summary is given using a 17.25in. ID shell with 166 tubes on two passes and a 3.5in. baffle space \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t74.8\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t54.2\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t delPs is :  psi \t4.7\n",
-      "\t delPt is :  psi \t2.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=340.; # inlet hot fluid,F\n",
-    "T2=240.; # outlet hot fluid,F\n",
-    "t1=200.; # inlet cold fluid,F\n",
-    "t2=230.; # outlet cold fluid,F\n",
-    "W=29800; # lb/hr\n",
-    "w=103000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for straw oil \\t\"\n",
-    "c=0.58; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for straw oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for naphtha \\t\"\n",
-    "c=0.56; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt1=40.;\n",
-    "delt2=T1-t2; # F\n",
-    "delt2=110.\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.885 \\t\" # from fig 18\n",
-    "delt=(0.885*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "L=16;\n",
-    "Fc=0.405; # from fig.17\n",
-    "Kc=0.23; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8a\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(16*a1));\n",
-    "print\"\\t number of tubes are :\\t\",N1\n",
-    "N2=124; # assuming two tube passes, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,straw oil \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=3.5; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=3.63; # at 280.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46; # from fig.28\n",
-    "Z=0.224; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=1.5cp and 35 API\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,naphtha \\t\"\n",
-    "Nt=124;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=1.31; # at 212F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=102; # from fig.24\n",
-    "Z=0.167; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu4=0.54cp and 48 API\n",
-    "Hi=((jH)*(1/D)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "phyt=1;\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00225; # friction factor for reynolds number 7000, using fig.29\n",
-    "s=0.76; # for reynolds number 7000,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 31300, using fig.26\n",
-    "s=0.72;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : %.1f Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t The first trial is disqualified because of failure to meet the required dirt factor \\t\"\n",
-    "print\"\\t Proceeding as above and carrying the viscosity correction and pressure drops to completion the new summary is given using a 17.25in. ID shell with 166 tubes on two passes and a 3.5in. baffle space \\t\"\n",
-    "UD1=60; # assumption for 2 tube passes,3.5 baffle spacing and 17.25in ID\n",
-    "UC1=74.8;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=54.2;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.005; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "delPs1=4.7;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPt1=2.1;\n",
-    "print\"\\t delPt is :  psi \\t\",delPt1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.2 pgno:235"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lean oil \t\n",
-      "\t total heat required for lean oil is :  Btu/hr \t8984203.2\n",
-      "\t for rich oil \t\n",
-      "\t total heat required for rich oil is :  Btu/hr \t8924995.95\n",
-      "\t Q is :  V \t8954599.575\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t55.0\n",
-      "\t LMTD is : F \t57.5283364148\n",
-      "\t R is :  \t0.974358974359\n",
-      "\t S is :  \t0.78\n",
-      "\t FT is 0.875 \t\n",
-      "\t delt is :  F \t50.337294363\n",
-      "\t ratio of two local temperature difference is :  \t1.09090909091\n",
-      "\t caloric temperature of hot fluid is :  F \t251.2\n",
-      "\t caloric temperature of cold fluid is :  \t193.6\n",
-      "\t A1 is :  ft**2 \t3557.83904889\n",
-      "\t number of tubes are :  \t566.390577064\n",
-      "\t total surface area is :  ft**2 \t3643.328\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t48.8267738849\n",
-      "\t hot fluid:inner tube side,lean oil \t\n",
-      "\t flow area is :  ft**2 \t0.202731481481\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t416501.667047\n",
-      "\t reynolds number is :  \t10109.4536086\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t130.609284333\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t107.970341715\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t107.970341715\n",
-      "\t cold fluid:shell side,rich oil \t\n",
-      "\t flow area is :  ft**2 \t0.322916666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t267428.129032\n",
-      "\t reynolds number is :  \t6721.07731695\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t121.073684211\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t121.073684211\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.32759598913\n",
-      "\t delPr is :  psi \t1.4961038961\n",
-      "\t delPT is :  psi \t5.82369988524\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t64\n",
-      "\t delPs is :  psi \t6.44657740525\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.073599733\n",
-      "\t actual Rd is : %.4f (hr)*(ft**2)*(F)/Btu \t0.00295933089476\n",
-      "\t The initial assumptions have provided an exchanger which very nearly meets all the requirements. Eight-pass units would meet the heat-transfer requirement but would give a tube-side pressure drop of 14 psi. The trial exchanger will be somewhat less suitable when the value of Q, is also taken into account. If the minimum dirt factor of 0.0040 is to be taken literally, it will be necessary to try the next size shell \t\n",
-      "\t Assume a 33 in. ID shell with six1 tube passes and baffies spaced 12-in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t52.3\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0047\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.004\n",
-      "\t delPs is :  psi \t4.4\n",
-      "\t delPt is :  psi \t7.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"   \n",
-    "T1=350.; # inlet hot fluid,F\n",
-    "T2=160.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=295.; # outlet cold fluid,F\n",
-    "W=84438; # lb/hr\n",
-    "w=86357; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lean oil \\t\"\n",
-    "c=0.56; # Btu/(lb)*(F)\n",
-    "Qh=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lean oil is :  Btu/hr \\t\",Qh\n",
-    "print\"\\t for rich oil \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Qc=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for rich oil is :  Btu/hr \\t\",Qc\n",
-    "Q=(Qh+Qc)/(2);\n",
-    "print\"\\t Q is :  V \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.875 \\t\"# for 4-8 exchanger,from fig 21\n",
-    "delt=(0.875*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.48; # from fig.17\n",
-    "Kc=0.32; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "UD1=50; # assume, from table 8a\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(16*a1*2)); # 2-4 exchanger in series\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=580; # assuming six tube passes,31in ID, from table 9\n",
-    "A2=(N2*16*a1*2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:inner tube side,lean oil \\t\"\n",
-    "Nt=580;\n",
-    "n=6; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=2.13; # at 212F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=36.5; # from fig.24\n",
-    "Z=0.185; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu4=0.88cp and 35 API\n",
-    "Hi=((jH)*(1/D)*(Z)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "phyt=1;\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,rich oil \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT))/(2); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=3.15; # at 193.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=45; # from fig.28\n",
-    "Z=0.213; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft), at mu3=1.3cp and 35 API\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00027; # friction factor for reynolds number 10100, using fig.26\n",
-    "s=0.77;\n",
-    "delPt=((2*f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.024; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*2*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0023; # friction factor for reynolds number 6720, using fig.29\n",
-    "s=0.79; # for reynolds number 6720,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "De=0.0792;\n",
-    "N=(4*12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : %.4f (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t The initial assumptions have provided an exchanger which very nearly meets all the requirements. Eight-pass units would meet the heat-transfer requirement but would give a tube-side pressure drop of 14 psi. The trial exchanger will be somewhat less suitable when the value of Q, is also taken into account. If the minimum dirt factor of 0.0040 is to be taken literally, it will be necessary to try the next size shell \\t\"\n",
-    "print\"\\t Assume a 33 in. ID shell with six1 tube passes and baffies spaced 12-in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \\t\"\n",
-    "UC1=52.3;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=42;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0047; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.004; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=4.4;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=7.9;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.3 pgno:238"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for caustic \t\n",
-      "\t total heat required for caustic is :  Btu/hr \t6160000.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t6160000.0\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t70.0\n",
-      "\t LMTD is : F \t53.6684619193\n",
-      "\t R is :  \t1.75\n",
-      "\t S is :  \t0.363636363636\n",
-      "\t FT is 0.815 \t\n",
-      "\t delt is :  F \t43.7397964643\n",
-      "\t caloric temperature of hot fluid is :  F \t155.0\n",
-      "\t caloric temperature of cold fluid is :  \t100.0\n",
-      "\t A1 is :  ft**2 \t563.331382215\n",
-      "\t number of tubes are :  \t134.485146633\n",
-      "\t total surface area is :  ft**2 \t586.432\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t240.152047558\n",
-      "\t hot fluid:shell side,caustic \t\n",
-      "\t flow area is :  ft**2 \t0.187152777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t534322.820037\n",
-      "\t reynolds number is :  \t17423.5702186\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t718.75\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t718.75\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.132708333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1160439.56044\n",
-      "\t V is  fps \t5.15750915751\n",
-      "\t reynolds number is :  \t46350.8904888\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t1165.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t972.1104\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are : %.0f \t28\n",
-      "\t delPs is :  psi \t6.97705175383\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.27604456957\n",
-      "\t delPr is :  psi \t2.88\n",
-      "\t delPT is :  psi \t7.15604456957\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t413.224149078\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00174403453004\n",
-      "\t Adjustment of the baffie space to use the full 10 psi will still not permit the exchanger to make the 0.002 dirt factor. The value of UD has been assumed too high \t\n",
-      "\t Try a 21.25 in ID shell with four tube passes and a 6 in baffie space This corresponds to 170 tubes \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t39\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t200\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0024\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.002\n",
-      "\t delPs is :  psi \t9.8\n",
-      "\t delPt is :  psi \t4.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=190.; # inlet hot fluid,F\n",
-    "T2=120.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=154000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for caustic \\t\"\n",
-    "c=0.88; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for caustic is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.815 \\t\" # for 4-8 exchanger,from fig 21\n",
-    "delt=(0.815*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "UD1=250; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(16*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=140; # assuming four tube passes,19.25in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,caustic \\t\"\n",
-    "ID=19.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.84; # at 155F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.72/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=75; # from fig.28\n",
-    "Z=0.575; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1; # low viscosity\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=140;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=Gt/(3600*62.5);\n",
-    "print\"\\t V is  fps \\t\",V\n",
-    "mu2=1.74; # at 100F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1240*0.94; # from fig 25\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.834; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0019; # friction factor for reynolds number 17400, using fig.29\n",
-    "s=1.115; # for reynolds number 17400,using fig.6\n",
-    "Ds=19.25/12; # ft\n",
-    "De=0.06;\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : %.0f \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00018; # friction factor for reynolds number 46300, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.18; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t Adjustment of the baffie space to use the full 10 psi will still not permit the exchanger to make the 0.002 dirt factor. The value of UD has been assumed too high \\t\"\n",
-    "print\"\\t Try a 21.25 in ID shell with four tube passes and a 6 in baffie space This corresponds to 170 tubes \\t\"\n",
-    "UC1=39\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=200;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0024; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.002; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=9.8;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=4.9;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.4 pgno:241"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9956700\n",
-      "\t for alcohol \t\n",
-      "\t total heat required for alcohol is :  Btu/hr \t9936000.0\n",
-      "\t Q is :  V \t9946350.0\n",
-      "\t delt1 is :  F \t145.0\n",
-      "\t delt2 is :  F \t25.0\n",
-      "\t LMTD is : F \t68.3416294443\n",
-      "\t caloric temperature of hot fluid is :  F \t450.0\n",
-      "\t caloric temperature of cold fluid is :  \t280.0\n",
-      "\t A1 is :f ft**2 \t727.693360612\n",
-      "\t number of tubes are :  \t231.631449138\n",
-      "\t total surface area is :  ft**2 \t728.8512\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t199.68228374\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.439833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t23531.640773\n",
-      "\t reynolds number is :  \t52084.3641314\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,alcohol \t\n",
-      "\t flow area is :  ft**2 \t0.226041666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t508755.760369\n",
-      "\t reynolds number is :  \t21051.962498\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t269.75\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t269.75\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.421749731499\n",
-      "\t delPr is negligible \t\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t20\n",
-      "\t delPs is :  psi \t7.39957120534\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t228.633987851\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.000634152640616\n",
-      "\t This is clearly an instance in which UD was assumed too high.It is now a question of how much too high. With the aid of the summary it is apparent thatin a larger shell a clean overall coefficient of about 200 may be expected \t\n",
-      "\t Assume a 27in. ID shell with 2 tube passes,334 tubes and baffies spaced 7in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t214\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t138.5\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.002\n",
-      "\t delPs is :  psi \t0.23\n",
-      "\t delPt is :  psi \t7.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=225.; # inlet hot fluid,F\n",
-    "T2=225.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=200.; # outlet cold fluid,F\n",
-    "W=10350; # lb/hr\n",
-    "w=115000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=962; # Btu/(lb)\n",
-    "Qh=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Qh\n",
-    "print\"\\t for alcohol \\t\"\n",
-    "c=0.72; # Btu/(lb)*(F)\n",
-    "Qc=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for alcohol is :  Btu/hr \\t\",Qc\n",
-    "Q=(Qh+Qc)/(2);\n",
-    "print\"\\t Q is :  V \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1)); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2)); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "L=12;\n",
-    "UD1=200; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :f ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=232; # assuming two tube passes,23.25in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=232;\n",
-    "n=2; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.0314; # at 225F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,alcohol \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # minimum baffle spacing,from eq 11.4,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.45; # at 193.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.72/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=83; # from fig.28\n",
-    "Z=0.195; # Z=(K*(c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000175; # friction factor for reynolds number 52000, using fig.26\n",
-    "s=0.00076;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(1)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "print\"\\t delPr is negligible \\t\"\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0018; # friction factor for reynolds number 21000, using fig.29\n",
-    "s=0.78; # for reynolds number 21000,using fig.6\n",
-    "Ds=1.94; # ft\n",
-    "De=0.06;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t This is clearly an instance in which UD was assumed too high.It is now a question of how much too high. With the aid of the summary it is apparent thatin a larger shell a clean overall coefficient of about 200 may be expected \\t\"\n",
-    "print\"\\t Assume a 27in. ID shell with 2 tube passes,334 tubes and baffies spaced 7in. apart, since the pressure drop increases with the diameter of the shell for a given mass velocity. \\t\"\n",
-    "UC1=214;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=138.5;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.0025; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd2=0.002; \n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd2\n",
-    "delPs1=0.23;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPT1=7.1;\n",
-    "print\"\\t delPt is :  psi \\t\",delPT1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 11.5 pgno:246"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 11.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for gas \t\n",
-      "\t total heat required for gas is :  Btu/hr \t1290625.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t1290000.0\n",
-      "\t delt1 is :  F \t45.0\n",
-      "\t delt2 is :  F \t150.0\n",
-      "\t LMTD is : F \t87.3092936462\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.117647058824\n",
-      "\t FT is 0.935 \t\n",
-      "\t delt is :  F \t81.6341895592\n",
-      "\t caloric temperature of hot fluid is :  F \t187.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t A1 is :  ft**2 \t1067.71638982\n",
-      "\t number of tubes are :  \t339.863887771\n",
-      "\t total surface area is :  ft**2 \t1124.6928\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14.0502389358\n",
-      "\t When solved in a manner identical with the preceding examples and using the smallest integral number of bundle crosses (five) corresponding to a 28.8 in spacing \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.7\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14\n",
-      "\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \t0.027\n",
-      "\t required Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t delPs is :  psi \t5.2\n",
-      "\t delPt is :  psi \t1.0\n",
-      "\t The first trial is disqualified because of failure to meet the required dirt factor and the the pressure drop is five times greater than the allowable \t\n",
-      "\t This would be unsatisfactory, since gases require large inlet connections and the flow distribution on the first and third bundle crosses would be poor and the conditions of allowable pressure drop would still not be met \t\n",
-      "\t A1 is :  ft**2 \t1053.48017129\n",
-      "\t number of tubes are : %. \t335.332369267\n",
-      "\t total surface area is :  ft**2 \t1068.144\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t14.7940751147\n",
-      "\t hot fluid:shell side,gas \t\n",
-      "\t flow area is :  ft**2 \t1.03333333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t19983.8709677\n",
-      "\t reynolds number is :  \t32973.3870968\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t17.9454545455\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t17.9454545455\n",
-      "\t cold fluid:inner tube side,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.107430555556\n",
-      "\t mass velocity is : %lb/(hr)*(ft**2) \t600387.847447\n",
-      "\t V is :  fps \t2.6683904331\n",
-      "\t reynolds number is :  \t21289.2629579\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t667\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t553.61\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.788231357313\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.14770229996\n",
-      "\t delPr is :  psi \t2.496\n",
-      "\t delPT is :  psi \t5.64370229996\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t17.4\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0099\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 11.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=41300.; # lb/hr\n",
-    "w=64500.; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for gas \\t\"\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.935 \\t\" # from fig 18\n",
-    "delt=(0.935*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=14.8; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=358; # assuming 12 tube passes, from table 9\n",
-    "L=12;\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t When solved in a manner identical with the preceding examples and using the smallest integral number of bundle crosses (five) corresponding to a 28.8 in spacing \\t\"\n",
-    "UC1=22.7;\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UC1\n",
-    "UD2=14;\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD2\n",
-    "Rd1=0.027; \n",
-    "print\"\\t calculated Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "Rd1=0.005; \n",
-    "print\"\\t required Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd1\n",
-    "delPs1=5.2;\n",
-    "print\"\\t delPs is :  psi \\t\",delPs1\n",
-    "delPt1=1.0;\n",
-    "print\"\\t delPt is :  psi \\t\",delPt1\n",
-    "print\"\\t The first trial is disqualified because of failure to meet the required dirt factor and the the pressure drop is five times greater than the allowable \\t\"\n",
-    "print\"\\t This would be unsatisfactory, since gases require large inlet connections and the flow distribution on the first and third bundle crosses would be poor and the conditions of allowable pressure drop would still not be met \\t\"\n",
-    "UD1=15; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(delt)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.2618; # ft**2/lin ft\n",
-    "N1=(A1/(12*a1));\n",
-    "print\"\\t number of tubes are : %. \\t\",N1\n",
-    "N2=340; # assuming eight tube passes, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,gas \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.25; # clearance\n",
-    "B=24; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As)/(2); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.050; # at 187.5F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=105; # from fig.28\n",
-    "k=0.015; # Btu/(hr)(ft**2)( degree F/ft)\n",
-    "Z=0.94; # Z=((c*mu3/k)**(1/3)),Btu/(hr)(ft**2)(F/ft)\n",
-    "Ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "phys=1;\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\t\"\n",
-    "Nt=340;\n",
-    "n=12; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : %lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.96; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=667; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.83; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "phyt=1;\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 33000, using fig.29\n",
-    "s=0.0012; # for reynolds number 33000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 21300, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.052; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",delPT\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=-1*(((Uc-UD)/((UD)*(Uc)))-0.02); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Caluculations_for_Process_Heat_Conditions.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Caluculations_for_Process_Heat.ipynb
index bc4e7d41..bc4e7d41 100755
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Caluculations_for_Process_Heat_Conditions.ipynb
+++ b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_11_Caluculations_for_Process_Heat.ipynb
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours____.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours____.ipynb
deleted file mode 100755
index 41f93fc2..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours____.ipynb
+++ /dev/null
@@ -1,1348 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 12 Condensation of Single Vapours    "
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.1 pgno:274"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is : F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1199.91715754\n",
-      "\t number of tubes are :  \t764.083773266\n",
-      "\t total surface area is :  ft**2 \t1202.9264\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t100.74733825\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t flow area is :  ft**2 \t1.33543445393\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t44929.1987513\n",
-      "\t G1 is : %.1f lb/(hr)*(lin ft) \t7500\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t124.701882845\n",
-      "\t tf is :  F \t184.350941423\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t172\n",
-      "\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number is :  \t85031.2935045\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.937425488924\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.32625636683\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t148.3\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.;# inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=101; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(8*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "A2=(N2*8*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=31; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "L=8; # ft\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "G1=(W/(L*N2**(2/3)))# from eq.12.43\n",
-    "print\"\\t G1 is : %.1f lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.094; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.8; # from table 6\n",
-    "muf=0.62; # cp, from fig 14\n",
-    "ho=172; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fir 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00141; # friction factor for reynolds number 84600, using fig.29\n",
-    "s=0.00381; # for reynolds number 84600,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overalcoefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.2 pgno:277"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is f F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1731.30904159\n",
-      "\t L is :  ft \t11.5139815143\n",
-      "\t total surface area is :  ft**2 \t1804.3896\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t67.164892167\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t399.12856929\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t114.545970488\n",
-      "\t tf is :  F \t179.272985244\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t102\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area is :  ft**2 \t1.24927739239\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t48027.7641824\n",
-      "\t reynolds number is :  \t90895.5206428\n",
-      "\t number of crosses are :  \t5\n",
-      "\t delPs is :  psi \t1.7726452141\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.0\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t8.2\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t93.2\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.004\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.; # inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=(A1/(N2*a1));\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "A2=(N2*12*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "G1=(W/(3.14*N2*Do)); # from eq.12.36\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=100; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.0945; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.76; # from table 6\n",
-    "muf=0.65; # cp, from fig 14\n",
-    "ho=102; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=29; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fig 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.0014; # friction factor for reynolds number 91000, using fig.29\n",
-    "s=0.00381; # for reynolds number 91000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(5); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # eq 6.13,(hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.3 pgno:285"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for butane \t\n",
-      "\t total heat required for desuperheating of butane is :  Btu/hr \t861106.4\n",
-      "\t total heat required for condensing of butane is :  Btu/hr \t3886162\n",
-      "\t total heat required for  butane is :  Btu/hr \t4747268.4\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4742500.0\n",
-      "\t deltw is :  F \t28\n",
-      "\t t2 is :  F \t93.0\n",
-      "\t for desuperheating \t\n",
-      "\t delt1 is :  F \t37.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t63.4354185149\n",
-      "\t w1 is :  lb/hr \t13574.5364366\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t37.0\n",
-      "\t LMTD is : F \t47.6304956503\n",
-      "\t w1 is :  lb/hr \t81589.787109\n",
-      "\t delt is :  F \t49.8348522147\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t82.5\n",
-      "\t hot fluid:shell side,butane \t\n",
-      "\t flow area is :f ft**2 \t0.484375\n",
-      "\t desuperheating \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t57719.7419355\n",
-      "\t reynolds number is :  \t145094.392606\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t45.2593972603\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.184555555556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t734196.267309\n",
-      "\t V is :  fps \t3.26309452137\n",
-      "\t reynolds number is :  \t17989.5483506\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t800\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.3603962493\n",
-      "\t clean surface required for desuperheating :  ft**2 \t320.453481046\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t2912.29166667\n",
-      "\t tw is :  F \t92.9489164087\n",
-      "\t tf is :  F \t110.224458204\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t207\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t157.653742802\n",
-      "\t clean surface required for desuperheating :  ft**2 \t517.525214808\n",
-      "\t total clean surface :  ft**2 \t837.978695854\n",
-      "\t assumed condensing length percentage :  \t0.617587556066\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t113.564132378\n",
-      "\t total surface area is :  ft**2 \t1105.5616\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t86.0778119876\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t desuperheating \t\n",
-      "\t number of crosses are :  \t6.4\n",
-      "\t row is  lb/ft**3 \t1.09763894416\n",
-      "\t s is  \t0.0175622231065\n",
-      "\t delPs is :  psi \t0.964762124732\n",
-      "\t condensation \t\n",
-      "\t number of crosses are : \t9.6\n",
-      "\t delPsc is :  psi \t0.723571593549\n",
-      "\t delPS is :  psi \t1.68833371828\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t delPr is :  psi \t1.2\n",
-      "\t delPT is :  psi \t4.1\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=130.; # outlet hot fluid,F\n",
-    "T3=125.; # after condensation\n",
-    "t1=65.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=27958; # lb/hr\n",
-    "w=135500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for butane \\t\"\n",
-    "c=0.44; # Btu/(lb)(F)\n",
-    "qd=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for desuperheating of butane is :  Btu/hr \\t\",qd\n",
-    "HT2=309; # enthalpy at T2, Btu/lb\n",
-    "HT3=170; # enthalpy at T3, Btu/lb\n",
-    "qc=(W*(HT2-HT3)); # for condensation\n",
-    "print\"\\t total heat required for condensing of butane is :  Btu/hr \\t\",qc\n",
-    "Q=qd+qc;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t1+deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for desuperheating \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDd=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDd\n",
-    "w1=(qd/LMTDd);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDc=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w2=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T3)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,butane \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :f ft**2 \\t\",As\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # at 165F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.73/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=239; # from fig.28\n",
-    "k=0.012; # Btu/(hr)*(ft**2)*(F/ft), from table 5\n",
-    "Z=0.96; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=352;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=2.11; # at 82.5F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=800; # fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Ud=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ud\n",
-    "Ad=(qd/(Ud*LMTDd));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ad\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Lc=16*0.6; # condensation occurs 60 of the tube length\n",
-    "G1=(W/(Lc*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.075; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "sf=0.55; # from table 6\n",
-    "muf=0.14; # cp, from fig 14\n",
-    "ho=207; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ac\n",
-    "AC=Ad+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "lc=(Ac/(Ac+Ad));\n",
-    "print\"\\t assumed condensing length percentage :  \\t\",lc\n",
-    "UC=((Ud*Ad)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Ld=6.4; #ft\n",
-    "De=0.0608; # fig 28\n",
-    "f=0.0013; # friction factor for reynolds number 145000, using fig.29\n",
-    "Ds=1.94; # ft\n",
-    "phys=1;\n",
-    "N=(12*Ld/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "row=(58.1/((359)*(625/492)*(14.7/99.7)));\n",
-    "print\"\\t row is  lb/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPsd=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPsd\n",
-    "print\"\\t condensation \\t\"\n",
-    "N=(12*Lc/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq 12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "delPS=delPsd+delPsc;\n",
-    "print\"\\t delPS is :  psi \\t\",delPS\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.075; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.4 pgno:290"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000.0\n",
-      "\t deltw is : F \t18\n",
-      "\t t2 is : F \t82.0\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.0\n",
-      "\t delt2 is :  F \t30.0\n",
-      "\t LMTD is : F \t36.1514237668\n",
-      "\t w1 is : lb/hr \t84229.0477863\n",
-      "\t subcooling \t\n",
-      "\t delt1 is : F \t20.0\n",
-      "\t delt2 is :  F \t43.0\n",
-      "\t LMTD is f F \t30.0807554052\n",
-      "\t w1 is :  lb/hr \t9948.22091297\n",
-      "\t delt is :  F \t35.465033613\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t289.206403856\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.193993055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t860855.557544\n",
-      "\t V is :  fps \t3.8260247002\n",
-      "\t reynolds number is : %.2e \t22477.8951137\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t tw is :  F \t95.1964008573\n",
-      "\t tf is :  F \t111.348200429\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t120\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t103.947681332\n",
-      "\t clean surface required for dcondensation :  ft**2 \t803.043110735\n",
-      "\t subcooling \t\n",
-      "\t flow area is :  ft**2 \t0.520833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t40320.0\n",
-      "\t reynolds number is :  \t6939.13043478\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t68.2933263158\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t62.7761756841\n",
-      "\t clean surface required for desuperheating :  ft**2 \t158.471279981\n",
-      "\t total clean surface :  ft**2 \t961.514390716\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t97.1620302154\n",
-      "\t total surface area is :  ft**2 \t1162.096\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t81.0408681377\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00204736690467\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t reynolds number is  \t193536.0\n",
-      "\t rowvapour is  ld/ft**3 \t0.342030962803\n",
-      "\t s is  \t0.00547249540485\n",
-      "\t number of crosses are :  \t14.4\n",
-      "\t delPsc is :  psi \t1.29132938612\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.9\n",
-      "\t delPr is :  psi \t1.6\n",
-      "\t delPT is :  psi \t5.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "T3=100.; # after sucooling\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "c=0.57; # Btu/(lb)(F)\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is : F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2;\n",
-    "print\"\\t delt1 is : F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "Nt=370; # number of tubes\n",
-    "G1=(W/(3.14*Nt*Do)); # from eq.12.42\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : %.2e \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=125; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.077; # Btu/(hr)*(ft**2)*(F/ft), table 4\n",
-    "sf=0.6; # from table 6\n",
-    "muf=0.19; # cp, from fig 14\n",
-    "ho=120; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(3040000/(104*36.4));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ID=25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.46; # at 112.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46.5; # from fig.28\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Z=1.51; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "Lc=13.4; #ft\n",
-    "De=0.0792; # fig 28\n",
-    "f=0.0012; # friction factor for reynolds number 193000, using fig.29\n",
-    "mu3=0.0165; # at 127.5F\n",
-    "Ds=2.08; # ft\n",
-    "phys=1;\n",
-    "Res1=(De*Gs/mu3);\n",
-    "print\"\\t reynolds number is  \\t\",Res1\n",
-    "rowvap=(72.2/((359)*(590/492)*(14.7/25)));\n",
-    "print\"\\t rowvapour is  ld/ft**3 \\t\",rowvap\n",
-    "s=(rowvap/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "N=(12*Lc/B)+(1); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 22500, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.1; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.5 pgno:295"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000\n",
-      "\t deltw is :  F \t18.2\n",
-      "\t t2 is :  F \t81.8\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.2\n",
-      "\t delt2 is :  F \t30\n",
-      "\t LMTD is : F \t36.2404655222\n",
-      "\t w1 is :  lb/hr \t84022.0994992\n",
-      "\t subcooling \t\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t43.2\n",
-      "\t LMTD is : F \t30.1594958556\n",
-      "\t w1 is :  lb/hr \t9922.24808506\n",
-      "\t delt is : % F \t35.5529639184\n",
-      "\t caloric temperature of hot fluid is :  F \t127\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t a is :  in**2 \t123.75\n",
-      "\t number of submerged tubes are :  \t93.3248407643\n",
-      "\t number of tubes for condensation are :  \t276.675159236\n",
-      "\t flooded surface :  \t0.252229299363\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t1312.5\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.145062323071\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1151229.32312\n",
-      "\t V is :  fps \t5.11657476943\n",
-      "\t reynolds number is :  \t30059.8767704\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t251\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t189.718954672\n",
-      "\t clean surface required for dcondensation :  ft**2 \t442.876673258\n",
-      "\t subcooling \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t50\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46.9772690634\n",
-      "\t clean surface required for desuperheating :  ft**2 \t211.213812188\n",
-      "\t total clean surface :  ft**2 \t654.090485446\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t143.625919769\n",
-      "\t total surface area is :  ft**2 \t1160\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t80.9865065381\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0054\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t38391.2248629\n",
-      "\t reynolds number is :  \t184277.879342\n",
-      "\t number of crosses are :  \t10\n",
-      "\t delPsc is :  psi \t1.0\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130; # inlet hot fluid,F\n",
-    "T2=125; # outlet hot fluid,F\n",
-    "T3=100; # after subcooling\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t3=100; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "c=0.57; # Btu/(lb)(\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)-++++++++-\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=18.2;\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is : % F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "C1=0.198; # for 0.3Ds\n",
-    "Ds=25; # in\n",
-    "L=16; # ft\n",
-    "N=370\n",
-    "a=(C1*Ds**2);\n",
-    "print\"\\t a is :  in**2 \\t\",a\n",
-    "N1=((N*a*4)/(3.14*Ds**2));\n",
-    "print\"\\t number of submerged tubes are :  \\t\",N1\n",
-    "Nt=N-N1;\n",
-    "print\"\\t number of tubes for condensation are :  \\t\",Nt\n",
-    "Af=(N1/N);\n",
-    "print\"\\t flooded surface :  \\t\",Af\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "G1=(W/(L*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=251; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ho=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A=1160; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "print\"\\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\\t\"\n",
-    "As=0.547; # ft**2\n",
-    "Gs=(W/(As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "De=0.0792; # fig 28\n",
-    "Res=((De)*(Gs)/0.0165); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00121; # friction factor for reynolds number 193000, using fig.29\n",
-    "s=0.00454; # for reynolds number 193000,using fig.6\n",
-    "Ds=2.08; # ft\n",
-    "B=18\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",round(delPsc)\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#e \n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.6 pgno:299"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for carbon disulfide \t\n",
-      "\t total heat required for carbon disulfide is :  Btu/hr \t4200000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4200000.0\n",
-      "\t delt1 is :  F \t91.0\n",
-      "\t delt2 is :  F \t56.0\n",
-      "\t LMTD is : F \t72.1704928998\n",
-      "\t caloric temperature of hot fluid is :  F \t176.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t cold fluid:shell side,water \t\n",
-      "\t flow area is :  ft**2 \t0.1796875\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t667826.086957\n",
-      "\t reynolds number is :  \t31112.8388747\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t786.545454545\n",
-      "\t tw is :  F \t122.793674699\n",
-      "\t tf is :  F \t149.396837349\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t G1 is : lb/(hr)*(lin ft) \t1044.06562495\n",
-      "\t reynolds number is :  \t6141.56249973\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t0.251\n",
-      "\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t0.207493333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.207438610331\n",
-      "\t total surface area is :  ft**2 \t555.9216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t104.682978368\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-4.81115068056\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t flow area is :  ft**2 \t0.371208333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t80645.1612903\n",
-      "\t reynolds number is :  \t143770.856507\n",
-      "\t row is  ld/ft**3 \t0.572484035397\n",
-      "\t s is  \t0.00915974456635\n",
-      "\t delPt is :  psi \t0.4\n",
-      "\t allowable delPa is negligible psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t32.0\n",
-      "\t delPs is :  psi \t8.4\n",
-      "\t allowable delPT is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=176.; # inlet hot fluid,F\n",
-    "T2=176.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=120000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for carbon disulfide \\t\"\n",
-    "l=140; # Btu/(lb)\n",
-    "Q=((W)*l); # Btu/hr\n",
-    "print\"\\t total heat required for carbon disulfide is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+T1)/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "hio=300; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t cold fluid:shell side,water \\t\"\n",
-    "ID=17.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=6; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.7; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0792; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=103; # from fig.28\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Z=1.68; # Z=((c)*(mu1)/k)**(1/3); # prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "kf=0.09; # Btu/(hr)*(ft**2)*(F/ft), from fig 14\n",
-    "sf=1.26; # from table 6\n",
-    "rowf=78.8; # lb/ft**3\n",
-    "muf=0.68; # cp, from fig 24\n",
-    "Nt=177;\n",
-    "D=0.0517; # ft\n",
-    "G1=(W/(3.14*Nt*D));\n",
-    "print\"\\t G1 is : lb/(hr)*(lin ft) \\t\",G1\n",
-    "Ret=((4)*(G1)/muf); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(0.251*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(1/3)); # hi*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(-1)=0.251, from fig 12.12\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=.75; #ft\n",
-    "hio1=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "L=16;\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(30000/(0.372)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.029; # at inlet,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "row=(76.1/((359)*(636/492)*(14.7/39.7)));\n",
-    "print\"\\t row is  ld/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "f=0.000138; # friction factor for reynolds number 143000, using fig.26\n",
-    "delPt=((f*(Gt**2)*(16)*(1))/(5.22*(10**10)*(0.0517)*(s)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt+0.1,1)\n",
-    "print\"\\t allowable delPa is negligible psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 31000, using fig.29\n",
-    "s=1; # for reynolds number 31000,using fig.6\n",
-    "Ds=17.25/12.; # ft\n",
-    "B=6.;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPT is 2 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.7 pgno:308"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t223.55\n",
-      "\t area is :  ft**2 \t31250.0\n",
-      "\t t2 is :  F \t86.0\n",
-      "\t circulation rate is :  gpm \t29176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "V=7.5; # fps\n",
-    "W=250000.;\n",
-    "CCl=0.85;\n",
-    "CT=1.;\n",
-    "CL=1.;\n",
-    "Ct=263.;\n",
-    "UD=(CCl*CT*CL*Ct*(V**(1/2)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(W/8);\n",
-    "print\"\\t area is :  ft**2 \\t\",A\n",
-    "a1=0.229; # ft**2/ft, table 10\n",
-    "at=0.475; # in**2, table 10\n",
-    "t1=70;\n",
-    "Ts=91.72; #F\n",
-    "n=2;\n",
-    "L=26;\n",
-    "t2=((Ts)-((Ts-t1)/((10)**(0.000279*UD*L*n*a1/(V*at))))+8); \n",
-    "print\"\\t t2 is :  F \\t\",round(t2) # calculation mistake in book\n",
-    "Go=(W*950)/((t2-t1)*500);\n",
-    "print\"\\t circulation rate is :  gpm \\t\",round(Go)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____1.ipynb
deleted file mode 100755
index d6ed4d36..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____1.ipynb
+++ /dev/null
@@ -1,1339 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 12 Condensation of Single Vapours    "
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.1 pgno:274"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is : F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1199.91715754\n",
-      "\t number of tubes are :  \t764.083773266\n",
-      "\t total surface area is :  ft**2 \t1202.9264\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t100.74733825\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t flow area is :  ft**2 \t1.33543445393\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t44929.1987513\n",
-      "\t G1 is : %.1f lb/(hr)*(lin ft) \t7500\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t124.701882845\n",
-      "\t tf is :  F \t184.350941423\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t172\n",
-      "\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number is :  \t85031.2935045\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.937425488924\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.32625636683\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t148.3\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.;# inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=101; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(8*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "A2=(N2*8*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=31; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "L=8; # ft\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "G1=(W/(L*N2**(2/3)))# from eq.12.43\n",
-    "print\"\\t G1 is : %.1f lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.094; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.8; # from table 6\n",
-    "muf=0.62; # cp, from fig 14\n",
-    "ho=172; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fir 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00141; # friction factor for reynolds number 84600, using fig.29\n",
-    "s=0.00381; # for reynolds number 84600,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overalcoefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.2 pgno:277"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is f F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1731.30904159\n",
-      "\t L is :  ft \t11.5139815143\n",
-      "\t total surface area is :  ft**2 \t1804.3896\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t67.164892167\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t399.12856929\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t114.545970488\n",
-      "\t tf is :  F \t179.272985244\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t102\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area is :  ft**2 \t1.24927739239\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t48027.7641824\n",
-      "\t reynolds number is :  \t90895.5206428\n",
-      "\t number of crosses are :  \t5\n",
-      "\t delPs is :  psi \t1.7726452141\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.0\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t8.2\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t93.2\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.004\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.; # inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=(A1/(N2*a1));\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "A2=(N2*12*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "G1=(W/(3.14*N2*Do)); # from eq.12.36\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=100; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.0945; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.76; # from table 6\n",
-    "muf=0.65; # cp, from fig 14\n",
-    "ho=102; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=29; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fig 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.0014; # friction factor for reynolds number 91000, using fig.29\n",
-    "s=0.00381; # for reynolds number 91000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(5); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # eq 6.13,(hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.3 pgno:285"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for butane \t\n",
-      "\t total heat required for desuperheating of butane is :  Btu/hr \t861106.4\n",
-      "\t total heat required for condensing of butane is :  Btu/hr \t3886162\n",
-      "\t total heat required for  butane is :  Btu/hr \t4747268.4\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4742500.0\n",
-      "\t deltw is :  F \t28\n",
-      "\t t2 is :  F \t93.0\n",
-      "\t for desuperheating \t\n",
-      "\t delt1 is :  F \t37.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t63.4354185149\n",
-      "\t w1 is :  lb/hr \t13574.5364366\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t37.0\n",
-      "\t LMTD is : F \t47.6304956503\n",
-      "\t w1 is :  lb/hr \t81589.787109\n",
-      "\t delt is :  F \t49.8348522147\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t82.5\n",
-      "\t hot fluid:shell side,butane \t\n",
-      "\t flow area is :f ft**2 \t0.484375\n",
-      "\t desuperheating \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t57719.7419355\n",
-      "\t reynolds number is :  \t145094.392606\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t45.2593972603\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.184555555556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t734196.267309\n",
-      "\t V is :  fps \t3.26309452137\n",
-      "\t reynolds number is :  \t17989.5483506\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t800\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.3603962493\n",
-      "\t clean surface required for desuperheating :  ft**2 \t320.453481046\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t2912.29166667\n",
-      "\t tw is :  F \t92.9489164087\n",
-      "\t tf is :  F \t110.224458204\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t207\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t157.653742802\n",
-      "\t clean surface required for desuperheating :  ft**2 \t517.525214808\n",
-      "\t total clean surface :  ft**2 \t837.978695854\n",
-      "\t assumed condensing length percentage :  \t0.617587556066\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t113.564132378\n",
-      "\t total surface area is :  ft**2 \t1105.5616\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t86.0778119876\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t desuperheating \t\n",
-      "\t number of crosses are :  \t6.4\n",
-      "\t row is  lb/ft**3 \t1.09763894416\n",
-      "\t s is  \t0.0175622231065\n",
-      "\t delPs is :  psi \t0.964762124732\n",
-      "\t condensation \t\n",
-      "\t number of crosses are : \t9.6\n",
-      "\t delPsc is :  psi \t0.723571593549\n",
-      "\t delPS is :  psi \t1.68833371828\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t delPr is :  psi \t1.2\n",
-      "\t delPT is :  psi \t4.1\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=130.; # outlet hot fluid,F\n",
-    "T3=125.; # after condensation\n",
-    "t1=65.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=27958; # lb/hr\n",
-    "w=135500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for butane \\t\"\n",
-    "c=0.44; # Btu/(lb)(F)\n",
-    "qd=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for desuperheating of butane is :  Btu/hr \\t\",qd\n",
-    "HT2=309; # enthalpy at T2, Btu/lb\n",
-    "HT3=170; # enthalpy at T3, Btu/lb\n",
-    "qc=(W*(HT2-HT3)); # for condensation\n",
-    "print\"\\t total heat required for condensing of butane is :  Btu/hr \\t\",qc\n",
-    "Q=qd+qc;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t1+deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for desuperheating \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDd=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDd\n",
-    "w1=(qd/LMTDd);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDc=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w2=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T3)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,butane \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :f ft**2 \\t\",As\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # at 165F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.73/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=239; # from fig.28\n",
-    "k=0.012; # Btu/(hr)*(ft**2)*(F/ft), from table 5\n",
-    "Z=0.96; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=352;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=2.11; # at 82.5F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=800; # fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Ud=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ud\n",
-    "Ad=(qd/(Ud*LMTDd));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ad\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Lc=16*0.6; # condensation occurs 60 of the tube length\n",
-    "G1=(W/(Lc*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.075; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "sf=0.55; # from table 6\n",
-    "muf=0.14; # cp, from fig 14\n",
-    "ho=207; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ac\n",
-    "AC=Ad+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "lc=(Ac/(Ac+Ad));\n",
-    "print\"\\t assumed condensing length percentage :  \\t\",lc\n",
-    "UC=((Ud*Ad)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Ld=6.4; #ft\n",
-    "De=0.0608; # fig 28\n",
-    "f=0.0013; # friction factor for reynolds number 145000, using fig.29\n",
-    "Ds=1.94; # ft\n",
-    "phys=1;\n",
-    "N=(12*Ld/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "row=(58.1/((359)*(625/492)*(14.7/99.7)));\n",
-    "print\"\\t row is  lb/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPsd=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPsd\n",
-    "print\"\\t condensation \\t\"\n",
-    "N=(12*Lc/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq 12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "delPS=delPsd+delPsc;\n",
-    "print\"\\t delPS is :  psi \\t\",delPS\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.075; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.4 pgno:290"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000.0\n",
-      "\t deltw is : F \t18\n",
-      "\t t2 is : F \t82.0\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.0\n",
-      "\t delt2 is :  F \t30.0\n",
-      "\t LMTD is : F \t36.1514237668\n",
-      "\t w1 is : lb/hr \t84229.0477863\n",
-      "\t subcooling \t\n",
-      "\t delt1 is : F \t20.0\n",
-      "\t delt2 is :  F \t43.0\n",
-      "\t LMTD is f F \t30.0807554052\n",
-      "\t w1 is :  lb/hr \t9948.22091297\n",
-      "\t delt is :  F \t35.465033613\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t289.206403856\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.193993055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t860855.557544\n",
-      "\t V is :  fps \t3.8260247002\n",
-      "\t reynolds number is : %.2e \t22477.8951137\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t tw is :  F \t95.1964008573\n",
-      "\t tf is :  F \t111.348200429\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t120\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t103.947681332\n",
-      "\t clean surface required for dcondensation :  ft**2 \t803.043110735\n",
-      "\t subcooling \t\n",
-      "\t flow area is :  ft**2 \t0.520833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t40320.0\n",
-      "\t reynolds number is :  \t6939.13043478\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t68.2933263158\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t62.7761756841\n",
-      "\t clean surface required for desuperheating :  ft**2 \t158.471279981\n",
-      "\t total clean surface :  ft**2 \t961.514390716\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t97.1620302154\n",
-      "\t total surface area is :  ft**2 \t1162.096\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t81.0408681377\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00204736690467\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t reynolds number is  \t193536.0\n",
-      "\t rowvapour is  ld/ft**3 \t0.342030962803\n",
-      "\t s is  \t0.00547249540485\n",
-      "\t number of crosses are :  \t14.4\n",
-      "\t delPsc is :  psi \t1.29132938612\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.9\n",
-      "\t delPr is :  psi \t1.6\n",
-      "\t delPT is :  psi \t5.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "T3=100.; # after sucooling\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "c=0.57; # Btu/(lb)(F)\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is : F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2;\n",
-    "print\"\\t delt1 is : F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "Nt=370; # number of tubes\n",
-    "G1=(W/(3.14*Nt*Do)); # from eq.12.42\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : %.2e \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=125; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.077; # Btu/(hr)*(ft**2)*(F/ft), table 4\n",
-    "sf=0.6; # from table 6\n",
-    "muf=0.19; # cp, from fig 14\n",
-    "ho=120; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(3040000/(104*36.4));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ID=25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.46; # at 112.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46.5; # from fig.28\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Z=1.51; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "Lc=13.4; #ft\n",
-    "De=0.0792; # fig 28\n",
-    "f=0.0012; # friction factor for reynolds number 193000, using fig.29\n",
-    "mu3=0.0165; # at 127.5F\n",
-    "Ds=2.08; # ft\n",
-    "phys=1;\n",
-    "Res1=(De*Gs/mu3);\n",
-    "print\"\\t reynolds number is  \\t\",Res1\n",
-    "rowvap=(72.2/((359)*(590/492)*(14.7/25)));\n",
-    "print\"\\t rowvapour is  ld/ft**3 \\t\",rowvap\n",
-    "s=(rowvap/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "N=(12*Lc/B)+(1); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 22500, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.1; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.5 pgno:295"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000\n",
-      "\t deltw is :  F \t18.2\n",
-      "\t t2 is :  F \t81.8\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.2\n",
-      "\t delt2 is :  F \t30\n",
-      "\t LMTD is : F \t36.2404655222\n",
-      "\t w1 is :  lb/hr \t84022.0994992\n",
-      "\t subcooling \t\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t43.2\n",
-      "\t LMTD is : F \t30.1594958556\n",
-      "\t w1 is :  lb/hr \t9922.24808506\n",
-      "\t delt is : % F \t35.5529639184\n",
-      "\t caloric temperature of hot fluid is :  F \t127\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t a is :  in**2 \t123.75\n",
-      "\t number of submerged tubes are :  \t93.3248407643\n",
-      "\t number of tubes for condensation are :  \t276.675159236\n",
-      "\t flooded surface :  \t0.252229299363\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t1312.5\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.145062323071\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1151229.32312\n",
-      "\t V is :  fps \t5.11657476943\n",
-      "\t reynolds number is :  \t30059.8767704\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t251\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t189.718954672\n",
-      "\t clean surface required for dcondensation :  ft**2 \t442.876673258\n",
-      "\t subcooling \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t50\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46.9772690634\n",
-      "\t clean surface required for desuperheating :  ft**2 \t211.213812188\n",
-      "\t total clean surface :  ft**2 \t654.090485446\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t143.625919769\n",
-      "\t total surface area is :  ft**2 \t1160\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t80.9865065381\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0054\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t38391.2248629\n",
-      "\t reynolds number is :  \t184277.879342\n",
-      "\t number of crosses are :  \t10\n",
-      "\t delPsc is :  psi \t1.0\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130; # inlet hot fluid,F\n",
-    "T2=125; # outlet hot fluid,F\n",
-    "T3=100; # after subcooling\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t3=100; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "c=0.57; # Btu/(lb)(\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)-++++++++-\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=18.2;\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is : % F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "C1=0.198; # for 0.3Ds\n",
-    "Ds=25; # in\n",
-    "L=16; # ft\n",
-    "N=370\n",
-    "a=(C1*Ds**2);\n",
-    "print\"\\t a is :  in**2 \\t\",a\n",
-    "N1=((N*a*4)/(3.14*Ds**2));\n",
-    "print\"\\t number of submerged tubes are :  \\t\",N1\n",
-    "Nt=N-N1;\n",
-    "print\"\\t number of tubes for condensation are :  \\t\",Nt\n",
-    "Af=(N1/N);\n",
-    "print\"\\t flooded surface :  \\t\",Af\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "G1=(W/(L*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=251; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ho=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A=1160; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "print\"\\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\\t\"\n",
-    "As=0.547; # ft**2\n",
-    "Gs=(W/(As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "De=0.0792; # fig 28\n",
-    "Res=((De)*(Gs)/0.0165); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00121; # friction factor for reynolds number 193000, using fig.29\n",
-    "s=0.00454; # for reynolds number 193000,using fig.6\n",
-    "Ds=2.08; # ft\n",
-    "B=18\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",round(delPsc)\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#e \n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.6 pgno:299"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for carbon disulfide \t\n",
-      "\t total heat required for carbon disulfide is :  Btu/hr \t4200000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4200000.0\n",
-      "\t delt1 is :  F \t91.0\n",
-      "\t delt2 is :  F \t56.0\n",
-      "\t LMTD is : F \t72.1704928998\n",
-      "\t caloric temperature of hot fluid is :  F \t176.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t cold fluid:shell side,water \t\n",
-      "\t flow area is :  ft**2 \t0.1796875\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t667826.086957\n",
-      "\t reynolds number is :  \t31112.8388747\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t786.545454545\n",
-      "\t tw is :  F \t122.793674699\n",
-      "\t tf is :  F \t149.396837349\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t G1 is : lb/(hr)*(lin ft) \t1044.06562495\n",
-      "\t reynolds number is :  \t6141.56249973\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t0.251\n",
-      "\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t0.207493333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.207438610331\n",
-      "\t total surface area is :  ft**2 \t555.9216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t104.682978368\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-4.81115068056\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t flow area is :  ft**2 \t0.371208333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t80645.1612903\n",
-      "\t reynolds number is :  \t143770.856507\n",
-      "\t row is  ld/ft**3 \t0.572484035397\n",
-      "\t s is  \t0.00915974456635\n",
-      "\t delPt is :  psi \t0.4\n",
-      "\t allowable delPa is negligible psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t32.0\n",
-      "\t delPs is :  psi \t8.4\n",
-      "\t allowable delPT is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=176.; # inlet hot fluid,F\n",
-    "T2=176.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=120000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for carbon disulfide \\t\"\n",
-    "l=140; # Btu/(lb)\n",
-    "Q=((W)*l); # Btu/hr\n",
-    "print\"\\t total heat required for carbon disulfide is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+T1)/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "hio=300; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t cold fluid:shell side,water \\t\"\n",
-    "ID=17.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=6; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.7; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0792; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=103; # from fig.28\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Z=1.68; # Z=((c)*(mu1)/k)**(1/3); # prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "kf=0.09; # Btu/(hr)*(ft**2)*(F/ft), from fig 14\n",
-    "sf=1.26; # from table 6\n",
-    "rowf=78.8; # lb/ft**3\n",
-    "muf=0.68; # cp, from fig 24\n",
-    "Nt=177;\n",
-    "D=0.0517; # ft\n",
-    "G1=(W/(3.14*Nt*D));\n",
-    "print\"\\t G1 is : lb/(hr)*(lin ft) \\t\",G1\n",
-    "Ret=((4)*(G1)/muf); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(0.251*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(1/3)); # hi*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(-1)=0.251, from fig 12.12\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=.75; #ft\n",
-    "hio1=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "L=16;\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(30000/(0.372)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.029; # at inlet,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "row=(76.1/((359)*(636/492)*(14.7/39.7)));\n",
-    "print\"\\t row is  ld/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "f=0.000138; # friction factor for reynolds number 143000, using fig.26\n",
-    "delPt=((f*(Gt**2)*(16)*(1))/(5.22*(10**10)*(0.0517)*(s)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt+0.1,1)\n",
-    "print\"\\t allowable delPa is negligible psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 31000, using fig.29\n",
-    "s=1; # for reynolds number 31000,using fig.6\n",
-    "Ds=17.25/12.; # ft\n",
-    "B=6.;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPT is 2 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.7 pgno:308"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t223.55\n",
-      "\t area is :  ft**2 \t31250.0\n",
-      "\t t2 is :  F \t86.0\n",
-      "\t circulation rate is :  gpm \t29176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "V=7.5; # fps\n",
-    "W=250000.;\n",
-    "CCl=0.85;\n",
-    "CT=1.;\n",
-    "CL=1.;\n",
-    "Ct=263.;\n",
-    "UD=(CCl*CT*CL*Ct*(V**(1/2)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(W/8);\n",
-    "print\"\\t area is :  ft**2 \\t\",A\n",
-    "a1=0.229; # ft**2/ft, table 10\n",
-    "at=0.475; # in**2, table 10\n",
-    "t1=70;\n",
-    "Ts=91.72; #F\n",
-    "n=2;\n",
-    "L=26;\n",
-    "t2=((Ts)-((Ts-t1)/((10)**(0.000279*UD*L*n*a1/(V*at))))+8); \n",
-    "print\"\\t t2 is :  F \\t\",round(t2) # calculation mistake in book\n",
-    "Go=(W*950)/((t2-t1)*500);\n",
-    "print\"\\t circulation rate is :  gpm \\t\",round(Go)\n",
-    "# end\n",
-    "\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____2.ipynb
deleted file mode 100755
index d6ed4d36..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____2.ipynb
+++ /dev/null
@@ -1,1339 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 12 Condensation of Single Vapours    "
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.1 pgno:274"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is : F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1199.91715754\n",
-      "\t number of tubes are :  \t764.083773266\n",
-      "\t total surface area is :  ft**2 \t1202.9264\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t100.74733825\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t flow area is :  ft**2 \t1.33543445393\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t44929.1987513\n",
-      "\t G1 is : %.1f lb/(hr)*(lin ft) \t7500\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t124.701882845\n",
-      "\t tf is :  F \t184.350941423\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t172\n",
-      "\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number is :  \t85031.2935045\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.937425488924\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.32625636683\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t148.3\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.;# inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=101; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(8*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "A2=(N2*8*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=31; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "L=8; # ft\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "G1=(W/(L*N2**(2/3)))# from eq.12.43\n",
-    "print\"\\t G1 is : %.1f lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.094; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.8; # from table 6\n",
-    "muf=0.62; # cp, from fig 14\n",
-    "ho=172; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fir 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00141; # friction factor for reynolds number 84600, using fig.29\n",
-    "s=0.00381; # for reynolds number 84600,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overalcoefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.2 pgno:277"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is f F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1731.30904159\n",
-      "\t L is :  ft \t11.5139815143\n",
-      "\t total surface area is :  ft**2 \t1804.3896\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t67.164892167\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t399.12856929\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t114.545970488\n",
-      "\t tf is :  F \t179.272985244\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t102\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area is :  ft**2 \t1.24927739239\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t48027.7641824\n",
-      "\t reynolds number is :  \t90895.5206428\n",
-      "\t number of crosses are :  \t5\n",
-      "\t delPs is :  psi \t1.7726452141\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.0\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t8.2\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t93.2\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.004\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.; # inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=(A1/(N2*a1));\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "A2=(N2*12*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "G1=(W/(3.14*N2*Do)); # from eq.12.36\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=100; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.0945; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.76; # from table 6\n",
-    "muf=0.65; # cp, from fig 14\n",
-    "ho=102; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=29; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fig 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.0014; # friction factor for reynolds number 91000, using fig.29\n",
-    "s=0.00381; # for reynolds number 91000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(5); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # eq 6.13,(hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.3 pgno:285"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for butane \t\n",
-      "\t total heat required for desuperheating of butane is :  Btu/hr \t861106.4\n",
-      "\t total heat required for condensing of butane is :  Btu/hr \t3886162\n",
-      "\t total heat required for  butane is :  Btu/hr \t4747268.4\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4742500.0\n",
-      "\t deltw is :  F \t28\n",
-      "\t t2 is :  F \t93.0\n",
-      "\t for desuperheating \t\n",
-      "\t delt1 is :  F \t37.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t63.4354185149\n",
-      "\t w1 is :  lb/hr \t13574.5364366\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t37.0\n",
-      "\t LMTD is : F \t47.6304956503\n",
-      "\t w1 is :  lb/hr \t81589.787109\n",
-      "\t delt is :  F \t49.8348522147\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t82.5\n",
-      "\t hot fluid:shell side,butane \t\n",
-      "\t flow area is :f ft**2 \t0.484375\n",
-      "\t desuperheating \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t57719.7419355\n",
-      "\t reynolds number is :  \t145094.392606\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t45.2593972603\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.184555555556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t734196.267309\n",
-      "\t V is :  fps \t3.26309452137\n",
-      "\t reynolds number is :  \t17989.5483506\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t800\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.3603962493\n",
-      "\t clean surface required for desuperheating :  ft**2 \t320.453481046\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t2912.29166667\n",
-      "\t tw is :  F \t92.9489164087\n",
-      "\t tf is :  F \t110.224458204\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t207\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t157.653742802\n",
-      "\t clean surface required for desuperheating :  ft**2 \t517.525214808\n",
-      "\t total clean surface :  ft**2 \t837.978695854\n",
-      "\t assumed condensing length percentage :  \t0.617587556066\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t113.564132378\n",
-      "\t total surface area is :  ft**2 \t1105.5616\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t86.0778119876\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t desuperheating \t\n",
-      "\t number of crosses are :  \t6.4\n",
-      "\t row is  lb/ft**3 \t1.09763894416\n",
-      "\t s is  \t0.0175622231065\n",
-      "\t delPs is :  psi \t0.964762124732\n",
-      "\t condensation \t\n",
-      "\t number of crosses are : \t9.6\n",
-      "\t delPsc is :  psi \t0.723571593549\n",
-      "\t delPS is :  psi \t1.68833371828\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t delPr is :  psi \t1.2\n",
-      "\t delPT is :  psi \t4.1\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=130.; # outlet hot fluid,F\n",
-    "T3=125.; # after condensation\n",
-    "t1=65.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=27958; # lb/hr\n",
-    "w=135500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for butane \\t\"\n",
-    "c=0.44; # Btu/(lb)(F)\n",
-    "qd=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for desuperheating of butane is :  Btu/hr \\t\",qd\n",
-    "HT2=309; # enthalpy at T2, Btu/lb\n",
-    "HT3=170; # enthalpy at T3, Btu/lb\n",
-    "qc=(W*(HT2-HT3)); # for condensation\n",
-    "print\"\\t total heat required for condensing of butane is :  Btu/hr \\t\",qc\n",
-    "Q=qd+qc;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t1+deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for desuperheating \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDd=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDd\n",
-    "w1=(qd/LMTDd);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDc=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w2=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T3)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,butane \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :f ft**2 \\t\",As\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # at 165F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.73/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=239; # from fig.28\n",
-    "k=0.012; # Btu/(hr)*(ft**2)*(F/ft), from table 5\n",
-    "Z=0.96; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=352;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=2.11; # at 82.5F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=800; # fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Ud=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ud\n",
-    "Ad=(qd/(Ud*LMTDd));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ad\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Lc=16*0.6; # condensation occurs 60 of the tube length\n",
-    "G1=(W/(Lc*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.075; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "sf=0.55; # from table 6\n",
-    "muf=0.14; # cp, from fig 14\n",
-    "ho=207; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ac\n",
-    "AC=Ad+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "lc=(Ac/(Ac+Ad));\n",
-    "print\"\\t assumed condensing length percentage :  \\t\",lc\n",
-    "UC=((Ud*Ad)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Ld=6.4; #ft\n",
-    "De=0.0608; # fig 28\n",
-    "f=0.0013; # friction factor for reynolds number 145000, using fig.29\n",
-    "Ds=1.94; # ft\n",
-    "phys=1;\n",
-    "N=(12*Ld/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "row=(58.1/((359)*(625/492)*(14.7/99.7)));\n",
-    "print\"\\t row is  lb/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPsd=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPsd\n",
-    "print\"\\t condensation \\t\"\n",
-    "N=(12*Lc/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq 12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "delPS=delPsd+delPsc;\n",
-    "print\"\\t delPS is :  psi \\t\",delPS\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.075; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.4 pgno:290"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000.0\n",
-      "\t deltw is : F \t18\n",
-      "\t t2 is : F \t82.0\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.0\n",
-      "\t delt2 is :  F \t30.0\n",
-      "\t LMTD is : F \t36.1514237668\n",
-      "\t w1 is : lb/hr \t84229.0477863\n",
-      "\t subcooling \t\n",
-      "\t delt1 is : F \t20.0\n",
-      "\t delt2 is :  F \t43.0\n",
-      "\t LMTD is f F \t30.0807554052\n",
-      "\t w1 is :  lb/hr \t9948.22091297\n",
-      "\t delt is :  F \t35.465033613\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t289.206403856\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.193993055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t860855.557544\n",
-      "\t V is :  fps \t3.8260247002\n",
-      "\t reynolds number is : %.2e \t22477.8951137\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t tw is :  F \t95.1964008573\n",
-      "\t tf is :  F \t111.348200429\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t120\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t103.947681332\n",
-      "\t clean surface required for dcondensation :  ft**2 \t803.043110735\n",
-      "\t subcooling \t\n",
-      "\t flow area is :  ft**2 \t0.520833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t40320.0\n",
-      "\t reynolds number is :  \t6939.13043478\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t68.2933263158\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t62.7761756841\n",
-      "\t clean surface required for desuperheating :  ft**2 \t158.471279981\n",
-      "\t total clean surface :  ft**2 \t961.514390716\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t97.1620302154\n",
-      "\t total surface area is :  ft**2 \t1162.096\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t81.0408681377\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00204736690467\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t reynolds number is  \t193536.0\n",
-      "\t rowvapour is  ld/ft**3 \t0.342030962803\n",
-      "\t s is  \t0.00547249540485\n",
-      "\t number of crosses are :  \t14.4\n",
-      "\t delPsc is :  psi \t1.29132938612\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.9\n",
-      "\t delPr is :  psi \t1.6\n",
-      "\t delPT is :  psi \t5.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "T3=100.; # after sucooling\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "c=0.57; # Btu/(lb)(F)\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is : F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2;\n",
-    "print\"\\t delt1 is : F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "Nt=370; # number of tubes\n",
-    "G1=(W/(3.14*Nt*Do)); # from eq.12.42\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : %.2e \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=125; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.077; # Btu/(hr)*(ft**2)*(F/ft), table 4\n",
-    "sf=0.6; # from table 6\n",
-    "muf=0.19; # cp, from fig 14\n",
-    "ho=120; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(3040000/(104*36.4));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ID=25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.46; # at 112.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46.5; # from fig.28\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Z=1.51; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "Lc=13.4; #ft\n",
-    "De=0.0792; # fig 28\n",
-    "f=0.0012; # friction factor for reynolds number 193000, using fig.29\n",
-    "mu3=0.0165; # at 127.5F\n",
-    "Ds=2.08; # ft\n",
-    "phys=1;\n",
-    "Res1=(De*Gs/mu3);\n",
-    "print\"\\t reynolds number is  \\t\",Res1\n",
-    "rowvap=(72.2/((359)*(590/492)*(14.7/25)));\n",
-    "print\"\\t rowvapour is  ld/ft**3 \\t\",rowvap\n",
-    "s=(rowvap/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "N=(12*Lc/B)+(1); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 22500, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.1; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.5 pgno:295"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000\n",
-      "\t deltw is :  F \t18.2\n",
-      "\t t2 is :  F \t81.8\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.2\n",
-      "\t delt2 is :  F \t30\n",
-      "\t LMTD is : F \t36.2404655222\n",
-      "\t w1 is :  lb/hr \t84022.0994992\n",
-      "\t subcooling \t\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t43.2\n",
-      "\t LMTD is : F \t30.1594958556\n",
-      "\t w1 is :  lb/hr \t9922.24808506\n",
-      "\t delt is : % F \t35.5529639184\n",
-      "\t caloric temperature of hot fluid is :  F \t127\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t a is :  in**2 \t123.75\n",
-      "\t number of submerged tubes are :  \t93.3248407643\n",
-      "\t number of tubes for condensation are :  \t276.675159236\n",
-      "\t flooded surface :  \t0.252229299363\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t1312.5\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.145062323071\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1151229.32312\n",
-      "\t V is :  fps \t5.11657476943\n",
-      "\t reynolds number is :  \t30059.8767704\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t251\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t189.718954672\n",
-      "\t clean surface required for dcondensation :  ft**2 \t442.876673258\n",
-      "\t subcooling \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t50\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46.9772690634\n",
-      "\t clean surface required for desuperheating :  ft**2 \t211.213812188\n",
-      "\t total clean surface :  ft**2 \t654.090485446\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t143.625919769\n",
-      "\t total surface area is :  ft**2 \t1160\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t80.9865065381\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0054\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t38391.2248629\n",
-      "\t reynolds number is :  \t184277.879342\n",
-      "\t number of crosses are :  \t10\n",
-      "\t delPsc is :  psi \t1.0\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130; # inlet hot fluid,F\n",
-    "T2=125; # outlet hot fluid,F\n",
-    "T3=100; # after subcooling\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t3=100; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "c=0.57; # Btu/(lb)(\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)-++++++++-\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=18.2;\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is : % F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "C1=0.198; # for 0.3Ds\n",
-    "Ds=25; # in\n",
-    "L=16; # ft\n",
-    "N=370\n",
-    "a=(C1*Ds**2);\n",
-    "print\"\\t a is :  in**2 \\t\",a\n",
-    "N1=((N*a*4)/(3.14*Ds**2));\n",
-    "print\"\\t number of submerged tubes are :  \\t\",N1\n",
-    "Nt=N-N1;\n",
-    "print\"\\t number of tubes for condensation are :  \\t\",Nt\n",
-    "Af=(N1/N);\n",
-    "print\"\\t flooded surface :  \\t\",Af\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "G1=(W/(L*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=251; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ho=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A=1160; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "print\"\\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\\t\"\n",
-    "As=0.547; # ft**2\n",
-    "Gs=(W/(As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "De=0.0792; # fig 28\n",
-    "Res=((De)*(Gs)/0.0165); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00121; # friction factor for reynolds number 193000, using fig.29\n",
-    "s=0.00454; # for reynolds number 193000,using fig.6\n",
-    "Ds=2.08; # ft\n",
-    "B=18\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",round(delPsc)\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#e \n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.6 pgno:299"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for carbon disulfide \t\n",
-      "\t total heat required for carbon disulfide is :  Btu/hr \t4200000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4200000.0\n",
-      "\t delt1 is :  F \t91.0\n",
-      "\t delt2 is :  F \t56.0\n",
-      "\t LMTD is : F \t72.1704928998\n",
-      "\t caloric temperature of hot fluid is :  F \t176.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t cold fluid:shell side,water \t\n",
-      "\t flow area is :  ft**2 \t0.1796875\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t667826.086957\n",
-      "\t reynolds number is :  \t31112.8388747\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t786.545454545\n",
-      "\t tw is :  F \t122.793674699\n",
-      "\t tf is :  F \t149.396837349\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t G1 is : lb/(hr)*(lin ft) \t1044.06562495\n",
-      "\t reynolds number is :  \t6141.56249973\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t0.251\n",
-      "\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t0.207493333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.207438610331\n",
-      "\t total surface area is :  ft**2 \t555.9216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t104.682978368\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-4.81115068056\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t flow area is :  ft**2 \t0.371208333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t80645.1612903\n",
-      "\t reynolds number is :  \t143770.856507\n",
-      "\t row is  ld/ft**3 \t0.572484035397\n",
-      "\t s is  \t0.00915974456635\n",
-      "\t delPt is :  psi \t0.4\n",
-      "\t allowable delPa is negligible psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t32.0\n",
-      "\t delPs is :  psi \t8.4\n",
-      "\t allowable delPT is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=176.; # inlet hot fluid,F\n",
-    "T2=176.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=120000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for carbon disulfide \\t\"\n",
-    "l=140; # Btu/(lb)\n",
-    "Q=((W)*l); # Btu/hr\n",
-    "print\"\\t total heat required for carbon disulfide is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+T1)/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "hio=300; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t cold fluid:shell side,water \\t\"\n",
-    "ID=17.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=6; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.7; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0792; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=103; # from fig.28\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Z=1.68; # Z=((c)*(mu1)/k)**(1/3); # prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "kf=0.09; # Btu/(hr)*(ft**2)*(F/ft), from fig 14\n",
-    "sf=1.26; # from table 6\n",
-    "rowf=78.8; # lb/ft**3\n",
-    "muf=0.68; # cp, from fig 24\n",
-    "Nt=177;\n",
-    "D=0.0517; # ft\n",
-    "G1=(W/(3.14*Nt*D));\n",
-    "print\"\\t G1 is : lb/(hr)*(lin ft) \\t\",G1\n",
-    "Ret=((4)*(G1)/muf); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(0.251*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(1/3)); # hi*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(-1)=0.251, from fig 12.12\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=.75; #ft\n",
-    "hio1=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "L=16;\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(30000/(0.372)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.029; # at inlet,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "row=(76.1/((359)*(636/492)*(14.7/39.7)));\n",
-    "print\"\\t row is  ld/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "f=0.000138; # friction factor for reynolds number 143000, using fig.26\n",
-    "delPt=((f*(Gt**2)*(16)*(1))/(5.22*(10**10)*(0.0517)*(s)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt+0.1,1)\n",
-    "print\"\\t allowable delPa is negligible psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 31000, using fig.29\n",
-    "s=1; # for reynolds number 31000,using fig.6\n",
-    "Ds=17.25/12.; # ft\n",
-    "B=6.;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPT is 2 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.7 pgno:308"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t223.55\n",
-      "\t area is :  ft**2 \t31250.0\n",
-      "\t t2 is :  F \t86.0\n",
-      "\t circulation rate is :  gpm \t29176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "V=7.5; # fps\n",
-    "W=250000.;\n",
-    "CCl=0.85;\n",
-    "CT=1.;\n",
-    "CL=1.;\n",
-    "Ct=263.;\n",
-    "UD=(CCl*CT*CL*Ct*(V**(1/2)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(W/8);\n",
-    "print\"\\t area is :  ft**2 \\t\",A\n",
-    "a1=0.229; # ft**2/ft, table 10\n",
-    "at=0.475; # in**2, table 10\n",
-    "t1=70;\n",
-    "Ts=91.72; #F\n",
-    "n=2;\n",
-    "L=26;\n",
-    "t2=((Ts)-((Ts-t1)/((10)**(0.000279*UD*L*n*a1/(V*at))))+8); \n",
-    "print\"\\t t2 is :  F \\t\",round(t2) # calculation mistake in book\n",
-    "Go=(W*950)/((t2-t1)*500);\n",
-    "print\"\\t circulation rate is :  gpm \\t\",round(Go)\n",
-    "# end\n",
-    "\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____3.ipynb
deleted file mode 100755
index d6ed4d36..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_12_Condensation_of_Single_Vapours_____3.ipynb
+++ /dev/null
@@ -1,1339 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 12 Condensation of Single Vapours    "
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.1 pgno:274"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is : F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1199.91715754\n",
-      "\t number of tubes are :  \t764.083773266\n",
-      "\t total surface area is :  ft**2 \t1202.9264\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t100.74733825\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t flow area is :  ft**2 \t1.33543445393\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t44929.1987513\n",
-      "\t G1 is : %.1f lb/(hr)*(lin ft) \t7500\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t124.701882845\n",
-      "\t tf is :  F \t184.350941423\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t172\n",
-      "\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number is :  \t85031.2935045\n",
-      "\t number of crosses are :  \t3\n",
-      "\t delPs is :  psi \t0.937425488924\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.32625636683\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t148.3\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.;# inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=101; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "N1=(A1/(8*a1));\n",
-    "print\"\\t number of tubes are :  \\t\",N1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "A2=(N2*8*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=31; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "L=8; # ft\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "G1=(W/(L*N2**(2/3)))# from eq.12.43\n",
-    "print\"\\t G1 is : %.1f lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio # calculation mistake\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.094; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.8; # from table 6\n",
-    "muf=0.62; # cp, from fig 14\n",
-    "ho=172; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t Based on h=172 instead of the assumed 200 a new value of tw,and tf could be obtained to give a more exact value of h based on fluid properties at a value of tf more nearly correct \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fir 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00141; # friction factor for reynolds number 84600, using fig.29\n",
-    "s=0.00381; # for reynolds number 84600,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(3); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overalcoefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.2 pgno:277"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for propanol \t\n",
-      "\t total heat required for propanol is :  Btu/hr \t17100000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t17080000.0\n",
-      "\t delt1 is :  F \t159.0\n",
-      "\t delt2 is :  F \t124.0\n",
-      "\t LMTD is f F \t140.93382183\n",
-      "\t caloric temperature of hot fluid is :  F \t244.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t A1 is :  ft**2 \t1731.30904159\n",
-      "\t L is :  ft \t11.5139815143\n",
-      "\t total surface area is :  ft**2 \t1804.3896\n",
-      "\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t67.164892167\n",
-      "\t hot fluid:shell side,propanol \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t399.12856929\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.401618055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1215084.81317\n",
-      "\t V is :  fps \t5.40037694742\n",
-      "\t reynolds number is :  \t36103.3820924\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t1300\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1074.66666667\n",
-      "\t tw is :  F \t114.545970488\n",
-      "\t tf is :  F \t179.272985244\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t102\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area is :  ft**2 \t1.24927739239\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t48027.7641824\n",
-      "\t reynolds number is :  \t90895.5206428\n",
-      "\t number of crosses are :  \t5\n",
-      "\t delPs is :  psi \t1.7726452141\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.0\n",
-      "\t delPr is :  psi \t3.2\n",
-      "\t delPT is :  psi \t8.2\n",
-      "\t allowable delPT is 10 psi \t\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t93.2\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.004\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=244.; # inlet hot fluid,F\n",
-    "T2=244.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=488000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for propanol \\t\"\n",
-    "l=285; # Btu/(lb)\n",
-    "Q=((W)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for propanol is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "UD1=70; # assume, from table 8\n",
-    "A1=((Q)/((UD1)*(LMTD)));\n",
-    "print\"\\t A1 is :  ft**2 \\t\",A1\n",
-    "N2=766; # assuming 4 tube passes, from table 9\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=(A1/(N2*a1));\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "A2=(N2*12*a1); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t correct design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "print\"\\t hot fluid:shell side,propanol \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "G1=(W/(3.14*N2*Do)); # from eq.12.36\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=766;\n",
-    "n=4; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.74; # at 102.5F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=1300; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=100; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.0945; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "sf=0.76; # from table 6\n",
-    "muf=0.65; # cp, from fig 14\n",
-    "ho=102; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "ID=31; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=29; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,from eq 7.1,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,from eq 7.2,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # lb/(ft)*(hr), fig 15\n",
-    "De=0.0458; # fig 28\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.0014; # friction factor for reynolds number 91000, using fig.29\n",
-    "s=0.00381; # for reynolds number 91000,using fig.6\n",
-    "Ds=31/12; # ft\n",
-    "phys=1;\n",
-    "N=(5); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00019; # friction factor for reynolds number 36200, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.2; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",round(Uc,1)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # eq 6.13,(hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.3 pgno:285"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for butane \t\n",
-      "\t total heat required for desuperheating of butane is :  Btu/hr \t861106.4\n",
-      "\t total heat required for condensing of butane is :  Btu/hr \t3886162\n",
-      "\t total heat required for  butane is :  Btu/hr \t4747268.4\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4742500.0\n",
-      "\t deltw is :  F \t28\n",
-      "\t t2 is :  F \t93.0\n",
-      "\t for desuperheating \t\n",
-      "\t delt1 is :  F \t37.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t63.4354185149\n",
-      "\t w1 is :  lb/hr \t13574.5364366\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t60.0\n",
-      "\t delt2 is :  F \t37.0\n",
-      "\t LMTD is : F \t47.6304956503\n",
-      "\t w1 is :  lb/hr \t81589.787109\n",
-      "\t delt is :  F \t49.8348522147\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t82.5\n",
-      "\t hot fluid:shell side,butane \t\n",
-      "\t flow area is :f ft**2 \t0.484375\n",
-      "\t desuperheating \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t57719.7419355\n",
-      "\t reynolds number is :  \t145094.392606\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t45.2593972603\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.184555555556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t734196.267309\n",
-      "\t V is :  fps \t3.26309452137\n",
-      "\t reynolds number is :  \t17989.5483506\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t800\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.3603962493\n",
-      "\t clean surface required for desuperheating :  ft**2 \t320.453481046\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t2912.29166667\n",
-      "\t tw is :  F \t92.9489164087\n",
-      "\t tf is :  F \t110.224458204\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t207\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t157.653742802\n",
-      "\t clean surface required for desuperheating :  ft**2 \t517.525214808\n",
-      "\t total clean surface :  ft**2 \t837.978695854\n",
-      "\t assumed condensing length percentage :  \t0.617587556066\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t113.564132378\n",
-      "\t total surface area is :  ft**2 \t1105.5616\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t86.0778119876\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.003\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t desuperheating \t\n",
-      "\t number of crosses are :  \t6.4\n",
-      "\t row is  lb/ft**3 \t1.09763894416\n",
-      "\t s is  \t0.0175622231065\n",
-      "\t delPs is :  psi \t0.964762124732\n",
-      "\t condensation \t\n",
-      "\t number of crosses are : \t9.6\n",
-      "\t delPsc is :  psi \t0.723571593549\n",
-      "\t delPS is :  psi \t1.68833371828\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t delPr is :  psi \t1.2\n",
-      "\t delPT is :  psi \t4.1\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=130.; # outlet hot fluid,F\n",
-    "T3=125.; # after condensation\n",
-    "t1=65.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=27958; # lb/hr\n",
-    "w=135500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for butane \\t\"\n",
-    "c=0.44; # Btu/(lb)(F)\n",
-    "qd=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for desuperheating of butane is :  Btu/hr \\t\",qd\n",
-    "HT2=309; # enthalpy at T2, Btu/lb\n",
-    "HT3=170; # enthalpy at T3, Btu/lb\n",
-    "qc=(W*(HT2-HT3)); # for condensation\n",
-    "print\"\\t total heat required for condensing of butane is :  Btu/hr \\t\",qc\n",
-    "Q=qd+qc;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t1+deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for desuperheating \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDd=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDd\n",
-    "w1=(qd/LMTDd);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDc=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w2=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T3)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,butane \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :f ft**2 \\t\",As\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0242; # at 165F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.73/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=239; # from fig.28\n",
-    "k=0.012; # Btu/(hr)*(ft**2)*(F/ft), from table 5\n",
-    "Z=0.96; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # H0=(h0/phya),using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=352;\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=2.11; # at 82.5F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=800; # fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Ud=((hio)*(ho)/(hio+ho)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ud\n",
-    "Ad=(qd/(Ud*LMTDd));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ad\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Lc=16*0.6; # condensation occurs 60 of the tube length\n",
-    "G1=(W/(Lc*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "ho=200; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.075; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "sf=0.55; # from table 6\n",
-    "muf=0.14; # cp, from fig 14\n",
-    "ho=207; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",Ac\n",
-    "AC=Ad+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "lc=(Ac/(Ac+Ad));\n",
-    "print\"\\t assumed condensing length percentage :  \\t\",lc\n",
-    "UC=((Ud*Ad)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,3)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t desuperheating \\t\"\n",
-    "Ld=6.4; #ft\n",
-    "De=0.0608; # fig 28\n",
-    "f=0.0013; # friction factor for reynolds number 145000, using fig.29\n",
-    "Ds=1.94; # ft\n",
-    "phys=1;\n",
-    "N=(12*Ld/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "row=(58.1/((359)*(625/492)*(14.7/99.7)));\n",
-    "print\"\\t row is  lb/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPsd=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPsd\n",
-    "print\"\\t condensation \\t\"\n",
-    "N=(12*Lc/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq 12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "delPS=delPsd+delPsc;\n",
-    "print\"\\t delPS is :  psi \\t\",delPS\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.075; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.4 pgno:290"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000.0\n",
-      "\t deltw is : F \t18\n",
-      "\t t2 is : F \t82.0\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.0\n",
-      "\t delt2 is :  F \t30.0\n",
-      "\t LMTD is : F \t36.1514237668\n",
-      "\t w1 is : lb/hr \t84229.0477863\n",
-      "\t subcooling \t\n",
-      "\t delt1 is : F \t20.0\n",
-      "\t delt2 is :  F \t43.0\n",
-      "\t LMTD is f F \t30.0807554052\n",
-      "\t w1 is :  lb/hr \t9948.22091297\n",
-      "\t delt is :  F \t35.465033613\n",
-      "\t caloric temperature of hot fluid is :  F \t127.5\n",
-      "\t caloric temperature of cold fluid is :  F \t90.0\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t289.206403856\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.193993055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t860855.557544\n",
-      "\t V is :  fps \t3.8260247002\n",
-      "\t reynolds number is : %.2e \t22477.8951137\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t tw is :  F \t95.1964008573\n",
-      "\t tf is :  F \t111.348200429\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t120\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t103.947681332\n",
-      "\t clean surface required for dcondensation :  ft**2 \t803.043110735\n",
-      "\t subcooling \t\n",
-      "\t flow area is :  ft**2 \t0.520833333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t40320.0\n",
-      "\t reynolds number is :  \t6939.13043478\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t68.2933263158\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t62.7761756841\n",
-      "\t clean surface required for desuperheating :  ft**2 \t158.471279981\n",
-      "\t total clean surface :  ft**2 \t961.514390716\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t97.1620302154\n",
-      "\t total surface area is :  ft**2 \t1162.096\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t81.0408681377\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00204736690467\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t reynolds number is  \t193536.0\n",
-      "\t rowvapour is  ld/ft**3 \t0.342030962803\n",
-      "\t s is  \t0.00547249540485\n",
-      "\t number of crosses are :  \t14.4\n",
-      "\t delPsc is :  psi \t1.29132938612\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.9\n",
-      "\t delPr is :  psi \t1.6\n",
-      "\t delPT is :  psi \t5.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130.; # inlet hot fluid,F\n",
-    "T2=125.; # outlet hot fluid,F\n",
-    "T3=100.; # after sucooling\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t3=100.; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "c=0.57; # Btu/(lb)(F)\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=(qc/w);\n",
-    "print\"\\t deltw is : F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2;\n",
-    "print\"\\t delt1 is : F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is f F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "Do=0.0625; # ft\n",
-    "Nt=370; # number of tubes\n",
-    "G1=(W/(3.14*Nt*Do)); # from eq.12.42\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # at 90F,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : %.2e \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=125; # assumption\n",
-    "tw=(tc)+(((ho)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "kf=0.077; # Btu/(hr)*(ft**2)*(F/ft), table 4\n",
-    "sf=0.6; # from table 6\n",
-    "muf=0.19; # cp, from fig 14\n",
-    "ho=120; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(3040000/(104*36.4));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ID=25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.46; # at 112.5F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=46.5; # from fig.28\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Z=1.51; # Z=((c)*(mu1)/k)**(1/3)\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "Lc=13.4; #ft\n",
-    "De=0.0792; # fig 28\n",
-    "f=0.0012; # friction factor for reynolds number 193000, using fig.29\n",
-    "mu3=0.0165; # at 127.5F\n",
-    "Ds=2.08; # ft\n",
-    "phys=1;\n",
-    "Res1=(De*Gs/mu3);\n",
-    "print\"\\t reynolds number is  \\t\",Res1\n",
-    "rowvap=(72.2/((359)*(590/492)*(14.7/25)));\n",
-    "print\"\\t rowvapour is  ld/ft**3 \\t\",rowvap\n",
-    "s=(rowvap/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "N=(12*Lc/B)+(1); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",delPsc\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00022; # friction factor for reynolds number 22500, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.1; # X1=((V**2)/(2*g)),using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.5 pgno:295"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for pentane \t\n",
-      "\t total heat required for subcooling of pentane is :  Btu/hr \t299250.0\n",
-      "\t total heat required for condensing of pentane is :  Btu/hr \t3045000\n",
-      "\t total heat required for  pentane is :  Btu/hr \t3344250.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t3340000\n",
-      "\t deltw is :  F \t18.2\n",
-      "\t t2 is :  F \t81.8\n",
-      "\t for condensing \t\n",
-      "\t delt1 is :  F \t43.2\n",
-      "\t delt2 is :  F \t30\n",
-      "\t LMTD is : F \t36.2404655222\n",
-      "\t w1 is :  lb/hr \t84022.0994992\n",
-      "\t subcooling \t\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t43.2\n",
-      "\t LMTD is : F \t30.1594958556\n",
-      "\t w1 is :  lb/hr \t9922.24808506\n",
-      "\t delt is : % F \t35.5529639184\n",
-      "\t caloric temperature of hot fluid is :  F \t127\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,pentane \t\n",
-      "\t a is :  in**2 \t123.75\n",
-      "\t number of submerged tubes are :  \t93.3248407643\n",
-      "\t number of tubes for condensation are :  \t276.675159236\n",
-      "\t flooded surface :  \t0.252229299363\n",
-      "\t for condensaton \t\n",
-      "\t G1 is :  lb/(hr)*(lin ft) \t1312.5\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.145062323071\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1151229.32312\n",
-      "\t V is :  fps \t5.11657476943\n",
-      "\t reynolds number is :  \t30059.8767704\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t940\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t777.066666667\n",
-      "\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t251\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t189.718954672\n",
-      "\t clean surface required for dcondensation :  ft**2 \t442.876673258\n",
-      "\t subcooling \t\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t50\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t46.9772690634\n",
-      "\t clean surface required for desuperheating :  ft**2 \t211.213812188\n",
-      "\t total clean surface :  ft**2 \t654.090485446\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t143.625919769\n",
-      "\t total surface area is :  ft**2 \t1160\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t80.9865065381\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.0054\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t condensation \t\n",
-      "\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t38391.2248629\n",
-      "\t reynolds number is :  \t184277.879342\n",
-      "\t number of crosses are :  \t10\n",
-      "\t delPsc is :  psi \t1.0\n",
-      "\t delPss is negligible \t\n",
-      "\t allowable delPa is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=130; # inlet hot fluid,F\n",
-    "T2=125; # outlet hot fluid,F\n",
-    "T3=100; # after subcooling\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t3=100; # outlet cold fluid,F\n",
-    "W=21000; # lb/hr\n",
-    "w=167000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for pentane \\t\"\n",
-    "c=0.57; # Btu/(lb)(\n",
-    "qs=((W)*(c)*(T2-T3)); # Btu/hr\n",
-    "print\"\\t total heat required for subcooling of pentane is :  Btu/hr \\t\",qs\n",
-    "HT1=315; # enthalpy at T1, Btu/lb\n",
-    "HT2=170; # enthalpy at T2, Btu/lb\n",
-    "qc=(W*(HT1-HT2)); # for condensation\n",
-    "print\"\\t total heat required for condensing of pentane is :  Btu/hr \\t\",qc\n",
-    "Q=qs+qc;\n",
-    "print\"\\t total heat required for  pentane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)-++++++++-\n",
-    "Q=((w)*(c)*(t3-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "deltw=18.2;\n",
-    "print\"\\t deltw is :  F \\t\",deltw\n",
-    "t2=t3-deltw;\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t for condensing \\t\"\n",
-    "delt1=T2-t2; #F\n",
-    "delt2=T1-t3; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTDc=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDc\n",
-    "w1=(qc/LMTDc);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w1\n",
-    "print\"\\t subcooling \\t\"\n",
-    "delt3=T3-t1; #F\n",
-    "delt4=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt3\n",
-    "print\"\\t delt2 is :  F \\t\",delt4\n",
-    "LMTDs=((delt4-delt3)/((2.3)*(log10(delt4/delt3))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTDs\n",
-    "w2=(qs/LMTDs);\n",
-    "print\"\\t w1 is :  lb/hr \\t\",w2\n",
-    "delt=(Q/(w1+w2));\n",
-    "print\"\\t delt is : % F \\t\",delt\n",
-    "Tc=((T1)+(T2))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t3))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,pentane \\t\"\n",
-    "C1=0.198; # for 0.3Ds\n",
-    "Ds=25; # in\n",
-    "L=16; # ft\n",
-    "N=370\n",
-    "a=(C1*Ds**2);\n",
-    "print\"\\t a is :  in**2 \\t\",a\n",
-    "N1=((N*a*4)/(3.14*Ds**2));\n",
-    "print\"\\t number of submerged tubes are :  \\t\",N1\n",
-    "Nt=N-N1;\n",
-    "print\"\\t number of tubes for condensation are :  \\t\",Nt\n",
-    "Af=(N1/N);\n",
-    "print\"\\t flooded surface :  \\t\",Af\n",
-    "print\"\\t for condensaton \\t\"\n",
-    "G1=(W/(L*Nt**(2/3))); # from eq.12.43\n",
-    "print\"\\t G1 is :  lb/(hr)*(lin ft) \\t\",G1\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "n=4; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.98; # lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=940; #Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=251; # Btu/(hr)*(ft**2)*(F), from fig 12.9\n",
-    "print\"\\t Correct ho to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Ac=(qc/(Uc*LMTDc));\n",
-    "print\"\\t clean surface required for dcondensation :  ft**2 \\t\",Ac\n",
-    "print\"\\t subcooling \\t\"\n",
-    "ho=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Us=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Us\n",
-    "As=(qs/(Us*LMTDs));\n",
-    "print\"\\t clean surface required for desuperheating :  ft**2 \\t\",As\n",
-    "AC=As+Ac;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",AC\n",
-    "UC=((Us*As)+(Uc*Ac))/(AC);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A=1160; # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t condensation \\t\"\n",
-    "print\"\\t It will be necessary to spread the batHes to a spacing of 18in.to compensate for the reduction in crossfiow area due to the flooded subcooling zone. The tube-side pressure drop will be the same as before. Assume bundle flooded to 0.3Ds.\\t\"\n",
-    "As=0.547; # ft**2\n",
-    "Gs=(W/(As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "De=0.0792; # fig 28\n",
-    "Res=((De)*(Gs)/0.0165); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "f=0.00121; # friction factor for reynolds number 193000, using fig.29\n",
-    "s=0.00454; # for reynolds number 193000,using fig.6\n",
-    "Ds=2.08; # ft\n",
-    "B=18\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPsc=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys)))/(2); # using eq.12.47,psi\n",
-    "print\"\\t delPsc is :  psi \\t\",round(delPsc)\n",
-    "print\"\\t delPss is negligible \\t\"\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#e \n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.6 pgno:299"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for carbon disulfide \t\n",
-      "\t total heat required for carbon disulfide is :  Btu/hr \t4200000\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t4200000.0\n",
-      "\t delt1 is :  F \t91.0\n",
-      "\t delt2 is :  F \t56.0\n",
-      "\t LMTD is : F \t72.1704928998\n",
-      "\t caloric temperature of hot fluid is :  F \t176.0\n",
-      "\t caloric temperature of cold fluid is :  F \t102.5\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t cold fluid:shell side,water \t\n",
-      "\t flow area is :  ft**2 \t0.1796875\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t667826.086957\n",
-      "\t reynolds number is :  \t31112.8388747\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t786.545454545\n",
-      "\t tw is :  F \t122.793674699\n",
-      "\t tf is :  F \t149.396837349\n",
-      "\t hot fluid:inner tube side,carbon disulfide \t\n",
-      "\t G1 is : lb/(hr)*(lin ft) \t1044.06562495\n",
-      "\t reynolds number is :  \t6141.56249973\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t0.251\n",
-      "\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t0.207493333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.207438610331\n",
-      "\t total surface area is :  ft**2 \t555.9216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t104.682978368\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-4.81115068056\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t flow area is :  ft**2 \t0.371208333333\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t80645.1612903\n",
-      "\t reynolds number is :  \t143770.856507\n",
-      "\t row is  ld/ft**3 \t0.572484035397\n",
-      "\t s is  \t0.00915974456635\n",
-      "\t delPt is :  psi \t0.4\n",
-      "\t allowable delPa is negligible psi \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t32.0\n",
-      "\t delPs is :  psi \t8.4\n",
-      "\t allowable delPT is 2 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=176.; # inlet hot fluid,F\n",
-    "T2=176.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=120000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for carbon disulfide \\t\"\n",
-    "l=140; # Btu/(lb)\n",
-    "Q=((W)*l); # Btu/hr\n",
-    "print\"\\t total heat required for carbon disulfide is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "Tc=((T2)+T1)/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "hio=300; # Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t cold fluid:shell side,water \\t\"\n",
-    "ID=17.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=6; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(w/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=1.7; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0792; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=103; # from fig.28\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Z=1.68; # Z=((c)*(mu1)/k)**(1/3); # prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "tf=(Tc+tw)/(2); # from eq 12.19\n",
-    "print\"\\t tf is :  F \\t\",tf\n",
-    "print\"\\t hot fluid:inner tube side,carbon disulfide \\t\"\n",
-    "kf=0.09; # Btu/(hr)*(ft**2)*(F/ft), from fig 14\n",
-    "sf=1.26; # from table 6\n",
-    "rowf=78.8; # lb/ft**3\n",
-    "muf=0.68; # cp, from fig 24\n",
-    "Nt=177;\n",
-    "D=0.0517; # ft\n",
-    "G1=(W/(3.14*Nt*D));\n",
-    "print\"\\t G1 is : lb/(hr)*(lin ft) \\t\",G1\n",
-    "Ret=((4)*(G1)/muf); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(0.251*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(1/3)); # hi*(((kf**3)*(rowf**2)*(4.17*10**8))/(muf**2))**(-1)=0.251, from fig 12.12\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=.75; #ft\n",
-    "hio1=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hio1 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio1\n",
-    "Uc=((hio1)*(ho)/(hio1+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "L=16;\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(30000/(0.372)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.029; # at inlet,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "row=(76.1/((359)*(636/492)*(14.7/39.7)));\n",
-    "print\"\\t row is  ld/ft**3 \\t\",row\n",
-    "s=(row/62.5);\n",
-    "print\"\\t s is  \\t\",s\n",
-    "f=0.000138; # friction factor for reynolds number 143000, using fig.26\n",
-    "delPt=((f*(Gt**2)*(16)*(1))/(5.22*(10**10)*(0.0517)*(s)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt+0.1,1)\n",
-    "print\"\\t allowable delPa is negligible psi \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.0017; # friction factor for reynolds number 31000, using fig.29\n",
-    "s=1; # for reynolds number 31000,using fig.6\n",
-    "Ds=17.25/12.; # ft\n",
-    "B=6.;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPT is 2 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 12.7 pgno:308"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 12.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t223.55\n",
-      "\t area is :  ft**2 \t31250.0\n",
-      "\t t2 is :  F \t86.0\n",
-      "\t circulation rate is :  gpm \t29176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 12.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "V=7.5; # fps\n",
-    "W=250000.;\n",
-    "CCl=0.85;\n",
-    "CT=1.;\n",
-    "CL=1.;\n",
-    "Ct=263.;\n",
-    "UD=(CCl*CT*CL*Ct*(V**(1/2)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(W/8);\n",
-    "print\"\\t area is :  ft**2 \\t\",A\n",
-    "a1=0.229; # ft**2/ft, table 10\n",
-    "at=0.475; # in**2, table 10\n",
-    "t1=70;\n",
-    "Ts=91.72; #F\n",
-    "n=2;\n",
-    "L=26;\n",
-    "t2=((Ts)-((Ts-t1)/((10)**(0.000279*UD*L*n*a1/(V*at))))+8); \n",
-    "print\"\\t t2 is :  F \\t\",round(t2) # calculation mistake in book\n",
-    "Go=(W*950)/((t2-t1)*500);\n",
-    "print\"\\t circulation rate is :  gpm \\t\",round(Go)\n",
-    "# end\n",
-    "\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration.ipynb
deleted file mode 100755
index 2fc8b593..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration.ipynb
+++ /dev/null
@@ -1,1123 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 14 : Evapouration"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.1 pgno:383"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tQevap is  Btu/hr\t9610000\n",
-      "\tQ300 degreeF is  Btu/hr\t9600500\n",
-      "\tTemperature head =  degree F\t74\n",
-      "\tOverall coefficient \t605.5\n",
-      "\tSurface required is  ft^2\t2144.75416788\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "t1 = 300; # degreeF\n",
-    "t2 = 226; #degree F\n",
-    "bs = 700; # Btu/((hr)(ft^2)(ddegree F))\n",
-    "#Heat Balance\n",
-    "Qv = 10000 * 961; # Btu/hr\n",
-    "print\"\\tQevap is  Btu/hr\\t\",Qv\n",
-    "Q3 = 10550 * 910; #Btu/hr\n",
-    "print\"\\tQ300 degreeF is  Btu/hr\\t\",Q3\n",
-    "\n",
-    "delT = t1-t2; # degree F\n",
-    "print\"\\tTemperature head =  degree F\\t\",delT\n",
-    "Ud = bs * 0.865;\n",
-    "print\"\\tOverall coefficient \\t\",Ud\n",
-    "A = Qv*10/(Ud * delT); #ft^2\n",
-    "print\"\\tSurface required is  ft^2\\t\",A#Wrong calculation in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.2 pgno:412"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tTotal product is lb/hr\t10000.0\n",
-      "\tTotal evaporation is lb/hr\t40000.0\n",
-      "\tTotal temperature difference is del degree F\t119\n",
-      "\tAverage pressure difference is del psi/effect \t8.25\n",
-      "\t\t\t\t\t\tPressure, psia\t\t delP, psi \t Steam or vapor, degree F \t lambda, Btu/lb\t\tSteam chest, 1st effect \t 26.70 \t\t\t .... \t\t Ts = 244 \t\t ls = 949 \t\tSteam chest, 2nd effect \t 18.45 \t\t\t 8.25 \t\t t1 = 224 \t\t l1 = 961 \t\tSteam chest, 3rd effect \t 10.20(20.7 in. Hg) \t 8.25 \t\t t2 = 194 \t\t l1 = 981 \t\tVapor to condenser \t\t 1.95(26 in. Hg) \t 8.25 \t\t t2 = 125 \t\t l1 = 1022 \t\n",
-      "\t949*Ws + 50000*(100-224) = 961*w1\t\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\t\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\t\tw1+w2+w3 = 40000\t\n",
-      "\tSolving simultaneously\t\n",
-      "\tw1 = \t12400\n",
-      "\tw2 = \t13300\n",
-      "\tw3 = \t14300\n",
-      "\tW1-3 is \t40000\n",
-      "\tA1 is ft**2 \t1510\n",
-      "\tA2 is ft**2 \t1588\n",
-      "\tA3 is ft**2 \t1512\n",
-      "\tHeat to condenser is Btu/hr\t14614600\n",
-      "\tWater requirement is lb/hr\t417560\n",
-      "\t= gpm \t835\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "wf = 50000; #  lb/hr\n",
-    "sf = wf * 0.10; #  lb/hr\n",
-    "tp = sf/0.50; # lb/hr\n",
-    "print\"\\tTotal product is lb/hr\\t\",tp\n",
-    "te = wf - tp;\n",
-    "print\"\\tTotal evaporation is lb/hr\\t\",te\n",
-    "cf = 1.0;\n",
-    "tF = 100;  # degree F\n",
-    "T1 = 244; # degree F\n",
-    "T2 = 125; # degree F\n",
-    "U1=600; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U2=250; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U3=125; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "\n",
-    "T = T1-T2;\n",
-    "print\"\\tTotal temperature difference is del degree F\\t\",T\n",
-    "df = (26.70- 1.95)/3; # psi/effect\n",
-    "print\"\\tAverage pressure difference is del psi/effect \\t\",df\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\tPressure, psia\\t\\t delP, psi \\t Steam or vapor, degree F \\t lambda, Btu/lb\\t\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\t .... \\t\\t Ts = 244 \\t\\t ls = 949 \\t\\tSteam chest, 2nd effect \\t 18.45 \\t\\t\\t 8.25 \\t\\t t1 = 224 \\t\\t l1 = 961 \\t\\tSteam chest, 3rd effect \\t 10.20(20.7 in. Hg) \\t 8.25 \\t\\t t2 = 194 \\t\\t l1 = 981 \\t\\tVapor to condenser \\t\\t 1.95(26 in. Hg) \\t 8.25 \\t\\t t2 = 125 \\t\\t l1 = 1022 \\t\"\n",
-    "\n",
-    "print\"\\t949*Ws + 50000*(100-224) = 961*w1\\t\\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\\t\\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\\t\\tw1+w2+w3 = 40000\\t\"\n",
-    "print\"\\tSolving simultaneously\\t\"\n",
-    "w1=12400;\n",
-    "print\"\\tw1 = \\t\",w1\n",
-    "w2=13300;\n",
-    "print\"\\tw2 = \\t\",w2\n",
-    "w3=14300;\n",
-    "print\"\\tw3 = \\t\",w3\n",
-    "\n",
-    "Wt = w1+w2+w3;\n",
-    "print\"\\tW1-3 is \\t\",Wt\n",
-    "Ws = 19100;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "Ts = 244;\n",
-    "t1 = 224;\n",
-    "t2 = 194;\n",
-    "t3 = 125;\n",
-    "\n",
-    "A1 = (Ws * lms)/(U1*(Ts-t1)); #ft**2\n",
-    "print\"\\tA1 is ft**2 \\t\",A1\n",
-    "A2 = (w1*lm1)/(U2*(t1-t2)); #ft**2\n",
-    "print\"\\tA2 is ft**2 \\t\",A2\n",
-    "A3 = (w2 * lm2)/(U3*(t2-t3)); #ft**2\n",
-    "print\"\\tA3 is ft**2 \\t\",A3\n",
-    "\n",
-    "hc = w3 * lm3; # Btu/hr, WRONG CALCULATION IN TEXT BOOK\n",
-    "print\"\\tHeat to condenser is Btu/hr\\t\",hc\n",
-    "wr = hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement is lb/hr\\t\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t= gpm \\t\",wr1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.3 pgno:414"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t981*w2 + 50000*(100-125) = 1022*w3\n",
-      "\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\n",
-      "\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\n",
-      "\tw1+w2+w3 = 40000\n",
-      "\n",
-      "\tSolving simultaneously\n",
-      "\n",
-      "\tw1-3 =  \n",
-      "40000\n",
-      "\tA1 is  ft**2\n",
-      "2010\n",
-      "\tA2 is  ft**2\n",
-      "2043\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tAverage surface is  ft**2\n",
-      "1700\n",
-      "\n",
-      "\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\n",
-      "5100\n",
-      "\tRecalculation\n",
-      "\n",
-      "\tA1 is  ft**2\n",
-      "0\n",
-      "\tA2 is  ft**2\n",
-      "0\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tTs-t3 is  degreeF\n",
-      "119\n",
-      "\t\t\t\t\tPressure, psia\t\t Steam or vapor, degreeF \t lambda, Btu/lb\n",
-      "\tSteam chest, 1st effect \t 26.70 \t\t\tTs = 244 \t\t 949 \n",
-      "\tSteam chest, 2nd effect \t 16.0 \t\t\t t1 = 216 \t\t 968 \n",
-      "\tSteam chest, 3rd effect \t 16.4 in. Hg) \t\t t2 = 175 \t\t 992 \n",
-      "\tVapor to condenser \t\t 26 in. Hg \t\t t3 = 125 \t\t l1 = 1022 \n",
-      "\n",
-      "\tw1 is \n",
-      "15450\n",
-      "\tw2 is \n",
-      "13200\n",
-      "\tw3 is \n",
-      "11350\n",
-      "\tWs is \n",
-      "16850\n",
-      "\tHeat to condenser is  Btu/hr\n",
-      "11599700\n",
-      "\tWater requirement  lb/hr\n",
-      "331420\n",
-      "\t\t\t= gpm\n",
-      "662\n",
-      "\tEconomy, lb evaporation/lb steam \n",
-      "2\n",
-      "\t\t\t\tForward\t\tBackward\n",
-      "\tTotal steam, lb/hr\t19100\t\t16850\n",
-      "\tCooling water, gpm\t840\t\t664\n",
-      "\tTotal surface, ft**2\t4800\t\t4500\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Same conditions as example 14.2\n",
-    "U1 = 400; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U2 = 250; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U3 = 175; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "\n",
-    "w1 = 50000; # lb/hr     From example 14.2\n",
-    "wt = 40000; # lb/hr     From example 14.2\n",
-    "cf = 1; # From example 14.2\n",
-    "\n",
-    "print\"\\t981*w2 + 50000*(100-125) = 1022*w3\\n\\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\\n\\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\\n\\tw1+w2+w3 = 40000\\n\"\n",
-    "print\"\\tSolving simultaneously\\n\"\n",
-    "w1 = 15950;\n",
-    "w2 = 12900;\n",
-    "w3 = 11150;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "\n",
-    "wt = w1+w2+w3;\n",
-    "print\"\\tw1-3 =  \\n\",wt\n",
-    "Ws = 16950;\n",
-    "A1 = (Ws*lms)/(U1*20); #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A1\n",
-    "A2 = (w1*lm1)/(U2*30); #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A2\n",
-    "A3 = (w2*lm2)/(U3*69); #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A3\n",
-    "\n",
-    "Avs = (A1 + A2 + A3)/3; #ft**2\n",
-    "print\"\\tAverage surface is  ft**2\\n\",Avs\n",
-    "Av1 = 3 * Avs; #ft**2\n",
-    "print\"\\n\\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\\n\",Av1\n",
-    "print\"\\tRecalculation\\n\"\n",
-    "Av2 = 1500; #ft**2, assume\n",
-    "dT1 = 28; #degreeF\n",
-    "A4 = (20/dT1)*A1; #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A4\n",
-    "dT2 = 41; #degreeF\n",
-    "A5  = (30/dT2)*A2; #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A5\n",
-    "dT3 = 50; #degreeF\n",
-    "A6 = (69/50)*A3; #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A6\n",
-    "del1 = 119; #degreeF\n",
-    "print\"\\tTs-t3 is  degreeF\\n\",del1\n",
-    "print\"\\t\\t\\t\\t\\tPressure, psia\\t\\t Steam or vapor, degreeF \\t lambda, Btu/lb\\n\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\tTs = 244 \\t\\t 949 \\n\\tSteam chest, 2nd effect \\t 16.0 \\t\\t\\t t1 = 216 \\t\\t 968 \\n\\tSteam chest, 3rd effect \\t 16.4 in. Hg) \\t\\t t2 = 175 \\t\\t 992 \\n\\tVapor to condenser \\t\\t 26 in. Hg \\t\\t t3 = 125 \\t\\t l1 = 1022 \\n\"\n",
-    "\n",
-    "w1 = 15450; #Solving again for \n",
-    "print\"\\tw1 is \\n\",w1\n",
-    "w2 = 13200;\n",
-    "print\"\\tw2 is \\n\",w2\n",
-    "w3 = 11350;\n",
-    "print\"\\tw3 is \\n\",w3\n",
-    "Ws = 16850;\n",
-    "print\"\\tWs is \\n\",Ws\n",
-    "Hc = w3 * 1022;\n",
-    "print\"\\tHeat to condenser is  Btu/hr\\n\",Hc\n",
-    "wr = Hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement  lb/hr\\n\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t\\t\\t= gpm\\n\",wr1\n",
-    "ec = wt/Ws;\n",
-    "print\"\\tEconomy, lb evaporation/lb steam \\n\",ec\n",
-    "\n",
-    "#comparision of forward and backward feed\n",
-    "print\"\\t\\t\\t\\tForward\\t\\tBackward\\n\\tTotal steam, lb/hr\\t19100\\t\\t16850\\n\\tCooling water, gpm\\t840\\t\\t664\\n\\tTotal surface, ft**2\\t4800\\t\\t4500\"\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.4 pgno:418"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.4 \n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\n",
-      "\n",
-      "\tEffects\t\tWater evaporated(lb/(hr)*(ft**2))\n",
-      "\n",
-      "\t1\t\t14-16\n",
-      "\t2\t\t6-8\n",
-      "\t3\t\t5-6\n",
-      "\t4\t\t4-5\n",
-      "\t5\t\t3-4\n",
-      "\n",
-      "\n",
-      "\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam  flow, lb/hr\t\t42600\t\t38000\n",
-      "\t2.Steam pressure, psi/in.Hg\t30\t\t30\t\t15\t\t5\t\t4\t\t14.5\n",
-      "\n",
-      "\t3.Steam temp,degreeF\t\t\t274\t\t274\t\t250\t\t227\t\t205\t\t181\n",
-      "\n",
-      "\t4.delT,degreeF\t\t\t23\t\t23\t\t21\t\t20\t\t20\t\t27\n",
-      "\t5.Liquor temp, degreeF\t\t251\t\t251\t\t229\t\t207\t\t185\t\t164\n",
-      "\t6.BPR, degreeF\t\t\t1\t\t1\t\t2\t\t2\t\t4\t\t7\n",
-      "\t7.Vapor temp, degreeF\t\t250\t\t250\t\t227\t\t205\t\t181\t\t147\n",
-      "\t8.Vapor pressure, pis/in.Hg\t15\t\t15\t\t5\t\t4\t\t14.5\t\t23\n",
-      "\t9.Lambda, Btu/lb\t\t946\t\t946\t\t960\t\t975\t\t990\t\t1010\n",
-      "\t10.Liquor in, lb/hr\t\t229000\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\n",
-      "\t11.Liqour out, lb/hr\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\t\t49600\n",
-      "\t12.Evaporation,lb/hr\t\t38800\t\t36200\t\t36900\t\t29300\t\t23800\t\t14400\n",
-      "\t13.degreeBrix(out)\t\t\t15.7\t\t19.4\t\t25.5\t\t34.4\t\t46.5\t\t50.0\n",
-      "\t14.A,ft**2\t\t\t3500\t\t3500\t\t5000\t\t5000\t\t5000\t\t3500\n",
-      "\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\t478\t\t425\t\t310\t\t264\t\t219\t\t138\n",
-      "\t16.UD delT,Btu/(hr)*(ft**2)\t11000\t\t9780\t\t6520\t\t5270\t\t4390\t\t3740\n",
-      "\n",
-      "\tTotal temperature difference in the evaporator system =  degreeF\n",
-      "127\n",
-      "\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\n",
-      "16\n",
-      "\tTotal EFFECTIVE  temperature difference = degreeF\n",
-      "111\n",
-      "\n",
-      "\t\t\t\tSUGAR-JUICE HEATERS\n",
-      "\n",
-      "\tRaw-juice heaters\t\t\t\tClear=juice heaters\n",
-      "\t-----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr 229000 212 184 5834920.0\n",
-      "\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\n",
-      "229000 243 220 4792970.0\n",
-      "\tVapor temp. = 227degreeF\tdelT=26.6degreeF\t\tVapor temp. = 250degreeF\tdelT=15.8degreeF\n",
-      "\n",
-      "\tud1=.\t\t\t\t\t\tUD=ud2\n",
-      "231 243\n",
-      "\tSurface,A=A1 ft**2\t\t\t\tSurface,A=A2 ft**2\n",
-      "\n",
-      "949.601275917 1248.36432776\n",
-      "\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr 229000 184 144 8244000.0\n",
-      "\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\n",
-      "229000 220 200 4122000.0\n",
-      "\tVapor temp. = 205degreeF\tdelT=37.6degreeF\t\tVapor temp. = 227degreeF\tdelT=14.8degreeF\n",
-      "\n",
-      "\tUD=Ud3\t\t\t\t\t\tUD=Ud4\n",
-      "230 214\n",
-      "\tSurface,A=A3 ft**2\t\t\t\tSurface,A=A4 ft**2\n",
-      "\n",
-      "953.2839963 1301.46501642\n",
-      "\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr 229000 144 82 4122000.0\n",
-      "\t(Use 2 heaters at 1300 ft**2 each plus 1\n",
-      "\t\t\t\t\t\t\theater at 1300 ft**2 as spare)\n",
-      "\n",
-      "\tVapor temp. = 181degreeF\tdelT=62.2degreeF\n",
-      "\tSurface,A=\n",
-      "946.715663757\n",
-      "\t(Use 3 heaters at 100 ft**2\n",
-      "\teach plus 1 heater as spare)\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t----------------------------------------------------\n",
-      "\n",
-      "\t1A.Heat in steam........\n",
-      "38388138.0\n",
-      "\t   Heating liquor.......\n",
-      "\t\t\t\t%.3e\t.\n",
-      "1667120.0 36721018.0 38817.1437632\n",
-      "\t   Liqour to 1B\n",
-      "\t   =  lb/hr\n",
-      "190182.856237\n",
-      "\t1B.Heat in steam........\n",
-      "34979292.7593\n",
-      "\t   Heating liquor........\n",
-      "\t\t\t\t\n",
-      "0.0 34979292.7593 36975.9965744\n",
-      "\t   Liqour to 2d \n",
-      "\t   effect= lb/hr\n",
-      "153206.859662\n",
-      "\t\t\t\t\t\t\t\tLb/hr\n",
-      "\n",
-      "\t(a) Actual evaporation..................................\n",
-      "179400\n",
-      "\t(b) Equivalent evaporation from vapors of \n",
-      "\t    1st effect used for vaccum pans......................\n",
-      "145500\n",
-      "\t(c) Equivalent evaporation from 1st effect \n",
-      "\t    vapors used for clarified-juice heaters..............\n",
-      "19700\n",
-      "\t(d) Equivalent evaporation from 2d effect \n",
-      "\t    vapors used for clarified-and raw-juice heaters......\n",
-      "30600\n",
-      "\t(e) Equivalent evaporation from 3d effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "2.71828182846\n",
-      "\t(f) Equivalent evaporation from 4th effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "13100\n",
-      "\t                                                        -----\n",
-      "\n",
-      "\t     Extrapolated evaporation............................\n",
-      "406200\n",
-      "\t\tEstimated steam quantity =  lb/hr\n",
-      "81240\n",
-      "\t\tActual steam required from final heat balance =  lb/hr\n",
-      "80600\n",
-      "\t\t\t\t\t\t\tError =  lb/hr\n",
-      "640\n",
-      "\tGallons per minute of Water required =  gpm 583\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.4 \\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "from math import e\n",
-    "#Assumed that 37500 lb/hr of 15 psig vapor is bled from the first effect for use in thevaccum pans\n",
-    "print\"\\n\\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\\n\"\n",
-    "print\"\\tEffects\\t\\tWater evaporated(lb/(hr)*(ft**2))\\n\"\n",
-    "print\"\\t1\\t\\t14-16\\n\\t2\\t\\t6-8\\n\\t3\\t\\t5-6\\n\\t4\\t\\t4-5\\n\\t5\\t\\t3-4\\n\"\n",
-    "print\"\\n\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t42600\\t\\t38000\\n\\t2.Steam pressure, psi/in.Hg\\t30\\t\\t30\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\n\"\n",
-    "print\"\\t3.Steam temp,degreeF\\t\\t\\t274\\t\\t274\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\n\"\n",
-    "print\"\\t4.delT,degreeF\\t\\t\\t23\\t\\t23\\t\\t21\\t\\t20\\t\\t20\\t\\t27\\n\\t5.Liquor temp, degreeF\\t\\t251\\t\\t251\\t\\t229\\t\\t207\\t\\t185\\t\\t164\\n\\t6.BPR, degreeF\\t\\t\\t1\\t\\t1\\t\\t2\\t\\t2\\t\\t4\\t\\t7\\n\\t7.Vapor temp, degreeF\\t\\t250\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\t\\t147\\n\\t8.Vapor pressure, pis/in.Hg\\t15\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\t\\t23\\n\\t9.Lambda, Btu/lb\\t\\t946\\t\\t946\\t\\t960\\t\\t975\\t\\t990\\t\\t1010\\n\\t10.Liquor in, lb/hr\\t\\t229000\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\n\\t11.Liqour out, lb/hr\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\t\\t49600\\n\\t12.Evaporation,lb/hr\\t\\t38800\\t\\t36200\\t\\t36900\\t\\t29300\\t\\t23800\\t\\t14400\\n\\t13.degreeBrix(out)\\t\\t\\t15.7\\t\\t19.4\\t\\t25.5\\t\\t34.4\\t\\t46.5\\t\\t50.0\\n\\t14.A,ft**2\\t\\t\\t3500\\t\\t3500\\t\\t5000\\t\\t5000\\t\\t5000\\t\\t3500\\n\\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\\t478\\t\\t425\\t\\t310\\t\\t264\\t\\t219\\t\\t138\\n\\t16.UD delT,Btu/(hr)*(ft**2)\\t11000\\t\\t9780\\t\\t6520\\t\\t5270\\t\\t4390\\t\\t3740\\n\"#BPR values from fig 14.34a\n",
-    "#Saturate vapor pressure above the liquour determined from Table 7\n",
-    "#Saturated steam pressure in the following effect determined from Table 7\n",
-    "\n",
-    "t1 = 274; #degreeF\n",
-    "t2 = 147; #degreeF\n",
-    "t = t1-t2; #degreeF\n",
-    "print\"\\tTotal temperature difference in the evaporator system =  degreeF\\n\",t\n",
-    "bpr1 = 1; #degreeF\n",
-    "bpr2 = 2; #degreeF\n",
-    "bpr3 = 2; #degreeF\n",
-    "bpr4 = 4; #degreeF\n",
-    "bpr5 = 7; #degreeF\n",
-    "bpr = bpr1 + bpr2 + bpr3 + bpr4 + bpr5; #degreeF\n",
-    "print\"\\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\\n\",bpr\n",
-    "tf = t-bpr; #degreeF\n",
-    "print\"\\tTotal EFFECTIVE  temperature difference = degreeF\\n\",tf\n",
-    "lbh = 229000; #lb/hr\n",
-    "tp1=212; #degreeF\n",
-    "tp2=184; #degreeF\n",
-    "tp3=144; #degreeF\n",
-    "tp4=82; #degreeF\n",
-    "tj1=243; #degreeF\n",
-    "tj2=220; #degreeF\n",
-    "tj3=200; #degreeF\n",
-    "Ud1=231;\n",
-    "Ud2=243;\n",
-    "Ud3=230;\n",
-    "Ud4=214;\n",
-    "Ud5=217;\n",
-    "print\"\\n\\t\\t\\t\\tSUGAR-JUICE HEATERS\\n\"\n",
-    "print\"\\tRaw-juice heaters\\t\\t\\t\\tClear=juice heaters\\n\\t-----------------------------------------------------------------------------------------\\n\"\n",
-    "rj1=lbh*(tp1-tp2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr\",lbh,tp1,tp2,rj1\n",
-    "rj2=lbh*(tj1-tj2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\\n\",lbh,tj1,tj2,rj2\n",
-    "print\"\\tVapor temp. = 227degreeF\\tdelT=26.6degreeF\\t\\tVapor temp. = 250degreeF\\tdelT=15.8degreeF\\n\"\n",
-    "print\"\\tud1=.\\t\\t\\t\\t\\t\\tUD=ud2\\n\",Ud1,Ud2\n",
-    "A1=rj1/(26.6*Ud1);#ft**2\n",
-    "A2=rj2/(15.8*Ud2);#ft**2\n",
-    "print\"\\tSurface,A=A1 ft**2\\t\\t\\t\\tSurface,A=A2 ft**2\\n\\n\",A1,A2\n",
-    "\n",
-    "rj3=lbh*(tp2-tp3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr\",lbh,tp2,tp3,rj3\n",
-    "rj4=lbh*(tj2-tj3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\\n\",lbh,tj2,tj3,rj4\n",
-    "print\"\\tVapor temp. = 205degreeF\\tdelT=37.6degreeF\\t\\tVapor temp. = 227degreeF\\tdelT=14.8degreeF\\n\"\n",
-    "print\"\\tUD=Ud3\\t\\t\\t\\t\\t\\tUD=Ud4\\n\",Ud3,Ud4\n",
-    "A3=rj3/(37.6*Ud3);#ft**2\n",
-    "A4=rj4/(14.8*Ud4);#ft**2\n",
-    "print\"\\tSurface,A=A3 ft**2\\t\\t\\t\\tSurface,A=A4 ft**2\\n\\n\",A3,A4\n",
-    "\n",
-    "rj5=lbh*(tp3-tp4)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr\",lbh,tp3,tp4,rj4\n",
-    "print\"\\t(Use 2 heaters at 1300 ft**2 each plus 1\\n\\t\\t\\t\\t\\t\\t\\theater at 1300 ft**2 as spare)\\n\"\n",
-    "A5=rj5/(62.2*Ud5);#ft**2\n",
-    "print\"\\tVapor temp. = 181degreeF\\tdelT=62.2degreeF\\n\\tSurface,A=\\n\",A5\n",
-    "print\"\\t(Use 3 heaters at 100 ft**2\\n\\teach plus 1 heater as spare)\\n\\n\"\n",
-    "\n",
-    "v1=42600;#lb/hr\n",
-    "tt1=251;#degreeF\n",
-    "print\"\\t\\t\\t\\tHEAT BALANCE\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t----------------------------------------------------\\n\"\n",
-    "hia=v1*929*0.97;#Btu/hr\n",
-    "print\"\\t1A.Heat in steam........\\n\",hia\n",
-    "hla=lbh*(tt1-tj1)*0.91;#Btu/hr\n",
-    "hh=hia-hla;#Btu/hr\n",
-    "lb1=946;#Btu/lb\n",
-    "dif=hh/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor.......\\n\\t\\t\\t\\t%.3e\\t.\\n\",hla,hh,dif\n",
-    "ltob=lbh-dif;#lb/hr\n",
-    "print\"\\t   Liqour to 1B\\n\\t   =  lb/hr\\n\",ltob\n",
-    "hia1=dif*929*0.97;#Btu/hr\n",
-    "print\"\\t1B.Heat in steam........\\n\",hia1\n",
-    "hla1=ltob*(tt1-tt1)*0.91;#Btu/hr\n",
-    "hh1=hia1;#Btu/hr\n",
-    "dif1=hh1/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor........\\n\\t\\t\\t\\t\\n\",hla1,hh1,dif1\n",
-    "dif2=ltob-dif1;#lb/hr\n",
-    "print\"\\t   Liqour to 2d \\n\\t   effect= lb/hr\\n\",dif2\n",
-    "#Similarily the values in the table are calculated\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\tLb/hr\\n\"\n",
-    "aa=179400;#lb/hr\n",
-    "bb=145500;#lb/hr\n",
-    "cc=19700;#lb/hr\n",
-    "dd=30600;#lb/hr\n",
-    "ee=17900;#lb/hr\n",
-    "ff=13100;#lb/hr\n",
-    "tto=aa+bb+cc+dd+ee+ff;#lb/hr\n",
-    "print\"\\t(a) Actual evaporation..................................\\n\",aa\n",
-    "print\"\\t(b) Equivalent evaporation from vapors of \\n\\t    1st effect used for vaccum pans......................\\n\",bb\n",
-    "print\"\\t(c) Equivalent evaporation from 1st effect \\n\\t    vapors used for clarified-juice heaters..............\\n\",cc\n",
-    "print\"\\t(d) Equivalent evaporation from 2d effect \\n\\t    vapors used for clarified-and raw-juice heaters......\\n\",dd\n",
-    "print\"\\t(e) Equivalent evaporation from 3d effect \\n\\t    vapors used for raw-juice heaters....................\\n\",e\n",
-    "print\"\\t(f) Equivalent evaporation from 4th effect \\n\\t    vapors used for raw-juice heaters....................\\n\",ff\n",
-    "print\"\\t                                                        -----\\n\"\n",
-    "print\"\\t     Extrapolated evaporation............................\\n\",tto\n",
-    "esq=tto/5;#lb/hr\n",
-    "print\"\\t\\tEstimated steam quantity =  lb/hr\\n\",esq\n",
-    "aesq=80600;#lb/hr\n",
-    "err = esq-aesq;#lb/hr\n",
-    "print\"\\t\\tActual steam required from final heat balance =  lb/hr\\n\",aesq\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\tError =  lb/hr\\n\",err\n",
-    "ta=15;\n",
-    "Q=14575000; #Btu/hr Total hourly evaporation\n",
-    "Gpm=Q/(500*(t2-tp4-ta));#From equation 14.4\n",
-    "print\"\\tGallons per minute of Water required =  gpm\",Gpm\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.5 pgno:427"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 9,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.5\t\n",
-      "\tapproximate values are mentioned in the book \t\n",
-      "\tOverall temperature difference =  deg F\t155\n",
-      "\tThe estimated total BPR =  degF\t[10 18 25 31 36 41]\n",
-      "\tEffective temperature difference = %.0f degF\t[145 137 130 124 119 114]\n",
-      "\t\t\t\t\tEVAPORATOR SUMMARY\t\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\t\t\t\t\t\t----------------------------------------------------------------------------------------------\t\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\t1.Steam  flow, lb/hr\t\t20000\t\t2.Steam pressure, psi/in.Hg\t35\t\t14.5\t\t4\t\t7\t\t16.5\t\t22\t\t3.Steam temp,degF\t\t\t280\t\t249\t\t224\t\t199\t\t174\t\t151\t\t4.delT,degF\t\t\t21\t\t17\t\t18\t\t19\t\t18\t\t21\t\t5.Liquor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t6.BPR, degF\t\t\t10\t\t8\t\t7\t\t6\t\t5\t\t5\t\t7.Vapor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t8.Vapor pressure, pis/in.Hg\t14.5\t\t4\t\t7\t\t6\t\t5\t\t5\t\t9.Lambda, Btu/lb\t\t946\t\t962\t\t978\t\t994\t\t1008\t\t1022\t\t10.Liquor in, lb/hr\t\t73400\t\t88300\t\t101000\t\t113000\t\t72000\t\t72000\t\t11.Liqour out, lb/hr\t\t56200\t\t73400\t\t88300\t\t101100\t\t58300\t\t54700\t\t12.Evaporation,lb/hr\t\t17200\t\t14900\t\t12800\t\t11900\t\t13700\t\t17300\t\t13.Total solids, \t\t38.9\t\t29.8\t\t24.7\t\t21.6\t\t18.7\t\t20.0\t\t14.A,ft^2\t\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t15.UD,Btu/(hr)*(ft^2)*(degF)\t262\t\t295\t\t252\t\t251\t\t221\t\t221\t\t16.UD delT,Btu/(hr)*(ft^2)\t5510\t\t5000\t\t4530t\t\t4770\t\t3980\t\t4650\t\n",
-      "\t\tTotal amount of water evaporated = \t lb/hr\t[17200 32100 44900 56800 70500     0]\n",
-      "\tTheoretical amount of steam for a six-effect evaporator = \t lb/hr\t[ 2866  5350  7483  9466 11750     0]\n",
-      "\tSteam used for trail balance = \t lb/hr\t[  3822.22222222   7133.33333333   9977.77777778  12622.22222222\n",
-      "  15666.66666667      0.        ]\n",
-      "\tEstimate of the amount of evaporation in the first effect = \t lb/hr\t[  3295.9    6152.5    8605.45  10885.9   13512.5       0.  ]\n",
-      "\tEstimated discharge from second effect = \t lb/hr\t[ 59495.9   62352.5   64805.45  67085.9   69712.5   56200.  ]\n",
-      "\t\t\t\t\tHEAT BALANCE\t\n",
-      "\t\tCooling water at 60 degreeF = \t gpm\t710\n",
-      "\t--------------------------------------------------------\t\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\t\n",
-      "\t--------------------------------------------------------\t\n",
-      "\t1.a.Heat in steam \t\t17925600.0\n",
-      "\t  b.Heating liquor \t\t1625076.0\n",
-      "\t  c.Evaporation\t\t\t\t\t\t17230.9978858\n",
-      "\t  d.To flash tank\t2190591.08245\n",
-      "\t\t\t\t2239.86818247\n",
-      "\t  e.Flashed vapor=\t\t2239.86818247\n",
-      "\t  f.product \t53929.1339317\n",
-      "\t\t2.a.Heat in 1st vapors\t\t16300524.0\n",
-      "\t  b.Heating liqour\t\t1951430.0\n",
-      "\t  c.Evaporation= 14915.8981289\n",
-      "\t\t\t\t\t14915.8981289\n",
-      "\t  d.Liquor to 1b=\t\t73384.1018711\n",
-      "total hourly evapouration lb : 90000\n",
-      "economy is lb/lb : 4.5\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.5\\t\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\t\"\n",
-    "st1=280; #degF\n",
-    "vt6=125; #degF\n",
-    "odT=st1-vt6; #degF\n",
-    "print\"\\tOverall temperature difference =  deg F\\t\",odT #corresponding to 35 psig and 26 in. Hg\n",
-    "import numpy\n",
-    "bpr=numpy.array([10, 8, 7, 6, 5, 5])\n",
-    "#bpr(1)=10; #degF\n",
-    "#bpr(2)=8; #degF\n",
-    "#bpr(3)=7; #degF\n",
-    "#bpr(4)=6; #degF\n",
-    "#bpr(5)=5; #degF\n",
-    "#bpr(6)=5; #degF\n",
-    "i=1;\n",
-    "tbpr=numpy.array([0, 0, 0, 0, 0, 0]);\n",
-    "tbpr[0]=bpr[0];\n",
-    "while (i<6):\n",
-    "\n",
-    "    tbpr[i]=tbpr[i-1]+bpr[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\tThe estimated total BPR =  degF\\t\",tbpr #from fig. 14.36a\n",
-    "edT=odT-tbpr;\n",
-    "print\"\\tEffective temperature difference = %.0f degF\\t\",edT\n",
-    "print\"\\t\\t\\t\\t\\tEVAPORATOR SUMMARY\\t\\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\t\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\t\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t20000\\t\\t2.Steam pressure, psi/in.Hg\\t35\\t\\t14.5\\t\\t4\\t\\t7\\t\\t16.5\\t\\t22\\t\\t3.Steam temp,degF\\t\\t\\t280\\t\\t249\\t\\t224\\t\\t199\\t\\t174\\t\\t151\\t\\t4.delT,degF\\t\\t\\t21\\t\\t17\\t\\t18\\t\\t19\\t\\t18\\t\\t21\\t\\t5.Liquor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t6.BPR, degF\\t\\t\\t10\\t\\t8\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t7.Vapor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t8.Vapor pressure, pis/in.Hg\\t14.5\\t\\t4\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t9.Lambda, Btu/lb\\t\\t946\\t\\t962\\t\\t978\\t\\t994\\t\\t1008\\t\\t1022\\t\\t10.Liquor in, lb/hr\\t\\t73400\\t\\t88300\\t\\t101000\\t\\t113000\\t\\t72000\\t\\t72000\\t\\t11.Liqour out, lb/hr\\t\\t56200\\t\\t73400\\t\\t88300\\t\\t101100\\t\\t58300\\t\\t54700\\t\\t12.Evaporation,lb/hr\\t\\t17200\\t\\t14900\\t\\t12800\\t\\t11900\\t\\t13700\\t\\t17300\\t\\t13.Total solids, \\t\\t38.9\\t\\t29.8\\t\\t24.7\\t\\t21.6\\t\\t18.7\\t\\t20.0\\t\\t14.A,ft^2\\t\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t15.UD,Btu/(hr)*(ft^2)*(degF)\\t262\\t\\t295\\t\\t252\\t\\t251\\t\\t221\\t\\t221\\t\\t16.UD delT,Btu/(hr)*(ft^2)\\t5510\\t\\t5000\\t\\t4530t\\t\\t4770\\t\\t3980\\t\\t4650\\t\"#BPR values from fig 14.36a\n",
-    "#Specific-heat data are given in Fig. 14.36b\n",
-    "ev=numpy.array([17200, 14900, 12800, 11900, 13700, 17300]);\n",
-    "#ev(1)=17200; #lb/hr\n",
-    "#ev(2)=14900; #lb/hr\n",
-    "#ev(3)=12800; #lb/hr\n",
-    "#ev(4)=11900; #lb/hr\n",
-    "#ev(5)=13700; #lb/hr\n",
-    "#ev(6)=17300; #lb/hr\n",
-    "i=1;\n",
-    "tev =numpy.array([0, 0, 0, 0, 0, 0])\n",
-    "tev[0]=ev[0];\n",
-    "while (i<5):\n",
-    "    tev[i]= tev[i-1]+ev[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\tTotal amount of water evaporated = \\t lb/hr\\t\",tev\n",
-    "ttev=tev/6;#lb/hr\n",
-    "print\"\\tTheoretical amount of steam for a six-effect evaporator = \\t lb/hr\\t\",ttev\n",
-    "tev2=tev/(6*0.75); #lb/hr . order of 75 percent of theoretical\n",
-    "print\"\\tSteam used for trail balance = \\t lb/hr\\t\",tev2\n",
-    "lq=(tev/6);\n",
-    "lq=lq+(lq*0.15);\n",
-    "print\"\\tEstimate of the amount of evaporation in the first effect = \\t lb/hr\\t\",lq\n",
-    "lout6=54000;#lb/hr\n",
-    "lq2=lout6+lq+2200;#lb/hr\n",
-    "print\"\\tEstimated discharge from second effect = \\t lb/hr\\t\",lq2\n",
-    "print\"\\t\\t\\t\\t\\tHEAT BALANCE\\t\"\n",
-    "cw = 17750000/(500*(125-15-60)); #gpm, values from table 14.6\n",
-    "print\"\\t\\tCooling water at 60 degreeF = \\t gpm\\t\",cw\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\t\"\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "sf=20000;#lb/hr\n",
-    "lqi=73400;#lb/hr\n",
-    "the=90000;\n",
-    "lqi2=88300\n",
-    "lt1=259;#degreeF\n",
-    "lt2=232;#degreeF\n",
-    "lt3=206;#degreeF\n",
-    "ecn=90000./20000.;\n",
-    "ev=17200;#lb/hr\n",
-    "his=sf*924*0.97;#Btu/hr\n",
-    "print\"\\t1.a.Heat in steam \\t\\t\",his\n",
-    "hl=lqi*(lt1-lt2)*0.82;#Btu/hr\n",
-    "print\"\\t  b.Heating liquor \\t\\t\",hl\n",
-    "hh=his-hl;\n",
-    "ev1=(hh)/946;#lb/hr\n",
-    "print\"\\t  c.Evaporation\\t\\t\\t\\t\\t\\t\",ev1\n",
-    "dif=lqi-ev1;\n",
-    "tft=(dif)*(lt1-209)*0.78;\n",
-    "print\"\\t  d.To flash tank\\t\",tft\n",
-    "ev2=tft/978;#lb/hr\n",
-    "print\"\\t\\t\\t\\t\",ev2\n",
-    "print\"\\t  e.Flashed vapor=\\t\\t\",ev2\n",
-    "p=dif-ev2;\n",
-    "print\"\\t  f.product \\t\",p\n",
-    "print\"\\t\\t2.a.Heat in 1st vapors\\t\\t\",hh\n",
-    "hl2=lqi2*(lt2-lt3)*0.85;\n",
-    "print\"\\t  b.Heating liqour\\t\\t\",hl2\n",
-    "ev3=(hh-hl2)/962;\n",
-    "print\"\\t  c.Evaporation=\",ev3\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\",ev3\n",
-    "lto1=lqi2-ev3;\n",
-    "print\"\\t  d.Liquor to 1b=\\t\\t\",lto1\n",
-    "print\"total hourly evapouration lb :\",the\n",
-    "print\"economy is lb/lb :\",ecn\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.6 pgno:437"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.6\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tTotal temperature difference =  degreeF\n",
-      "159\n",
-      "\tThe effective temperature difference is  degreeF\n",
-      "56\n",
-      "\n",
-      "\t\t\tCAUSTIC EVAPORATOR MATERIAL BALANCE\n",
-      "\n",
-      "\tCell liquour at 120degreeF \t\tWash at 80degreeF\n",
-      "\n",
-      "\t---------------------------------------------\n",
-      "\n",
-      "\t8.75 prcnt NaOH = l1\n",
-      "\t16.6 prcnt NaCl = l2\t\t25 prcnt NaCl = w2\n",
-      "2000 3800 340\n",
-      "\t74.65 prcnt H20 = l3\t\t75 prcnt H20 = w2\n",
-      "17050 1020\n",
-      "\tTotal cell liquor = lq\tTotoal wash = w\n",
-      "22850 1360\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\t\t\t\tNaOH\t\tNaCl\t\tH20,Lb\tTotal,Lb\n",
-      "\t\t\t\tprcnt\tLb\tprcnt\tLb\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\tOverall operation:\n",
-      "\t  Cell liquor.......... 8.75\t2000 3800 17050 22850\n",
-      "\t  Wash................. ....\t....\t25.00\t340 1020 1360\n",
-      "\t  Total in............. ....\t2000 4140 18070 24210\n",
-      "\t  Product.............. 50.00\t2000 110 1890 4000\n",
-      "\t  Removed.............. ....\t....\t....\t\t%.0f\t%.0f\n",
-      "4030 16180 20210\n",
-      "\n",
-      "\t\t\t\t\tCAUSTIC EVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t--------------------\t\tFlash Tank\n",
-      "\t\t\t\t\t\\I\t\tII\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam pressure, psi/in.Hg\t30\n",
-      "\t2.Steam temperature,degreeF\t\t274\t\t169\n",
-      "\t3.delT,degreeF\t\t\t28\t\t28\n",
-      "\t4.Liquor temperature, degreeF\t246\t\t141\t\t192\n",
-      "\t5.BPR, degreeF\t\t\t77\t\t26\t\t77\n",
-      "\t6.Vapor temperature, degreeF\t\t169\t\t115\t\t115\n",
-      "\t7.Lambda, Btu/lb\t\t997\t\t1027\t\t1027\n",
-      "\t8.Feed, lb/hr\t\t\t22788\t\t50602\t\t13367\n",
-      "\t9.Product, lb/hr\t\t13367\t\t40352\t\t12813\n",
-      "\t10.Evaporation,lb/hr\t\t9421\t\t10250\t\t554\n",
-      "\t11.Heat flow, Btu/hr\t\t11890000\t11020000\n",
-      "\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\t700\n",
-      "\t13.A,ft**2\t\t\t683\t\t683\n",
-      "\t14.Tubes, OD, in. and BWG\t1,16\t\t1,16\n",
-      "\t15.Tube length, ft\t\t7\t\t7\n",
-      "\t16.No. tubes\t\t\t432\t\t432\n",
-      "\t17.Circulating pump. gpm\t3200 at 20 ft\t3200 at 20ft\t167 at 45 ft\n",
-      "\t18.Apparent efficiency, prcnt\t54\t\t64\n",
-      "\t18.BHP\t\t\t\t38\t\t35\t\t8.2\n",
-      "\t20.Motor,hp\t\t\t40\t\t40\t\t10.0\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\n",
-      "2700000.0\n",
-      "\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t251\t2970000\t\t25.4\t700\t670\t0.87\t\t3420000\n",
-      "\t252\t2480000\t\t25.0\t700\t680\t0.88\t\t2820000\n",
-      "\t252.5\t2290000\t\t24.7\t700\t685\t0.89\t\t2570000\t\t700\n",
-      "\t253\t2120000\t\t24.5\t700\t695\t0.90\t\t2520000\n",
-      "\n",
-      "\tThee gain per minute is gpm\n",
-      "3200\n",
-      "\n",
-      "\t\t\t\tCAUSTIC EVAPORATION HEAT BALANCE\n",
-      "\n",
-      "\t\t\t\t(Basis = 1ton/hr NaOH)\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t\tEFFECT\t\t\tBtu/hr\t\tEvaopration, lb/hr\n",
-      "\n",
-      "\t1.a.Heat in steam\t\thi\n",
-      "\t  b.Heating liquor\t\thl\n",
-      "\t  c.Resultant heat\t\trhf\n",
-      "\t  d.Heat of concentrate\t\thc\n",
-      "\t  e.Heat of vapors\t\thv\t%.0f\n",
-      "9511110.0 1452566.4 8058543.6 300000 7758543.6 7781.8892678\n",
-      "\n",
-      "\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\n",
-      "2430000.0\n",
-      "\tUD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t146\t2400000\t\t25.4\t700\t620\t0.80\t\t2790000\t\t700\n",
-      "\t146.5\t2160000\t\t25.2\t700\t683\t0.89\t\t2430000\n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.6\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "st1=274; #degreeF\n",
-    "vt6=115; #degreeF\n",
-    "odT=st1-vt6; #degreeF\n",
-    "print\"\\tTotal temperature difference =  degreeF\\n\",odT #corresponding to 35 psig\n",
-    "eb1=77;#degreeF, From fig.14.38\n",
-    "eb2=26;#degreeF, From fig.14.38\n",
-    "etd=odT-(eb1+eb2);#degreeF\n",
-    "print\"\\tThe effective temperature difference is  degreeF\\n\",etd\n",
-    "print\"\\n\\t\\t\\tCAUSTIC EVAPORATOR MATERIAL BALANCE\\n\"\n",
-    "#Basis: 1 ton/hr NaOH\n",
-    "print\"\\tCell liquour at 120degreeF \\t\\tWash at 80degreeF\\n\"\n",
-    "print\"\\t---------------------------------------------\\n\"\n",
-    "l1=2000;#Lb\n",
-    "l2=3800;#Lb\n",
-    "l3=17050;#Lb\n",
-    "lq=l1+l2+l3;#Lb\n",
-    "w1=340;#Lb\n",
-    "w2=1020;#Lb\n",
-    "w=w1+w2;#Lb\n",
-    "print\"\\t8.75 prcnt NaOH = l1\\n\\t16.6 prcnt NaCl = l2\\t\\t25 prcnt NaCl = w2\\n\",l1,l2,w1\n",
-    "print\"\\t74.65 prcnt H20 = l3\\t\\t75 prcnt H20 = w2\\n\",l3,w2\n",
-    "print\"\\tTotal cell liquor = lq\\tTotoal wash = w\\n\",lq,w\n",
-    "print\"\\n\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\t\\t\\tNaOH\\t\\tNaCl\\t\\tH20,Lb\\tTotal,Lb\\n\\t\\t\\t\\tprcnt\\tLb\\tprcnt\\tLb\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tOverall operation:\\n\\t  Cell liquor.......... 8.75\\t\",l1,l2,l3,lq\n",
-    "print\"\\t  Wash................. ....\\t....\\t25.00\\t\",w1,w2,w\n",
-    "wl1=l2+w1;#Lb\n",
-    "wl2=l3+w2;#Lb\n",
-    "wlt=lq+w;\n",
-    "print\"\\t  Total in............. ....\\t\",l1,wl1,wl2,wlt\n",
-    "prn=110;#Lb\n",
-    "prh=1890;#Lb\n",
-    "prt=4000;#Lb\n",
-    "print\"\\t  Product.............. 50.00\\t\",l1,prn,prh,prt\n",
-    "r1=wl1-prn;#Lb\n",
-    "r2=wl2-prh;#Lb\n",
-    "r3=wlt-prt;#Lb\n",
-    "gain=3200;#gpm\n",
-    "print\"\\t  Removed.............. ....\\t....\\t....\\t\\t%.0f\\t%.0f\\n\",r1,r2,r3\n",
-    "#Rest of the table is calculated similarily\n",
-    "print\"\\n\\t\\t\\t\\t\\tCAUSTIC EVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t--------------------\\t\\tFlash Tank\\n\\t\\t\\t\\t\\t\\I\\t\\tII\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam pressure, psi/in.Hg\\t30\\n\\t2.Steam temperature,degreeF\\t\\t274\\t\\t169\\n\\t3.delT,degreeF\\t\\t\\t28\\t\\t28\\n\\t4.Liquor temperature, degreeF\\t246\\t\\t141\\t\\t192\\n\\t5.BPR, degreeF\\t\\t\\t77\\t\\t26\\t\\t77\\n\\t6.Vapor temperature, degreeF\\t\\t169\\t\\t115\\t\\t115\\n\\t7.Lambda, Btu/lb\\t\\t997\\t\\t1027\\t\\t1027\\n\\t8.Feed, lb/hr\\t\\t\\t22788\\t\\t50602\\t\\t13367\\n\\t9.Product, lb/hr\\t\\t13367\\t\\t40352\\t\\t12813\\n\\t10.Evaporation,lb/hr\\t\\t9421\\t\\t10250\\t\\t554\\n\\t11.Heat flow, Btu/hr\\t\\t11890000\\t11020000\\n\\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\\t700\\n\\t13.A,ft**2\\t\\t\\t683\\t\\t683\\n\\t14.Tubes, OD, in. and BWG\\t1,16\\t\\t1,16\\n\\t15.Tube length, ft\\t\\t7\\t\\t7\\n\\t16.No. tubes\\t\\t\\t432\\t\\t432\\n\\t17.Circulating pump. gpm\\t3200 at 20 ft\\t3200 at 20ft\\t167 at 45 ft\\n\\t18.Apparent efficiency, prcnt\\t54\\t\\t64\\n\\t18.BHP\\t\\t\\t\\t38\\t\\t35\\t\\t8.2\\n\\t20.Motor,hp\\t\\t\\t40\\t\\t40\\t\\t10.0\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "V=8;\n",
-    "s=1.5;\n",
-    "G=V*s*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\\n\",G\n",
-    "UD=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Combining with a steam film coefficient of approximately 1500\n",
-    "print\"\\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t251\\t2970000\\t\\t25.4\\t700\\t670\\t0.87\\t\\t3420000\\n\\t252\\t2480000\\t\\t25.0\\t700\\t680\\t0.88\\t\\t2820000\\n\\t252.5\\t2290000\\t\\t24.7\\t700\\t685\\t0.89\\t\\t2570000\\t\\t700\\n\\t253\\t2120000\\t\\t24.5\\t700\\t695\\t0.90\\t\\t2520000\\n\"\n",
-    "print\"\\tThee gain per minute is gpm\\n\",gain\n",
-    "print\"\\n\\t\\t\\t\\tCAUSTIC EVAPORATION HEAT BALANCE\\n\"\n",
-    "print\"\\t\\t\\t\\t(Basis = 1ton/hr NaOH)\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\tEFFECT\\t\\t\\tBtu/hr\\t\\tEvaopration, lb/hr\\n\"\n",
-    "hi=10500*930*0.974;#Btu/hr\n",
-    "hl=18230*(246-150)*0.83;#Btu/hr\n",
-    "rh=hi-hl;#Btu/hr\n",
-    "hc=300000;#Btu/hr\n",
-    "hv=rh-hc;#Btu/hr\n",
-    "evv=hv/997;#lb/hr\n",
-    "print\"\\t1.a.Heat in steam\\t\\thi\\n\\t  b.Heating liquor\\t\\thl\\n\\t  c.Resultant heat\\t\\trhf\\n\\t  d.Heat of concentrate\\t\\thc\\n\\t  e.Heat of vapors\\t\\thv\\t%.0f\\n\",hi,hl,rh,hc,hv,evv\n",
-    "s1=1.35;\n",
-    "G1=V*s1*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\n\\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\\n\",G1\n",
-    "UD1=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Using thermal characteristics for this solution\n",
-    "print\"\\tUD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD1\n",
-    "#As for effect I:\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t146\\t2400000\\t\\t25.4\\t700\\t620\\t0.80\\t\\t2790000\\t\\t700\\n\\t146.5\\t2160000\\t\\t25.2\\t700\\t683\\t0.89\\t\\t2430000\\n\"\n",
-    "#end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.7 pgno:447"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.7\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tM1 =  lb\n",
-      "17900\n",
-      "\n",
-      "\t\t\t\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tEffects\t\t\t\t\tStraight triple effect\t\t\t\tThermocompression\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tSteam  flow, lb/hr\t\t22400\t\t\t\t\t\t17900\n",
-      "\tSteam pressure, psi in.Hg\t20\t\t9\t\t2\t\t20\t\t9\t\t2\n",
-      "\tSteam temp,degreeF\t\t\t258\t\t237\t\t217\t\t258\t\t237\t\t217\n",
-      "\ttdelT,degreeF\t\t\t20\t\t18\t\t22\t\t20\t\t18\t\t22\n",
-      "\tLiquor temp, degreeF\t\t\t238\t\t219\t\t195\t\t238\t\t219\t\t195\n",
-      "\tBPR, degreeF\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\tVapor temp, degreeF\t\t\t237\t\t217\t\t192\t\t237\t\t215\t\t192\n",
-      "\tVapor pressure, pis/in.Hg\t9\t\t2\t\t10\t\t9\t\t2\t\t10\n",
-      "\tLambda, Btu/lb\t\t\t954\t\t965\t\t983\t\t954\t\t965\t\t983\n",
-      "\tLiquor in, lb/hr\t\t100000\t\t79400\t\t56900\t\t109000\t\t70000\t\t52400\n",
-      "\tLiqour out, lb/hr\t\t79400\t\t56900\t\t33300\t\t70000\t\t52400\t\t33300\n",
-      "\tEvaporation,lb/hr\t\t20600\t\t22500\t\t23500\t\t30000\t\t17600\t\t19100\n",
-      "\tdegreeBrix(out)\t\t\t\t\t\t\t\t\t\t\t\t\t30\n",
-      "\tCondenser water, gpm\t\t\t\t455\t\t\t\t\t\t365\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\n",
-      "\t\t\t\tCondenser water = 455 gpm\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\t1.a.Heat in steam\t\n",
-      "\t20424320.0\n",
-      "b.Heating liquor\t\n",
-      "\t736000.0\n",
-      "c.Evaporation\t\t Evaporation/954\t\n",
-      "\t19688320.0 20637.6519916\n",
-      "d.Liquor to 2d =  79362.3480084\n",
-      "total evapouriation 66700\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.7\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "M2=14300;#From fig.14.43 and heat balance above\n",
-    "M1=32200-14300;#From fig.14.43 and heat balance above\n",
-    "print\"\\tM1 =  lb\\n\",M1\n",
-    "print\"\\n\\t\\t\\t\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tEffects\\t\\t\\t\\t\\tStraight triple effect\\t\\t\\t\\tThermocompression\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tSteam  flow, lb/hr\\t\\t22400\\t\\t\\t\\t\\t\\t17900\\n\\tSteam pressure, psi in.Hg\\t20\\t\\t9\\t\\t2\\t\\t20\\t\\t9\\t\\t2\\n\\tSteam temp,degreeF\\t\\t\\t258\\t\\t237\\t\\t217\\t\\t258\\t\\t237\\t\\t217\\n\\ttdelT,degreeF\\t\\t\\t20\\t\\t18\\t\\t22\\t\\t20\\t\\t18\\t\\t22\\n\\tLiquor temp, degreeF\\t\\t\\t238\\t\\t219\\t\\t195\\t\\t238\\t\\t219\\t\\t195\\n\\tBPR, degreeF\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\\tVapor temp, degreeF\\t\\t\\t237\\t\\t217\\t\\t192\\t\\t237\\t\\t215\\t\\t192\\n\\tVapor pressure, pis/in.Hg\\t9\\t\\t2\\t\\t10\\t\\t9\\t\\t2\\t\\t10\\n\\tLambda, Btu/lb\\t\\t\\t954\\t\\t965\\t\\t983\\t\\t954\\t\\t965\\t\\t983\\n\\tLiquor in, lb/hr\\t\\t100000\\t\\t79400\\t\\t56900\\t\\t109000\\t\\t70000\\t\\t52400\\n\\tLiqour out, lb/hr\\t\\t79400\\t\\t56900\\t\\t33300\\t\\t70000\\t\\t52400\\t\\t33300\\n\\tEvaporation,lb/hr\\t\\t20600\\t\\t22500\\t\\t23500\\t\\t30000\\t\\t17600\\t\\t19100\\n\\tdegreeBrix(out)\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t30\\n\\tCondenser water, gpm\\t\\t\\t\\t455\\t\\t\\t\\t\\t\\t365\\n\"\n",
-    "print\"\\n\\t\\t\\t\\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\\n\\t\\t\\t\\tCondenser water = 455 gpm\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "sf=22400;#lb/hr\n",
-    "lc=100000;#lb/hr\n",
-    "t1=238;#degreeF\n",
-    "t2=230;#degreeF\n",
-    "te=30000+17600+19100;\n",
-    "his=sf*940*0.97;#Btu/hr\n",
-    "hlq=lc*(t1-t2)*0.92;#Btu/hr\n",
-    "hd=his-hlq;#Btu/hr\n",
-    "eva=(hd)/954;#lb/hr\n",
-    "l2d=lc-eva;\n",
-    "print\"\\t1.a.Heat in steam\\t\\n\\t\" ,his \n",
-    "print\"b.Heating liquor\\t\\n\\t\",hlq\n",
-    "print\"c.Evaporation\\t\\t Evaporation/954\\t\\n\\t\",hd,eva  \n",
-    "print\"d.Liquor to 2d = \",l2d\n",
-    "print\"total evapouriation\",te\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_1.ipynb
deleted file mode 100755
index 6c6ad595..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_1.ipynb
+++ /dev/null
@@ -1,1114 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 14 : Evapouration"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.1 pgno:383"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tQevap is  Btu/hr\t9610000\n",
-      "\tQ300 degreeF is  Btu/hr\t9600500\n",
-      "\tTemperature head =  degree F\t74\n",
-      "\tOverall coefficient \t605.5\n",
-      "\tSurface required is  ft^2\t2144.75416788\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "t1 = 300; # degreeF\n",
-    "t2 = 226; #degree F\n",
-    "bs = 700; # Btu/((hr)(ft^2)(ddegree F))\n",
-    "#Heat Balance\n",
-    "Qv = 10000 * 961; # Btu/hr\n",
-    "print\"\\tQevap is  Btu/hr\\t\",Qv\n",
-    "Q3 = 10550 * 910; #Btu/hr\n",
-    "print\"\\tQ300 degreeF is  Btu/hr\\t\",Q3\n",
-    "\n",
-    "delT = t1-t2; # degree F\n",
-    "print\"\\tTemperature head =  degree F\\t\",delT\n",
-    "Ud = bs * 0.865;\n",
-    "print\"\\tOverall coefficient \\t\",Ud\n",
-    "A = Qv*10/(Ud * delT); #ft^2\n",
-    "print\"\\tSurface required is  ft^2\\t\",A#Wrong calculation in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.2 pgno:412"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tTotal product is lb/hr\t10000.0\n",
-      "\tTotal evaporation is lb/hr\t40000.0\n",
-      "\tTotal temperature difference is del degree F\t119\n",
-      "\tAverage pressure difference is del psi/effect \t8.25\n",
-      "\t\t\t\t\t\tPressure, psia\t\t delP, psi \t Steam or vapor, degree F \t lambda, Btu/lb\t\tSteam chest, 1st effect \t 26.70 \t\t\t .... \t\t Ts = 244 \t\t ls = 949 \t\tSteam chest, 2nd effect \t 18.45 \t\t\t 8.25 \t\t t1 = 224 \t\t l1 = 961 \t\tSteam chest, 3rd effect \t 10.20(20.7 in. Hg) \t 8.25 \t\t t2 = 194 \t\t l1 = 981 \t\tVapor to condenser \t\t 1.95(26 in. Hg) \t 8.25 \t\t t2 = 125 \t\t l1 = 1022 \t\n",
-      "\t949*Ws + 50000*(100-224) = 961*w1\t\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\t\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\t\tw1+w2+w3 = 40000\t\n",
-      "\tSolving simultaneously\t\n",
-      "\tw1 = \t12400\n",
-      "\tw2 = \t13300\n",
-      "\tw3 = \t14300\n",
-      "\tW1-3 is \t40000\n",
-      "\tA1 is ft**2 \t1510\n",
-      "\tA2 is ft**2 \t1588\n",
-      "\tA3 is ft**2 \t1512\n",
-      "\tHeat to condenser is Btu/hr\t14614600\n",
-      "\tWater requirement is lb/hr\t417560\n",
-      "\t= gpm \t835\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "wf = 50000; #  lb/hr\n",
-    "sf = wf * 0.10; #  lb/hr\n",
-    "tp = sf/0.50; # lb/hr\n",
-    "print\"\\tTotal product is lb/hr\\t\",tp\n",
-    "te = wf - tp;\n",
-    "print\"\\tTotal evaporation is lb/hr\\t\",te\n",
-    "cf = 1.0;\n",
-    "tF = 100;  # degree F\n",
-    "T1 = 244; # degree F\n",
-    "T2 = 125; # degree F\n",
-    "U1=600; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U2=250; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U3=125; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "\n",
-    "T = T1-T2;\n",
-    "print\"\\tTotal temperature difference is del degree F\\t\",T\n",
-    "df = (26.70- 1.95)/3; # psi/effect\n",
-    "print\"\\tAverage pressure difference is del psi/effect \\t\",df\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\tPressure, psia\\t\\t delP, psi \\t Steam or vapor, degree F \\t lambda, Btu/lb\\t\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\t .... \\t\\t Ts = 244 \\t\\t ls = 949 \\t\\tSteam chest, 2nd effect \\t 18.45 \\t\\t\\t 8.25 \\t\\t t1 = 224 \\t\\t l1 = 961 \\t\\tSteam chest, 3rd effect \\t 10.20(20.7 in. Hg) \\t 8.25 \\t\\t t2 = 194 \\t\\t l1 = 981 \\t\\tVapor to condenser \\t\\t 1.95(26 in. Hg) \\t 8.25 \\t\\t t2 = 125 \\t\\t l1 = 1022 \\t\"\n",
-    "\n",
-    "print\"\\t949*Ws + 50000*(100-224) = 961*w1\\t\\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\\t\\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\\t\\tw1+w2+w3 = 40000\\t\"\n",
-    "print\"\\tSolving simultaneously\\t\"\n",
-    "w1=12400;\n",
-    "print\"\\tw1 = \\t\",w1\n",
-    "w2=13300;\n",
-    "print\"\\tw2 = \\t\",w2\n",
-    "w3=14300;\n",
-    "print\"\\tw3 = \\t\",w3\n",
-    "\n",
-    "Wt = w1+w2+w3;\n",
-    "print\"\\tW1-3 is \\t\",Wt\n",
-    "Ws = 19100;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "Ts = 244;\n",
-    "t1 = 224;\n",
-    "t2 = 194;\n",
-    "t3 = 125;\n",
-    "\n",
-    "A1 = (Ws * lms)/(U1*(Ts-t1)); #ft**2\n",
-    "print\"\\tA1 is ft**2 \\t\",A1\n",
-    "A2 = (w1*lm1)/(U2*(t1-t2)); #ft**2\n",
-    "print\"\\tA2 is ft**2 \\t\",A2\n",
-    "A3 = (w2 * lm2)/(U3*(t2-t3)); #ft**2\n",
-    "print\"\\tA3 is ft**2 \\t\",A3\n",
-    "\n",
-    "hc = w3 * lm3; # Btu/hr, WRONG CALCULATION IN TEXT BOOK\n",
-    "print\"\\tHeat to condenser is Btu/hr\\t\",hc\n",
-    "wr = hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement is lb/hr\\t\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t= gpm \\t\",wr1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.3 pgno:414"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t981*w2 + 50000*(100-125) = 1022*w3\n",
-      "\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\n",
-      "\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\n",
-      "\tw1+w2+w3 = 40000\n",
-      "\n",
-      "\tSolving simultaneously\n",
-      "\n",
-      "\tw1-3 =  \n",
-      "40000\n",
-      "\tA1 is  ft**2\n",
-      "2010\n",
-      "\tA2 is  ft**2\n",
-      "2043\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tAverage surface is  ft**2\n",
-      "1700\n",
-      "\n",
-      "\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\n",
-      "5100\n",
-      "\tRecalculation\n",
-      "\n",
-      "\tA1 is  ft**2\n",
-      "0\n",
-      "\tA2 is  ft**2\n",
-      "0\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tTs-t3 is  degreeF\n",
-      "119\n",
-      "\t\t\t\t\tPressure, psia\t\t Steam or vapor, degreeF \t lambda, Btu/lb\n",
-      "\tSteam chest, 1st effect \t 26.70 \t\t\tTs = 244 \t\t 949 \n",
-      "\tSteam chest, 2nd effect \t 16.0 \t\t\t t1 = 216 \t\t 968 \n",
-      "\tSteam chest, 3rd effect \t 16.4 in. Hg) \t\t t2 = 175 \t\t 992 \n",
-      "\tVapor to condenser \t\t 26 in. Hg \t\t t3 = 125 \t\t l1 = 1022 \n",
-      "\n",
-      "\tw1 is \n",
-      "15450\n",
-      "\tw2 is \n",
-      "13200\n",
-      "\tw3 is \n",
-      "11350\n",
-      "\tWs is \n",
-      "16850\n",
-      "\tHeat to condenser is  Btu/hr\n",
-      "11599700\n",
-      "\tWater requirement  lb/hr\n",
-      "331420\n",
-      "\t\t\t= gpm\n",
-      "662\n",
-      "\tEconomy, lb evaporation/lb steam \n",
-      "2\n",
-      "\t\t\t\tForward\t\tBackward\n",
-      "\tTotal steam, lb/hr\t19100\t\t16850\n",
-      "\tCooling water, gpm\t840\t\t664\n",
-      "\tTotal surface, ft**2\t4800\t\t4500\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Same conditions as example 14.2\n",
-    "U1 = 400; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U2 = 250; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U3 = 175; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "\n",
-    "w1 = 50000; # lb/hr     From example 14.2\n",
-    "wt = 40000; # lb/hr     From example 14.2\n",
-    "cf = 1; # From example 14.2\n",
-    "\n",
-    "print\"\\t981*w2 + 50000*(100-125) = 1022*w3\\n\\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\\n\\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\\n\\tw1+w2+w3 = 40000\\n\"\n",
-    "print\"\\tSolving simultaneously\\n\"\n",
-    "w1 = 15950;\n",
-    "w2 = 12900;\n",
-    "w3 = 11150;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "\n",
-    "wt = w1+w2+w3;\n",
-    "print\"\\tw1-3 =  \\n\",wt\n",
-    "Ws = 16950;\n",
-    "A1 = (Ws*lms)/(U1*20); #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A1\n",
-    "A2 = (w1*lm1)/(U2*30); #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A2\n",
-    "A3 = (w2*lm2)/(U3*69); #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A3\n",
-    "\n",
-    "Avs = (A1 + A2 + A3)/3; #ft**2\n",
-    "print\"\\tAverage surface is  ft**2\\n\",Avs\n",
-    "Av1 = 3 * Avs; #ft**2\n",
-    "print\"\\n\\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\\n\",Av1\n",
-    "print\"\\tRecalculation\\n\"\n",
-    "Av2 = 1500; #ft**2, assume\n",
-    "dT1 = 28; #degreeF\n",
-    "A4 = (20/dT1)*A1; #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A4\n",
-    "dT2 = 41; #degreeF\n",
-    "A5  = (30/dT2)*A2; #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A5\n",
-    "dT3 = 50; #degreeF\n",
-    "A6 = (69/50)*A3; #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A6\n",
-    "del1 = 119; #degreeF\n",
-    "print\"\\tTs-t3 is  degreeF\\n\",del1\n",
-    "print\"\\t\\t\\t\\t\\tPressure, psia\\t\\t Steam or vapor, degreeF \\t lambda, Btu/lb\\n\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\tTs = 244 \\t\\t 949 \\n\\tSteam chest, 2nd effect \\t 16.0 \\t\\t\\t t1 = 216 \\t\\t 968 \\n\\tSteam chest, 3rd effect \\t 16.4 in. Hg) \\t\\t t2 = 175 \\t\\t 992 \\n\\tVapor to condenser \\t\\t 26 in. Hg \\t\\t t3 = 125 \\t\\t l1 = 1022 \\n\"\n",
-    "\n",
-    "w1 = 15450; #Solving again for \n",
-    "print\"\\tw1 is \\n\",w1\n",
-    "w2 = 13200;\n",
-    "print\"\\tw2 is \\n\",w2\n",
-    "w3 = 11350;\n",
-    "print\"\\tw3 is \\n\",w3\n",
-    "Ws = 16850;\n",
-    "print\"\\tWs is \\n\",Ws\n",
-    "Hc = w3 * 1022;\n",
-    "print\"\\tHeat to condenser is  Btu/hr\\n\",Hc\n",
-    "wr = Hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement  lb/hr\\n\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t\\t\\t= gpm\\n\",wr1\n",
-    "ec = wt/Ws;\n",
-    "print\"\\tEconomy, lb evaporation/lb steam \\n\",ec\n",
-    "\n",
-    "#comparision of forward and backward feed\n",
-    "print\"\\t\\t\\t\\tForward\\t\\tBackward\\n\\tTotal steam, lb/hr\\t19100\\t\\t16850\\n\\tCooling water, gpm\\t840\\t\\t664\\n\\tTotal surface, ft**2\\t4800\\t\\t4500\"\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.4 pgno:418"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.4 \n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\n",
-      "\n",
-      "\tEffects\t\tWater evaporated(lb/(hr)*(ft**2))\n",
-      "\n",
-      "\t1\t\t14-16\n",
-      "\t2\t\t6-8\n",
-      "\t3\t\t5-6\n",
-      "\t4\t\t4-5\n",
-      "\t5\t\t3-4\n",
-      "\n",
-      "\n",
-      "\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam  flow, lb/hr\t\t42600\t\t38000\n",
-      "\t2.Steam pressure, psi/in.Hg\t30\t\t30\t\t15\t\t5\t\t4\t\t14.5\n",
-      "\n",
-      "\t3.Steam temp,degreeF\t\t\t274\t\t274\t\t250\t\t227\t\t205\t\t181\n",
-      "\n",
-      "\t4.delT,degreeF\t\t\t23\t\t23\t\t21\t\t20\t\t20\t\t27\n",
-      "\t5.Liquor temp, degreeF\t\t251\t\t251\t\t229\t\t207\t\t185\t\t164\n",
-      "\t6.BPR, degreeF\t\t\t1\t\t1\t\t2\t\t2\t\t4\t\t7\n",
-      "\t7.Vapor temp, degreeF\t\t250\t\t250\t\t227\t\t205\t\t181\t\t147\n",
-      "\t8.Vapor pressure, pis/in.Hg\t15\t\t15\t\t5\t\t4\t\t14.5\t\t23\n",
-      "\t9.Lambda, Btu/lb\t\t946\t\t946\t\t960\t\t975\t\t990\t\t1010\n",
-      "\t10.Liquor in, lb/hr\t\t229000\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\n",
-      "\t11.Liqour out, lb/hr\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\t\t49600\n",
-      "\t12.Evaporation,lb/hr\t\t38800\t\t36200\t\t36900\t\t29300\t\t23800\t\t14400\n",
-      "\t13.degreeBrix(out)\t\t\t15.7\t\t19.4\t\t25.5\t\t34.4\t\t46.5\t\t50.0\n",
-      "\t14.A,ft**2\t\t\t3500\t\t3500\t\t5000\t\t5000\t\t5000\t\t3500\n",
-      "\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\t478\t\t425\t\t310\t\t264\t\t219\t\t138\n",
-      "\t16.UD delT,Btu/(hr)*(ft**2)\t11000\t\t9780\t\t6520\t\t5270\t\t4390\t\t3740\n",
-      "\n",
-      "\tTotal temperature difference in the evaporator system =  degreeF\n",
-      "127\n",
-      "\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\n",
-      "16\n",
-      "\tTotal EFFECTIVE  temperature difference = degreeF\n",
-      "111\n",
-      "\n",
-      "\t\t\t\tSUGAR-JUICE HEATERS\n",
-      "\n",
-      "\tRaw-juice heaters\t\t\t\tClear=juice heaters\n",
-      "\t-----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr 229000 212 184 5834920.0\n",
-      "\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\n",
-      "229000 243 220 4792970.0\n",
-      "\tVapor temp. = 227degreeF\tdelT=26.6degreeF\t\tVapor temp. = 250degreeF\tdelT=15.8degreeF\n",
-      "\n",
-      "\tud1=.\t\t\t\t\t\tUD=ud2\n",
-      "231 243\n",
-      "\tSurface,A=A1 ft**2\t\t\t\tSurface,A=A2 ft**2\n",
-      "\n",
-      "949.601275917 1248.36432776\n",
-      "\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr 229000 184 144 8244000.0\n",
-      "\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\n",
-      "229000 220 200 4122000.0\n",
-      "\tVapor temp. = 205degreeF\tdelT=37.6degreeF\t\tVapor temp. = 227degreeF\tdelT=14.8degreeF\n",
-      "\n",
-      "\tUD=Ud3\t\t\t\t\t\tUD=Ud4\n",
-      "230 214\n",
-      "\tSurface,A=A3 ft**2\t\t\t\tSurface,A=A4 ft**2\n",
-      "\n",
-      "953.2839963 1301.46501642\n",
-      "\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr 229000 144 82 4122000.0\n",
-      "\t(Use 2 heaters at 1300 ft**2 each plus 1\n",
-      "\t\t\t\t\t\t\theater at 1300 ft**2 as spare)\n",
-      "\n",
-      "\tVapor temp. = 181degreeF\tdelT=62.2degreeF\n",
-      "\tSurface,A=\n",
-      "946.715663757\n",
-      "\t(Use 3 heaters at 100 ft**2\n",
-      "\teach plus 1 heater as spare)\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t----------------------------------------------------\n",
-      "\n",
-      "\t1A.Heat in steam........\n",
-      "38388138.0\n",
-      "\t   Heating liquor.......\n",
-      "\t\t\t\t%.3e\t.\n",
-      "1667120.0 36721018.0 38817.1437632\n",
-      "\t   Liqour to 1B\n",
-      "\t   =  lb/hr\n",
-      "190182.856237\n",
-      "\t1B.Heat in steam........\n",
-      "34979292.7593\n",
-      "\t   Heating liquor........\n",
-      "\t\t\t\t\n",
-      "0.0 34979292.7593 36975.9965744\n",
-      "\t   Liqour to 2d \n",
-      "\t   effect= lb/hr\n",
-      "153206.859662\n",
-      "\t\t\t\t\t\t\t\tLb/hr\n",
-      "\n",
-      "\t(a) Actual evaporation..................................\n",
-      "179400\n",
-      "\t(b) Equivalent evaporation from vapors of \n",
-      "\t    1st effect used for vaccum pans......................\n",
-      "145500\n",
-      "\t(c) Equivalent evaporation from 1st effect \n",
-      "\t    vapors used for clarified-juice heaters..............\n",
-      "19700\n",
-      "\t(d) Equivalent evaporation from 2d effect \n",
-      "\t    vapors used for clarified-and raw-juice heaters......\n",
-      "30600\n",
-      "\t(e) Equivalent evaporation from 3d effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "2.71828182846\n",
-      "\t(f) Equivalent evaporation from 4th effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "13100\n",
-      "\t                                                        -----\n",
-      "\n",
-      "\t     Extrapolated evaporation............................\n",
-      "406200\n",
-      "\t\tEstimated steam quantity =  lb/hr\n",
-      "81240\n",
-      "\t\tActual steam required from final heat balance =  lb/hr\n",
-      "80600\n",
-      "\t\t\t\t\t\t\tError =  lb/hr\n",
-      "640\n",
-      "\tGallons per minute of Water required =  gpm 583\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.4 \\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "from math import e\n",
-    "#Assumed that 37500 lb/hr of 15 psig vapor is bled from the first effect for use in thevaccum pans\n",
-    "print\"\\n\\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\\n\"\n",
-    "print\"\\tEffects\\t\\tWater evaporated(lb/(hr)*(ft**2))\\n\"\n",
-    "print\"\\t1\\t\\t14-16\\n\\t2\\t\\t6-8\\n\\t3\\t\\t5-6\\n\\t4\\t\\t4-5\\n\\t5\\t\\t3-4\\n\"\n",
-    "print\"\\n\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t42600\\t\\t38000\\n\\t2.Steam pressure, psi/in.Hg\\t30\\t\\t30\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\n\"\n",
-    "print\"\\t3.Steam temp,degreeF\\t\\t\\t274\\t\\t274\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\n\"\n",
-    "print\"\\t4.delT,degreeF\\t\\t\\t23\\t\\t23\\t\\t21\\t\\t20\\t\\t20\\t\\t27\\n\\t5.Liquor temp, degreeF\\t\\t251\\t\\t251\\t\\t229\\t\\t207\\t\\t185\\t\\t164\\n\\t6.BPR, degreeF\\t\\t\\t1\\t\\t1\\t\\t2\\t\\t2\\t\\t4\\t\\t7\\n\\t7.Vapor temp, degreeF\\t\\t250\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\t\\t147\\n\\t8.Vapor pressure, pis/in.Hg\\t15\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\t\\t23\\n\\t9.Lambda, Btu/lb\\t\\t946\\t\\t946\\t\\t960\\t\\t975\\t\\t990\\t\\t1010\\n\\t10.Liquor in, lb/hr\\t\\t229000\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\n\\t11.Liqour out, lb/hr\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\t\\t49600\\n\\t12.Evaporation,lb/hr\\t\\t38800\\t\\t36200\\t\\t36900\\t\\t29300\\t\\t23800\\t\\t14400\\n\\t13.degreeBrix(out)\\t\\t\\t15.7\\t\\t19.4\\t\\t25.5\\t\\t34.4\\t\\t46.5\\t\\t50.0\\n\\t14.A,ft**2\\t\\t\\t3500\\t\\t3500\\t\\t5000\\t\\t5000\\t\\t5000\\t\\t3500\\n\\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\\t478\\t\\t425\\t\\t310\\t\\t264\\t\\t219\\t\\t138\\n\\t16.UD delT,Btu/(hr)*(ft**2)\\t11000\\t\\t9780\\t\\t6520\\t\\t5270\\t\\t4390\\t\\t3740\\n\"#BPR values from fig 14.34a\n",
-    "#Saturate vapor pressure above the liquour determined from Table 7\n",
-    "#Saturated steam pressure in the following effect determined from Table 7\n",
-    "\n",
-    "t1 = 274; #degreeF\n",
-    "t2 = 147; #degreeF\n",
-    "t = t1-t2; #degreeF\n",
-    "print\"\\tTotal temperature difference in the evaporator system =  degreeF\\n\",t\n",
-    "bpr1 = 1; #degreeF\n",
-    "bpr2 = 2; #degreeF\n",
-    "bpr3 = 2; #degreeF\n",
-    "bpr4 = 4; #degreeF\n",
-    "bpr5 = 7; #degreeF\n",
-    "bpr = bpr1 + bpr2 + bpr3 + bpr4 + bpr5; #degreeF\n",
-    "print\"\\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\\n\",bpr\n",
-    "tf = t-bpr; #degreeF\n",
-    "print\"\\tTotal EFFECTIVE  temperature difference = degreeF\\n\",tf\n",
-    "lbh = 229000; #lb/hr\n",
-    "tp1=212; #degreeF\n",
-    "tp2=184; #degreeF\n",
-    "tp3=144; #degreeF\n",
-    "tp4=82; #degreeF\n",
-    "tj1=243; #degreeF\n",
-    "tj2=220; #degreeF\n",
-    "tj3=200; #degreeF\n",
-    "Ud1=231;\n",
-    "Ud2=243;\n",
-    "Ud3=230;\n",
-    "Ud4=214;\n",
-    "Ud5=217;\n",
-    "print\"\\n\\t\\t\\t\\tSUGAR-JUICE HEATERS\\n\"\n",
-    "print\"\\tRaw-juice heaters\\t\\t\\t\\tClear=juice heaters\\n\\t-----------------------------------------------------------------------------------------\\n\"\n",
-    "rj1=lbh*(tp1-tp2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr\",lbh,tp1,tp2,rj1\n",
-    "rj2=lbh*(tj1-tj2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\\n\",lbh,tj1,tj2,rj2\n",
-    "print\"\\tVapor temp. = 227degreeF\\tdelT=26.6degreeF\\t\\tVapor temp. = 250degreeF\\tdelT=15.8degreeF\\n\"\n",
-    "print\"\\tud1=.\\t\\t\\t\\t\\t\\tUD=ud2\\n\",Ud1,Ud2\n",
-    "A1=rj1/(26.6*Ud1);#ft**2\n",
-    "A2=rj2/(15.8*Ud2);#ft**2\n",
-    "print\"\\tSurface,A=A1 ft**2\\t\\t\\t\\tSurface,A=A2 ft**2\\n\\n\",A1,A2\n",
-    "\n",
-    "rj3=lbh*(tp2-tp3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr\",lbh,tp2,tp3,rj3\n",
-    "rj4=lbh*(tj2-tj3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\\n\",lbh,tj2,tj3,rj4\n",
-    "print\"\\tVapor temp. = 205degreeF\\tdelT=37.6degreeF\\t\\tVapor temp. = 227degreeF\\tdelT=14.8degreeF\\n\"\n",
-    "print\"\\tUD=Ud3\\t\\t\\t\\t\\t\\tUD=Ud4\\n\",Ud3,Ud4\n",
-    "A3=rj3/(37.6*Ud3);#ft**2\n",
-    "A4=rj4/(14.8*Ud4);#ft**2\n",
-    "print\"\\tSurface,A=A3 ft**2\\t\\t\\t\\tSurface,A=A4 ft**2\\n\\n\",A3,A4\n",
-    "\n",
-    "rj5=lbh*(tp3-tp4)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr\",lbh,tp3,tp4,rj4\n",
-    "print\"\\t(Use 2 heaters at 1300 ft**2 each plus 1\\n\\t\\t\\t\\t\\t\\t\\theater at 1300 ft**2 as spare)\\n\"\n",
-    "A5=rj5/(62.2*Ud5);#ft**2\n",
-    "print\"\\tVapor temp. = 181degreeF\\tdelT=62.2degreeF\\n\\tSurface,A=\\n\",A5\n",
-    "print\"\\t(Use 3 heaters at 100 ft**2\\n\\teach plus 1 heater as spare)\\n\\n\"\n",
-    "\n",
-    "v1=42600;#lb/hr\n",
-    "tt1=251;#degreeF\n",
-    "print\"\\t\\t\\t\\tHEAT BALANCE\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t----------------------------------------------------\\n\"\n",
-    "hia=v1*929*0.97;#Btu/hr\n",
-    "print\"\\t1A.Heat in steam........\\n\",hia\n",
-    "hla=lbh*(tt1-tj1)*0.91;#Btu/hr\n",
-    "hh=hia-hla;#Btu/hr\n",
-    "lb1=946;#Btu/lb\n",
-    "dif=hh/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor.......\\n\\t\\t\\t\\t%.3e\\t.\\n\",hla,hh,dif\n",
-    "ltob=lbh-dif;#lb/hr\n",
-    "print\"\\t   Liqour to 1B\\n\\t   =  lb/hr\\n\",ltob\n",
-    "hia1=dif*929*0.97;#Btu/hr\n",
-    "print\"\\t1B.Heat in steam........\\n\",hia1\n",
-    "hla1=ltob*(tt1-tt1)*0.91;#Btu/hr\n",
-    "hh1=hia1;#Btu/hr\n",
-    "dif1=hh1/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor........\\n\\t\\t\\t\\t\\n\",hla1,hh1,dif1\n",
-    "dif2=ltob-dif1;#lb/hr\n",
-    "print\"\\t   Liqour to 2d \\n\\t   effect= lb/hr\\n\",dif2\n",
-    "#Similarily the values in the table are calculated\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\tLb/hr\\n\"\n",
-    "aa=179400;#lb/hr\n",
-    "bb=145500;#lb/hr\n",
-    "cc=19700;#lb/hr\n",
-    "dd=30600;#lb/hr\n",
-    "ee=17900;#lb/hr\n",
-    "ff=13100;#lb/hr\n",
-    "tto=aa+bb+cc+dd+ee+ff;#lb/hr\n",
-    "print\"\\t(a) Actual evaporation..................................\\n\",aa\n",
-    "print\"\\t(b) Equivalent evaporation from vapors of \\n\\t    1st effect used for vaccum pans......................\\n\",bb\n",
-    "print\"\\t(c) Equivalent evaporation from 1st effect \\n\\t    vapors used for clarified-juice heaters..............\\n\",cc\n",
-    "print\"\\t(d) Equivalent evaporation from 2d effect \\n\\t    vapors used for clarified-and raw-juice heaters......\\n\",dd\n",
-    "print\"\\t(e) Equivalent evaporation from 3d effect \\n\\t    vapors used for raw-juice heaters....................\\n\",e\n",
-    "print\"\\t(f) Equivalent evaporation from 4th effect \\n\\t    vapors used for raw-juice heaters....................\\n\",ff\n",
-    "print\"\\t                                                        -----\\n\"\n",
-    "print\"\\t     Extrapolated evaporation............................\\n\",tto\n",
-    "esq=tto/5;#lb/hr\n",
-    "print\"\\t\\tEstimated steam quantity =  lb/hr\\n\",esq\n",
-    "aesq=80600;#lb/hr\n",
-    "err = esq-aesq;#lb/hr\n",
-    "print\"\\t\\tActual steam required from final heat balance =  lb/hr\\n\",aesq\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\tError =  lb/hr\\n\",err\n",
-    "ta=15;\n",
-    "Q=14575000; #Btu/hr Total hourly evaporation\n",
-    "Gpm=Q/(500*(t2-tp4-ta));#From equation 14.4\n",
-    "print\"\\tGallons per minute of Water required =  gpm\",Gpm\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.5 pgno:427"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 9,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.5\t\n",
-      "\tapproximate values are mentioned in the book \t\n",
-      "\tOverall temperature difference =  deg F\t155\n",
-      "\tThe estimated total BPR =  degF\t[10 18 25 31 36 41]\n",
-      "\tEffective temperature difference = %.0f degF\t[145 137 130 124 119 114]\n",
-      "\t\t\t\t\tEVAPORATOR SUMMARY\t\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\t\t\t\t\t\t----------------------------------------------------------------------------------------------\t\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\t1.Steam  flow, lb/hr\t\t20000\t\t2.Steam pressure, psi/in.Hg\t35\t\t14.5\t\t4\t\t7\t\t16.5\t\t22\t\t3.Steam temp,degF\t\t\t280\t\t249\t\t224\t\t199\t\t174\t\t151\t\t4.delT,degF\t\t\t21\t\t17\t\t18\t\t19\t\t18\t\t21\t\t5.Liquor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t6.BPR, degF\t\t\t10\t\t8\t\t7\t\t6\t\t5\t\t5\t\t7.Vapor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t8.Vapor pressure, pis/in.Hg\t14.5\t\t4\t\t7\t\t6\t\t5\t\t5\t\t9.Lambda, Btu/lb\t\t946\t\t962\t\t978\t\t994\t\t1008\t\t1022\t\t10.Liquor in, lb/hr\t\t73400\t\t88300\t\t101000\t\t113000\t\t72000\t\t72000\t\t11.Liqour out, lb/hr\t\t56200\t\t73400\t\t88300\t\t101100\t\t58300\t\t54700\t\t12.Evaporation,lb/hr\t\t17200\t\t14900\t\t12800\t\t11900\t\t13700\t\t17300\t\t13.Total solids, \t\t38.9\t\t29.8\t\t24.7\t\t21.6\t\t18.7\t\t20.0\t\t14.A,ft^2\t\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t15.UD,Btu/(hr)*(ft^2)*(degF)\t262\t\t295\t\t252\t\t251\t\t221\t\t221\t\t16.UD delT,Btu/(hr)*(ft^2)\t5510\t\t5000\t\t4530t\t\t4770\t\t3980\t\t4650\t\n",
-      "\t\tTotal amount of water evaporated = \t lb/hr\t[17200 32100 44900 56800 70500     0]\n",
-      "\tTheoretical amount of steam for a six-effect evaporator = \t lb/hr\t[ 2866  5350  7483  9466 11750     0]\n",
-      "\tSteam used for trail balance = \t lb/hr\t[  3822.22222222   7133.33333333   9977.77777778  12622.22222222\n",
-      "  15666.66666667      0.        ]\n",
-      "\tEstimate of the amount of evaporation in the first effect = \t lb/hr\t[  3295.9    6152.5    8605.45  10885.9   13512.5       0.  ]\n",
-      "\tEstimated discharge from second effect = \t lb/hr\t[ 59495.9   62352.5   64805.45  67085.9   69712.5   56200.  ]\n",
-      "\t\t\t\t\tHEAT BALANCE\t\n",
-      "\t\tCooling water at 60 degreeF = \t gpm\t710\n",
-      "\t--------------------------------------------------------\t\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\t\n",
-      "\t--------------------------------------------------------\t\n",
-      "\t1.a.Heat in steam \t\t17925600.0\n",
-      "\t  b.Heating liquor \t\t1625076.0\n",
-      "\t  c.Evaporation\t\t\t\t\t\t17230.9978858\n",
-      "\t  d.To flash tank\t2190591.08245\n",
-      "\t\t\t\t2239.86818247\n",
-      "\t  e.Flashed vapor=\t\t2239.86818247\n",
-      "\t  f.product \t53929.1339317\n",
-      "\t\t2.a.Heat in 1st vapors\t\t16300524.0\n",
-      "\t  b.Heating liqour\t\t1951430.0\n",
-      "\t  c.Evaporation= 14915.8981289\n",
-      "\t\t\t\t\t14915.8981289\n",
-      "\t  d.Liquor to 1b=\t\t73384.1018711\n",
-      "total hourly evapouration lb : 90000\n",
-      "economy is lb/lb : 4.5\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.5\\t\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\t\"\n",
-    "st1=280; #degF\n",
-    "vt6=125; #degF\n",
-    "odT=st1-vt6; #degF\n",
-    "print\"\\tOverall temperature difference =  deg F\\t\",odT #corresponding to 35 psig and 26 in. Hg\n",
-    "import numpy\n",
-    "bpr=numpy.array([10, 8, 7, 6, 5, 5])\n",
-    "#bpr(1)=10; #degF\n",
-    "#bpr(2)=8; #degF\n",
-    "#bpr(3)=7; #degF\n",
-    "#bpr(4)=6; #degF\n",
-    "#bpr(5)=5; #degF\n",
-    "#bpr(6)=5; #degF\n",
-    "i=1;\n",
-    "tbpr=numpy.array([0, 0, 0, 0, 0, 0]);\n",
-    "tbpr[0]=bpr[0];\n",
-    "while (i<6):\n",
-    "\n",
-    "    tbpr[i]=tbpr[i-1]+bpr[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\tThe estimated total BPR =  degF\\t\",tbpr #from fig. 14.36a\n",
-    "edT=odT-tbpr;\n",
-    "print\"\\tEffective temperature difference = %.0f degF\\t\",edT\n",
-    "print\"\\t\\t\\t\\t\\tEVAPORATOR SUMMARY\\t\\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\t\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\t\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t20000\\t\\t2.Steam pressure, psi/in.Hg\\t35\\t\\t14.5\\t\\t4\\t\\t7\\t\\t16.5\\t\\t22\\t\\t3.Steam temp,degF\\t\\t\\t280\\t\\t249\\t\\t224\\t\\t199\\t\\t174\\t\\t151\\t\\t4.delT,degF\\t\\t\\t21\\t\\t17\\t\\t18\\t\\t19\\t\\t18\\t\\t21\\t\\t5.Liquor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t6.BPR, degF\\t\\t\\t10\\t\\t8\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t7.Vapor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t8.Vapor pressure, pis/in.Hg\\t14.5\\t\\t4\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t9.Lambda, Btu/lb\\t\\t946\\t\\t962\\t\\t978\\t\\t994\\t\\t1008\\t\\t1022\\t\\t10.Liquor in, lb/hr\\t\\t73400\\t\\t88300\\t\\t101000\\t\\t113000\\t\\t72000\\t\\t72000\\t\\t11.Liqour out, lb/hr\\t\\t56200\\t\\t73400\\t\\t88300\\t\\t101100\\t\\t58300\\t\\t54700\\t\\t12.Evaporation,lb/hr\\t\\t17200\\t\\t14900\\t\\t12800\\t\\t11900\\t\\t13700\\t\\t17300\\t\\t13.Total solids, \\t\\t38.9\\t\\t29.8\\t\\t24.7\\t\\t21.6\\t\\t18.7\\t\\t20.0\\t\\t14.A,ft^2\\t\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t15.UD,Btu/(hr)*(ft^2)*(degF)\\t262\\t\\t295\\t\\t252\\t\\t251\\t\\t221\\t\\t221\\t\\t16.UD delT,Btu/(hr)*(ft^2)\\t5510\\t\\t5000\\t\\t4530t\\t\\t4770\\t\\t3980\\t\\t4650\\t\"#BPR values from fig 14.36a\n",
-    "#Specific-heat data are given in Fig. 14.36b\n",
-    "ev=numpy.array([17200, 14900, 12800, 11900, 13700, 17300]);\n",
-    "#ev(1)=17200; #lb/hr\n",
-    "#ev(2)=14900; #lb/hr\n",
-    "#ev(3)=12800; #lb/hr\n",
-    "#ev(4)=11900; #lb/hr\n",
-    "#ev(5)=13700; #lb/hr\n",
-    "#ev(6)=17300; #lb/hr\n",
-    "i=1;\n",
-    "tev =numpy.array([0, 0, 0, 0, 0, 0])\n",
-    "tev[0]=ev[0];\n",
-    "while (i<5):\n",
-    "    tev[i]= tev[i-1]+ev[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\tTotal amount of water evaporated = \\t lb/hr\\t\",tev\n",
-    "ttev=tev/6;#lb/hr\n",
-    "print\"\\tTheoretical amount of steam for a six-effect evaporator = \\t lb/hr\\t\",ttev\n",
-    "tev2=tev/(6*0.75); #lb/hr . order of 75 percent of theoretical\n",
-    "print\"\\tSteam used for trail balance = \\t lb/hr\\t\",tev2\n",
-    "lq=(tev/6);\n",
-    "lq=lq+(lq*0.15);\n",
-    "print\"\\tEstimate of the amount of evaporation in the first effect = \\t lb/hr\\t\",lq\n",
-    "lout6=54000;#lb/hr\n",
-    "lq2=lout6+lq+2200;#lb/hr\n",
-    "print\"\\tEstimated discharge from second effect = \\t lb/hr\\t\",lq2\n",
-    "print\"\\t\\t\\t\\t\\tHEAT BALANCE\\t\"\n",
-    "cw = 17750000/(500*(125-15-60)); #gpm, values from table 14.6\n",
-    "print\"\\t\\tCooling water at 60 degreeF = \\t gpm\\t\",cw\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\t\"\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "sf=20000;#lb/hr\n",
-    "lqi=73400;#lb/hr\n",
-    "the=90000;\n",
-    "lqi2=88300\n",
-    "lt1=259;#degreeF\n",
-    "lt2=232;#degreeF\n",
-    "lt3=206;#degreeF\n",
-    "ecn=90000./20000.;\n",
-    "ev=17200;#lb/hr\n",
-    "his=sf*924*0.97;#Btu/hr\n",
-    "print\"\\t1.a.Heat in steam \\t\\t\",his\n",
-    "hl=lqi*(lt1-lt2)*0.82;#Btu/hr\n",
-    "print\"\\t  b.Heating liquor \\t\\t\",hl\n",
-    "hh=his-hl;\n",
-    "ev1=(hh)/946;#lb/hr\n",
-    "print\"\\t  c.Evaporation\\t\\t\\t\\t\\t\\t\",ev1\n",
-    "dif=lqi-ev1;\n",
-    "tft=(dif)*(lt1-209)*0.78;\n",
-    "print\"\\t  d.To flash tank\\t\",tft\n",
-    "ev2=tft/978;#lb/hr\n",
-    "print\"\\t\\t\\t\\t\",ev2\n",
-    "print\"\\t  e.Flashed vapor=\\t\\t\",ev2\n",
-    "p=dif-ev2;\n",
-    "print\"\\t  f.product \\t\",p\n",
-    "print\"\\t\\t2.a.Heat in 1st vapors\\t\\t\",hh\n",
-    "hl2=lqi2*(lt2-lt3)*0.85;\n",
-    "print\"\\t  b.Heating liqour\\t\\t\",hl2\n",
-    "ev3=(hh-hl2)/962;\n",
-    "print\"\\t  c.Evaporation=\",ev3\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\",ev3\n",
-    "lto1=lqi2-ev3;\n",
-    "print\"\\t  d.Liquor to 1b=\\t\\t\",lto1\n",
-    "print\"total hourly evapouration lb :\",the\n",
-    "print\"economy is lb/lb :\",ecn\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.6 pgno:437"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.6\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tTotal temperature difference =  degreeF\n",
-      "159\n",
-      "\tThe effective temperature difference is  degreeF\n",
-      "56\n",
-      "\n",
-      "\t\t\tCAUSTIC EVAPORATOR MATERIAL BALANCE\n",
-      "\n",
-      "\tCell liquour at 120degreeF \t\tWash at 80degreeF\n",
-      "\n",
-      "\t---------------------------------------------\n",
-      "\n",
-      "\t8.75 prcnt NaOH = l1\n",
-      "\t16.6 prcnt NaCl = l2\t\t25 prcnt NaCl = w2\n",
-      "2000 3800 340\n",
-      "\t74.65 prcnt H20 = l3\t\t75 prcnt H20 = w2\n",
-      "17050 1020\n",
-      "\tTotal cell liquor = lq\tTotoal wash = w\n",
-      "22850 1360\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\t\t\t\tNaOH\t\tNaCl\t\tH20,Lb\tTotal,Lb\n",
-      "\t\t\t\tprcnt\tLb\tprcnt\tLb\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\tOverall operation:\n",
-      "\t  Cell liquor.......... 8.75\t2000 3800 17050 22850\n",
-      "\t  Wash................. ....\t....\t25.00\t340 1020 1360\n",
-      "\t  Total in............. ....\t2000 4140 18070 24210\n",
-      "\t  Product.............. 50.00\t2000 110 1890 4000\n",
-      "\t  Removed.............. ....\t....\t....\t\t%.0f\t%.0f\n",
-      "4030 16180 20210\n",
-      "\n",
-      "\t\t\t\t\tCAUSTIC EVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t--------------------\t\tFlash Tank\n",
-      "\t\t\t\t\t\\I\t\tII\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam pressure, psi/in.Hg\t30\n",
-      "\t2.Steam temperature,degreeF\t\t274\t\t169\n",
-      "\t3.delT,degreeF\t\t\t28\t\t28\n",
-      "\t4.Liquor temperature, degreeF\t246\t\t141\t\t192\n",
-      "\t5.BPR, degreeF\t\t\t77\t\t26\t\t77\n",
-      "\t6.Vapor temperature, degreeF\t\t169\t\t115\t\t115\n",
-      "\t7.Lambda, Btu/lb\t\t997\t\t1027\t\t1027\n",
-      "\t8.Feed, lb/hr\t\t\t22788\t\t50602\t\t13367\n",
-      "\t9.Product, lb/hr\t\t13367\t\t40352\t\t12813\n",
-      "\t10.Evaporation,lb/hr\t\t9421\t\t10250\t\t554\n",
-      "\t11.Heat flow, Btu/hr\t\t11890000\t11020000\n",
-      "\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\t700\n",
-      "\t13.A,ft**2\t\t\t683\t\t683\n",
-      "\t14.Tubes, OD, in. and BWG\t1,16\t\t1,16\n",
-      "\t15.Tube length, ft\t\t7\t\t7\n",
-      "\t16.No. tubes\t\t\t432\t\t432\n",
-      "\t17.Circulating pump. gpm\t3200 at 20 ft\t3200 at 20ft\t167 at 45 ft\n",
-      "\t18.Apparent efficiency, prcnt\t54\t\t64\n",
-      "\t18.BHP\t\t\t\t38\t\t35\t\t8.2\n",
-      "\t20.Motor,hp\t\t\t40\t\t40\t\t10.0\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\n",
-      "2700000.0\n",
-      "\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t251\t2970000\t\t25.4\t700\t670\t0.87\t\t3420000\n",
-      "\t252\t2480000\t\t25.0\t700\t680\t0.88\t\t2820000\n",
-      "\t252.5\t2290000\t\t24.7\t700\t685\t0.89\t\t2570000\t\t700\n",
-      "\t253\t2120000\t\t24.5\t700\t695\t0.90\t\t2520000\n",
-      "\n",
-      "\tThee gain per minute is gpm\n",
-      "3200\n",
-      "\n",
-      "\t\t\t\tCAUSTIC EVAPORATION HEAT BALANCE\n",
-      "\n",
-      "\t\t\t\t(Basis = 1ton/hr NaOH)\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t\tEFFECT\t\t\tBtu/hr\t\tEvaopration, lb/hr\n",
-      "\n",
-      "\t1.a.Heat in steam\t\thi\n",
-      "\t  b.Heating liquor\t\thl\n",
-      "\t  c.Resultant heat\t\trhf\n",
-      "\t  d.Heat of concentrate\t\thc\n",
-      "\t  e.Heat of vapors\t\thv\t%.0f\n",
-      "9511110.0 1452566.4 8058543.6 300000 7758543.6 7781.8892678\n",
-      "\n",
-      "\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\n",
-      "2430000.0\n",
-      "\tUD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t146\t2400000\t\t25.4\t700\t620\t0.80\t\t2790000\t\t700\n",
-      "\t146.5\t2160000\t\t25.2\t700\t683\t0.89\t\t2430000\n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.6\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "st1=274; #degreeF\n",
-    "vt6=115; #degreeF\n",
-    "odT=st1-vt6; #degreeF\n",
-    "print\"\\tTotal temperature difference =  degreeF\\n\",odT #corresponding to 35 psig\n",
-    "eb1=77;#degreeF, From fig.14.38\n",
-    "eb2=26;#degreeF, From fig.14.38\n",
-    "etd=odT-(eb1+eb2);#degreeF\n",
-    "print\"\\tThe effective temperature difference is  degreeF\\n\",etd\n",
-    "print\"\\n\\t\\t\\tCAUSTIC EVAPORATOR MATERIAL BALANCE\\n\"\n",
-    "#Basis: 1 ton/hr NaOH\n",
-    "print\"\\tCell liquour at 120degreeF \\t\\tWash at 80degreeF\\n\"\n",
-    "print\"\\t---------------------------------------------\\n\"\n",
-    "l1=2000;#Lb\n",
-    "l2=3800;#Lb\n",
-    "l3=17050;#Lb\n",
-    "lq=l1+l2+l3;#Lb\n",
-    "w1=340;#Lb\n",
-    "w2=1020;#Lb\n",
-    "w=w1+w2;#Lb\n",
-    "print\"\\t8.75 prcnt NaOH = l1\\n\\t16.6 prcnt NaCl = l2\\t\\t25 prcnt NaCl = w2\\n\",l1,l2,w1\n",
-    "print\"\\t74.65 prcnt H20 = l3\\t\\t75 prcnt H20 = w2\\n\",l3,w2\n",
-    "print\"\\tTotal cell liquor = lq\\tTotoal wash = w\\n\",lq,w\n",
-    "print\"\\n\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\t\\t\\tNaOH\\t\\tNaCl\\t\\tH20,Lb\\tTotal,Lb\\n\\t\\t\\t\\tprcnt\\tLb\\tprcnt\\tLb\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tOverall operation:\\n\\t  Cell liquor.......... 8.75\\t\",l1,l2,l3,lq\n",
-    "print\"\\t  Wash................. ....\\t....\\t25.00\\t\",w1,w2,w\n",
-    "wl1=l2+w1;#Lb\n",
-    "wl2=l3+w2;#Lb\n",
-    "wlt=lq+w;\n",
-    "print\"\\t  Total in............. ....\\t\",l1,wl1,wl2,wlt\n",
-    "prn=110;#Lb\n",
-    "prh=1890;#Lb\n",
-    "prt=4000;#Lb\n",
-    "print\"\\t  Product.............. 50.00\\t\",l1,prn,prh,prt\n",
-    "r1=wl1-prn;#Lb\n",
-    "r2=wl2-prh;#Lb\n",
-    "r3=wlt-prt;#Lb\n",
-    "gain=3200;#gpm\n",
-    "print\"\\t  Removed.............. ....\\t....\\t....\\t\\t%.0f\\t%.0f\\n\",r1,r2,r3\n",
-    "#Rest of the table is calculated similarily\n",
-    "print\"\\n\\t\\t\\t\\t\\tCAUSTIC EVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t--------------------\\t\\tFlash Tank\\n\\t\\t\\t\\t\\t\\I\\t\\tII\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam pressure, psi/in.Hg\\t30\\n\\t2.Steam temperature,degreeF\\t\\t274\\t\\t169\\n\\t3.delT,degreeF\\t\\t\\t28\\t\\t28\\n\\t4.Liquor temperature, degreeF\\t246\\t\\t141\\t\\t192\\n\\t5.BPR, degreeF\\t\\t\\t77\\t\\t26\\t\\t77\\n\\t6.Vapor temperature, degreeF\\t\\t169\\t\\t115\\t\\t115\\n\\t7.Lambda, Btu/lb\\t\\t997\\t\\t1027\\t\\t1027\\n\\t8.Feed, lb/hr\\t\\t\\t22788\\t\\t50602\\t\\t13367\\n\\t9.Product, lb/hr\\t\\t13367\\t\\t40352\\t\\t12813\\n\\t10.Evaporation,lb/hr\\t\\t9421\\t\\t10250\\t\\t554\\n\\t11.Heat flow, Btu/hr\\t\\t11890000\\t11020000\\n\\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\\t700\\n\\t13.A,ft**2\\t\\t\\t683\\t\\t683\\n\\t14.Tubes, OD, in. and BWG\\t1,16\\t\\t1,16\\n\\t15.Tube length, ft\\t\\t7\\t\\t7\\n\\t16.No. tubes\\t\\t\\t432\\t\\t432\\n\\t17.Circulating pump. gpm\\t3200 at 20 ft\\t3200 at 20ft\\t167 at 45 ft\\n\\t18.Apparent efficiency, prcnt\\t54\\t\\t64\\n\\t18.BHP\\t\\t\\t\\t38\\t\\t35\\t\\t8.2\\n\\t20.Motor,hp\\t\\t\\t40\\t\\t40\\t\\t10.0\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "V=8;\n",
-    "s=1.5;\n",
-    "G=V*s*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\\n\",G\n",
-    "UD=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Combining with a steam film coefficient of approximately 1500\n",
-    "print\"\\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t251\\t2970000\\t\\t25.4\\t700\\t670\\t0.87\\t\\t3420000\\n\\t252\\t2480000\\t\\t25.0\\t700\\t680\\t0.88\\t\\t2820000\\n\\t252.5\\t2290000\\t\\t24.7\\t700\\t685\\t0.89\\t\\t2570000\\t\\t700\\n\\t253\\t2120000\\t\\t24.5\\t700\\t695\\t0.90\\t\\t2520000\\n\"\n",
-    "print\"\\tThee gain per minute is gpm\\n\",gain\n",
-    "print\"\\n\\t\\t\\t\\tCAUSTIC EVAPORATION HEAT BALANCE\\n\"\n",
-    "print\"\\t\\t\\t\\t(Basis = 1ton/hr NaOH)\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\tEFFECT\\t\\t\\tBtu/hr\\t\\tEvaopration, lb/hr\\n\"\n",
-    "hi=10500*930*0.974;#Btu/hr\n",
-    "hl=18230*(246-150)*0.83;#Btu/hr\n",
-    "rh=hi-hl;#Btu/hr\n",
-    "hc=300000;#Btu/hr\n",
-    "hv=rh-hc;#Btu/hr\n",
-    "evv=hv/997;#lb/hr\n",
-    "print\"\\t1.a.Heat in steam\\t\\thi\\n\\t  b.Heating liquor\\t\\thl\\n\\t  c.Resultant heat\\t\\trhf\\n\\t  d.Heat of concentrate\\t\\thc\\n\\t  e.Heat of vapors\\t\\thv\\t%.0f\\n\",hi,hl,rh,hc,hv,evv\n",
-    "s1=1.35;\n",
-    "G1=V*s1*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\n\\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\\n\",G1\n",
-    "UD1=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Using thermal characteristics for this solution\n",
-    "print\"\\tUD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD1\n",
-    "#As for effect I:\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t146\\t2400000\\t\\t25.4\\t700\\t620\\t0.80\\t\\t2790000\\t\\t700\\n\\t146.5\\t2160000\\t\\t25.2\\t700\\t683\\t0.89\\t\\t2430000\\n\"\n",
-    "#end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.7 pgno:447"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.7\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tM1 =  lb\n",
-      "17900\n",
-      "\n",
-      "\t\t\t\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tEffects\t\t\t\t\tStraight triple effect\t\t\t\tThermocompression\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tSteam  flow, lb/hr\t\t22400\t\t\t\t\t\t17900\n",
-      "\tSteam pressure, psi in.Hg\t20\t\t9\t\t2\t\t20\t\t9\t\t2\n",
-      "\tSteam temp,degreeF\t\t\t258\t\t237\t\t217\t\t258\t\t237\t\t217\n",
-      "\ttdelT,degreeF\t\t\t20\t\t18\t\t22\t\t20\t\t18\t\t22\n",
-      "\tLiquor temp, degreeF\t\t\t238\t\t219\t\t195\t\t238\t\t219\t\t195\n",
-      "\tBPR, degreeF\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\tVapor temp, degreeF\t\t\t237\t\t217\t\t192\t\t237\t\t215\t\t192\n",
-      "\tVapor pressure, pis/in.Hg\t9\t\t2\t\t10\t\t9\t\t2\t\t10\n",
-      "\tLambda, Btu/lb\t\t\t954\t\t965\t\t983\t\t954\t\t965\t\t983\n",
-      "\tLiquor in, lb/hr\t\t100000\t\t79400\t\t56900\t\t109000\t\t70000\t\t52400\n",
-      "\tLiqour out, lb/hr\t\t79400\t\t56900\t\t33300\t\t70000\t\t52400\t\t33300\n",
-      "\tEvaporation,lb/hr\t\t20600\t\t22500\t\t23500\t\t30000\t\t17600\t\t19100\n",
-      "\tdegreeBrix(out)\t\t\t\t\t\t\t\t\t\t\t\t\t30\n",
-      "\tCondenser water, gpm\t\t\t\t455\t\t\t\t\t\t365\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\n",
-      "\t\t\t\tCondenser water = 455 gpm\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\t1.a.Heat in steam\t\n",
-      "\t20424320.0\n",
-      "b.Heating liquor\t\n",
-      "\t736000.0\n",
-      "c.Evaporation\t\t Evaporation/954\t\n",
-      "\t19688320.0 20637.6519916\n",
-      "d.Liquor to 2d =  79362.3480084\n",
-      "total evapouriation 66700\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.7\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "M2=14300;#From fig.14.43 and heat balance above\n",
-    "M1=32200-14300;#From fig.14.43 and heat balance above\n",
-    "print\"\\tM1 =  lb\\n\",M1\n",
-    "print\"\\n\\t\\t\\t\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tEffects\\t\\t\\t\\t\\tStraight triple effect\\t\\t\\t\\tThermocompression\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tSteam  flow, lb/hr\\t\\t22400\\t\\t\\t\\t\\t\\t17900\\n\\tSteam pressure, psi in.Hg\\t20\\t\\t9\\t\\t2\\t\\t20\\t\\t9\\t\\t2\\n\\tSteam temp,degreeF\\t\\t\\t258\\t\\t237\\t\\t217\\t\\t258\\t\\t237\\t\\t217\\n\\ttdelT,degreeF\\t\\t\\t20\\t\\t18\\t\\t22\\t\\t20\\t\\t18\\t\\t22\\n\\tLiquor temp, degreeF\\t\\t\\t238\\t\\t219\\t\\t195\\t\\t238\\t\\t219\\t\\t195\\n\\tBPR, degreeF\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\\tVapor temp, degreeF\\t\\t\\t237\\t\\t217\\t\\t192\\t\\t237\\t\\t215\\t\\t192\\n\\tVapor pressure, pis/in.Hg\\t9\\t\\t2\\t\\t10\\t\\t9\\t\\t2\\t\\t10\\n\\tLambda, Btu/lb\\t\\t\\t954\\t\\t965\\t\\t983\\t\\t954\\t\\t965\\t\\t983\\n\\tLiquor in, lb/hr\\t\\t100000\\t\\t79400\\t\\t56900\\t\\t109000\\t\\t70000\\t\\t52400\\n\\tLiqour out, lb/hr\\t\\t79400\\t\\t56900\\t\\t33300\\t\\t70000\\t\\t52400\\t\\t33300\\n\\tEvaporation,lb/hr\\t\\t20600\\t\\t22500\\t\\t23500\\t\\t30000\\t\\t17600\\t\\t19100\\n\\tdegreeBrix(out)\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t30\\n\\tCondenser water, gpm\\t\\t\\t\\t455\\t\\t\\t\\t\\t\\t365\\n\"\n",
-    "print\"\\n\\t\\t\\t\\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\\n\\t\\t\\t\\tCondenser water = 455 gpm\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "sf=22400;#lb/hr\n",
-    "lc=100000;#lb/hr\n",
-    "t1=238;#degreeF\n",
-    "t2=230;#degreeF\n",
-    "te=30000+17600+19100;\n",
-    "his=sf*940*0.97;#Btu/hr\n",
-    "hlq=lc*(t1-t2)*0.92;#Btu/hr\n",
-    "hd=his-hlq;#Btu/hr\n",
-    "eva=(hd)/954;#lb/hr\n",
-    "l2d=lc-eva;\n",
-    "print\"\\t1.a.Heat in steam\\t\\n\\t\" ,his \n",
-    "print\"b.Heating liquor\\t\\n\\t\",hlq\n",
-    "print\"c.Evaporation\\t\\t Evaporation/954\\t\\n\\t\",hd,eva  \n",
-    "print\"d.Liquor to 2d = \",l2d\n",
-    "print\"total evapouriation\",te\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_2.ipynb
deleted file mode 100755
index 6c6ad595..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_2.ipynb
+++ /dev/null
@@ -1,1114 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 14 : Evapouration"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.1 pgno:383"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tQevap is  Btu/hr\t9610000\n",
-      "\tQ300 degreeF is  Btu/hr\t9600500\n",
-      "\tTemperature head =  degree F\t74\n",
-      "\tOverall coefficient \t605.5\n",
-      "\tSurface required is  ft^2\t2144.75416788\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "t1 = 300; # degreeF\n",
-    "t2 = 226; #degree F\n",
-    "bs = 700; # Btu/((hr)(ft^2)(ddegree F))\n",
-    "#Heat Balance\n",
-    "Qv = 10000 * 961; # Btu/hr\n",
-    "print\"\\tQevap is  Btu/hr\\t\",Qv\n",
-    "Q3 = 10550 * 910; #Btu/hr\n",
-    "print\"\\tQ300 degreeF is  Btu/hr\\t\",Q3\n",
-    "\n",
-    "delT = t1-t2; # degree F\n",
-    "print\"\\tTemperature head =  degree F\\t\",delT\n",
-    "Ud = bs * 0.865;\n",
-    "print\"\\tOverall coefficient \\t\",Ud\n",
-    "A = Qv*10/(Ud * delT); #ft^2\n",
-    "print\"\\tSurface required is  ft^2\\t\",A#Wrong calculation in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.2 pgno:412"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tTotal product is lb/hr\t10000.0\n",
-      "\tTotal evaporation is lb/hr\t40000.0\n",
-      "\tTotal temperature difference is del degree F\t119\n",
-      "\tAverage pressure difference is del psi/effect \t8.25\n",
-      "\t\t\t\t\t\tPressure, psia\t\t delP, psi \t Steam or vapor, degree F \t lambda, Btu/lb\t\tSteam chest, 1st effect \t 26.70 \t\t\t .... \t\t Ts = 244 \t\t ls = 949 \t\tSteam chest, 2nd effect \t 18.45 \t\t\t 8.25 \t\t t1 = 224 \t\t l1 = 961 \t\tSteam chest, 3rd effect \t 10.20(20.7 in. Hg) \t 8.25 \t\t t2 = 194 \t\t l1 = 981 \t\tVapor to condenser \t\t 1.95(26 in. Hg) \t 8.25 \t\t t2 = 125 \t\t l1 = 1022 \t\n",
-      "\t949*Ws + 50000*(100-224) = 961*w1\t\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\t\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\t\tw1+w2+w3 = 40000\t\n",
-      "\tSolving simultaneously\t\n",
-      "\tw1 = \t12400\n",
-      "\tw2 = \t13300\n",
-      "\tw3 = \t14300\n",
-      "\tW1-3 is \t40000\n",
-      "\tA1 is ft**2 \t1510\n",
-      "\tA2 is ft**2 \t1588\n",
-      "\tA3 is ft**2 \t1512\n",
-      "\tHeat to condenser is Btu/hr\t14614600\n",
-      "\tWater requirement is lb/hr\t417560\n",
-      "\t= gpm \t835\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "wf = 50000; #  lb/hr\n",
-    "sf = wf * 0.10; #  lb/hr\n",
-    "tp = sf/0.50; # lb/hr\n",
-    "print\"\\tTotal product is lb/hr\\t\",tp\n",
-    "te = wf - tp;\n",
-    "print\"\\tTotal evaporation is lb/hr\\t\",te\n",
-    "cf = 1.0;\n",
-    "tF = 100;  # degree F\n",
-    "T1 = 244; # degree F\n",
-    "T2 = 125; # degree F\n",
-    "U1=600; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U2=250; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U3=125; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "\n",
-    "T = T1-T2;\n",
-    "print\"\\tTotal temperature difference is del degree F\\t\",T\n",
-    "df = (26.70- 1.95)/3; # psi/effect\n",
-    "print\"\\tAverage pressure difference is del psi/effect \\t\",df\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\tPressure, psia\\t\\t delP, psi \\t Steam or vapor, degree F \\t lambda, Btu/lb\\t\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\t .... \\t\\t Ts = 244 \\t\\t ls = 949 \\t\\tSteam chest, 2nd effect \\t 18.45 \\t\\t\\t 8.25 \\t\\t t1 = 224 \\t\\t l1 = 961 \\t\\tSteam chest, 3rd effect \\t 10.20(20.7 in. Hg) \\t 8.25 \\t\\t t2 = 194 \\t\\t l1 = 981 \\t\\tVapor to condenser \\t\\t 1.95(26 in. Hg) \\t 8.25 \\t\\t t2 = 125 \\t\\t l1 = 1022 \\t\"\n",
-    "\n",
-    "print\"\\t949*Ws + 50000*(100-224) = 961*w1\\t\\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\\t\\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\\t\\tw1+w2+w3 = 40000\\t\"\n",
-    "print\"\\tSolving simultaneously\\t\"\n",
-    "w1=12400;\n",
-    "print\"\\tw1 = \\t\",w1\n",
-    "w2=13300;\n",
-    "print\"\\tw2 = \\t\",w2\n",
-    "w3=14300;\n",
-    "print\"\\tw3 = \\t\",w3\n",
-    "\n",
-    "Wt = w1+w2+w3;\n",
-    "print\"\\tW1-3 is \\t\",Wt\n",
-    "Ws = 19100;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "Ts = 244;\n",
-    "t1 = 224;\n",
-    "t2 = 194;\n",
-    "t3 = 125;\n",
-    "\n",
-    "A1 = (Ws * lms)/(U1*(Ts-t1)); #ft**2\n",
-    "print\"\\tA1 is ft**2 \\t\",A1\n",
-    "A2 = (w1*lm1)/(U2*(t1-t2)); #ft**2\n",
-    "print\"\\tA2 is ft**2 \\t\",A2\n",
-    "A3 = (w2 * lm2)/(U3*(t2-t3)); #ft**2\n",
-    "print\"\\tA3 is ft**2 \\t\",A3\n",
-    "\n",
-    "hc = w3 * lm3; # Btu/hr, WRONG CALCULATION IN TEXT BOOK\n",
-    "print\"\\tHeat to condenser is Btu/hr\\t\",hc\n",
-    "wr = hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement is lb/hr\\t\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t= gpm \\t\",wr1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.3 pgno:414"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t981*w2 + 50000*(100-125) = 1022*w3\n",
-      "\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\n",
-      "\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\n",
-      "\tw1+w2+w3 = 40000\n",
-      "\n",
-      "\tSolving simultaneously\n",
-      "\n",
-      "\tw1-3 =  \n",
-      "40000\n",
-      "\tA1 is  ft**2\n",
-      "2010\n",
-      "\tA2 is  ft**2\n",
-      "2043\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tAverage surface is  ft**2\n",
-      "1700\n",
-      "\n",
-      "\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\n",
-      "5100\n",
-      "\tRecalculation\n",
-      "\n",
-      "\tA1 is  ft**2\n",
-      "0\n",
-      "\tA2 is  ft**2\n",
-      "0\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tTs-t3 is  degreeF\n",
-      "119\n",
-      "\t\t\t\t\tPressure, psia\t\t Steam or vapor, degreeF \t lambda, Btu/lb\n",
-      "\tSteam chest, 1st effect \t 26.70 \t\t\tTs = 244 \t\t 949 \n",
-      "\tSteam chest, 2nd effect \t 16.0 \t\t\t t1 = 216 \t\t 968 \n",
-      "\tSteam chest, 3rd effect \t 16.4 in. Hg) \t\t t2 = 175 \t\t 992 \n",
-      "\tVapor to condenser \t\t 26 in. Hg \t\t t3 = 125 \t\t l1 = 1022 \n",
-      "\n",
-      "\tw1 is \n",
-      "15450\n",
-      "\tw2 is \n",
-      "13200\n",
-      "\tw3 is \n",
-      "11350\n",
-      "\tWs is \n",
-      "16850\n",
-      "\tHeat to condenser is  Btu/hr\n",
-      "11599700\n",
-      "\tWater requirement  lb/hr\n",
-      "331420\n",
-      "\t\t\t= gpm\n",
-      "662\n",
-      "\tEconomy, lb evaporation/lb steam \n",
-      "2\n",
-      "\t\t\t\tForward\t\tBackward\n",
-      "\tTotal steam, lb/hr\t19100\t\t16850\n",
-      "\tCooling water, gpm\t840\t\t664\n",
-      "\tTotal surface, ft**2\t4800\t\t4500\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Same conditions as example 14.2\n",
-    "U1 = 400; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U2 = 250; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U3 = 175; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "\n",
-    "w1 = 50000; # lb/hr     From example 14.2\n",
-    "wt = 40000; # lb/hr     From example 14.2\n",
-    "cf = 1; # From example 14.2\n",
-    "\n",
-    "print\"\\t981*w2 + 50000*(100-125) = 1022*w3\\n\\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\\n\\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\\n\\tw1+w2+w3 = 40000\\n\"\n",
-    "print\"\\tSolving simultaneously\\n\"\n",
-    "w1 = 15950;\n",
-    "w2 = 12900;\n",
-    "w3 = 11150;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "\n",
-    "wt = w1+w2+w3;\n",
-    "print\"\\tw1-3 =  \\n\",wt\n",
-    "Ws = 16950;\n",
-    "A1 = (Ws*lms)/(U1*20); #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A1\n",
-    "A2 = (w1*lm1)/(U2*30); #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A2\n",
-    "A3 = (w2*lm2)/(U3*69); #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A3\n",
-    "\n",
-    "Avs = (A1 + A2 + A3)/3; #ft**2\n",
-    "print\"\\tAverage surface is  ft**2\\n\",Avs\n",
-    "Av1 = 3 * Avs; #ft**2\n",
-    "print\"\\n\\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\\n\",Av1\n",
-    "print\"\\tRecalculation\\n\"\n",
-    "Av2 = 1500; #ft**2, assume\n",
-    "dT1 = 28; #degreeF\n",
-    "A4 = (20/dT1)*A1; #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A4\n",
-    "dT2 = 41; #degreeF\n",
-    "A5  = (30/dT2)*A2; #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A5\n",
-    "dT3 = 50; #degreeF\n",
-    "A6 = (69/50)*A3; #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A6\n",
-    "del1 = 119; #degreeF\n",
-    "print\"\\tTs-t3 is  degreeF\\n\",del1\n",
-    "print\"\\t\\t\\t\\t\\tPressure, psia\\t\\t Steam or vapor, degreeF \\t lambda, Btu/lb\\n\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\tTs = 244 \\t\\t 949 \\n\\tSteam chest, 2nd effect \\t 16.0 \\t\\t\\t t1 = 216 \\t\\t 968 \\n\\tSteam chest, 3rd effect \\t 16.4 in. Hg) \\t\\t t2 = 175 \\t\\t 992 \\n\\tVapor to condenser \\t\\t 26 in. Hg \\t\\t t3 = 125 \\t\\t l1 = 1022 \\n\"\n",
-    "\n",
-    "w1 = 15450; #Solving again for \n",
-    "print\"\\tw1 is \\n\",w1\n",
-    "w2 = 13200;\n",
-    "print\"\\tw2 is \\n\",w2\n",
-    "w3 = 11350;\n",
-    "print\"\\tw3 is \\n\",w3\n",
-    "Ws = 16850;\n",
-    "print\"\\tWs is \\n\",Ws\n",
-    "Hc = w3 * 1022;\n",
-    "print\"\\tHeat to condenser is  Btu/hr\\n\",Hc\n",
-    "wr = Hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement  lb/hr\\n\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t\\t\\t= gpm\\n\",wr1\n",
-    "ec = wt/Ws;\n",
-    "print\"\\tEconomy, lb evaporation/lb steam \\n\",ec\n",
-    "\n",
-    "#comparision of forward and backward feed\n",
-    "print\"\\t\\t\\t\\tForward\\t\\tBackward\\n\\tTotal steam, lb/hr\\t19100\\t\\t16850\\n\\tCooling water, gpm\\t840\\t\\t664\\n\\tTotal surface, ft**2\\t4800\\t\\t4500\"\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.4 pgno:418"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.4 \n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\n",
-      "\n",
-      "\tEffects\t\tWater evaporated(lb/(hr)*(ft**2))\n",
-      "\n",
-      "\t1\t\t14-16\n",
-      "\t2\t\t6-8\n",
-      "\t3\t\t5-6\n",
-      "\t4\t\t4-5\n",
-      "\t5\t\t3-4\n",
-      "\n",
-      "\n",
-      "\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam  flow, lb/hr\t\t42600\t\t38000\n",
-      "\t2.Steam pressure, psi/in.Hg\t30\t\t30\t\t15\t\t5\t\t4\t\t14.5\n",
-      "\n",
-      "\t3.Steam temp,degreeF\t\t\t274\t\t274\t\t250\t\t227\t\t205\t\t181\n",
-      "\n",
-      "\t4.delT,degreeF\t\t\t23\t\t23\t\t21\t\t20\t\t20\t\t27\n",
-      "\t5.Liquor temp, degreeF\t\t251\t\t251\t\t229\t\t207\t\t185\t\t164\n",
-      "\t6.BPR, degreeF\t\t\t1\t\t1\t\t2\t\t2\t\t4\t\t7\n",
-      "\t7.Vapor temp, degreeF\t\t250\t\t250\t\t227\t\t205\t\t181\t\t147\n",
-      "\t8.Vapor pressure, pis/in.Hg\t15\t\t15\t\t5\t\t4\t\t14.5\t\t23\n",
-      "\t9.Lambda, Btu/lb\t\t946\t\t946\t\t960\t\t975\t\t990\t\t1010\n",
-      "\t10.Liquor in, lb/hr\t\t229000\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\n",
-      "\t11.Liqour out, lb/hr\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\t\t49600\n",
-      "\t12.Evaporation,lb/hr\t\t38800\t\t36200\t\t36900\t\t29300\t\t23800\t\t14400\n",
-      "\t13.degreeBrix(out)\t\t\t15.7\t\t19.4\t\t25.5\t\t34.4\t\t46.5\t\t50.0\n",
-      "\t14.A,ft**2\t\t\t3500\t\t3500\t\t5000\t\t5000\t\t5000\t\t3500\n",
-      "\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\t478\t\t425\t\t310\t\t264\t\t219\t\t138\n",
-      "\t16.UD delT,Btu/(hr)*(ft**2)\t11000\t\t9780\t\t6520\t\t5270\t\t4390\t\t3740\n",
-      "\n",
-      "\tTotal temperature difference in the evaporator system =  degreeF\n",
-      "127\n",
-      "\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\n",
-      "16\n",
-      "\tTotal EFFECTIVE  temperature difference = degreeF\n",
-      "111\n",
-      "\n",
-      "\t\t\t\tSUGAR-JUICE HEATERS\n",
-      "\n",
-      "\tRaw-juice heaters\t\t\t\tClear=juice heaters\n",
-      "\t-----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr 229000 212 184 5834920.0\n",
-      "\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\n",
-      "229000 243 220 4792970.0\n",
-      "\tVapor temp. = 227degreeF\tdelT=26.6degreeF\t\tVapor temp. = 250degreeF\tdelT=15.8degreeF\n",
-      "\n",
-      "\tud1=.\t\t\t\t\t\tUD=ud2\n",
-      "231 243\n",
-      "\tSurface,A=A1 ft**2\t\t\t\tSurface,A=A2 ft**2\n",
-      "\n",
-      "949.601275917 1248.36432776\n",
-      "\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr 229000 184 144 8244000.0\n",
-      "\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\n",
-      "229000 220 200 4122000.0\n",
-      "\tVapor temp. = 205degreeF\tdelT=37.6degreeF\t\tVapor temp. = 227degreeF\tdelT=14.8degreeF\n",
-      "\n",
-      "\tUD=Ud3\t\t\t\t\t\tUD=Ud4\n",
-      "230 214\n",
-      "\tSurface,A=A3 ft**2\t\t\t\tSurface,A=A4 ft**2\n",
-      "\n",
-      "953.2839963 1301.46501642\n",
-      "\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr 229000 144 82 4122000.0\n",
-      "\t(Use 2 heaters at 1300 ft**2 each plus 1\n",
-      "\t\t\t\t\t\t\theater at 1300 ft**2 as spare)\n",
-      "\n",
-      "\tVapor temp. = 181degreeF\tdelT=62.2degreeF\n",
-      "\tSurface,A=\n",
-      "946.715663757\n",
-      "\t(Use 3 heaters at 100 ft**2\n",
-      "\teach plus 1 heater as spare)\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t----------------------------------------------------\n",
-      "\n",
-      "\t1A.Heat in steam........\n",
-      "38388138.0\n",
-      "\t   Heating liquor.......\n",
-      "\t\t\t\t%.3e\t.\n",
-      "1667120.0 36721018.0 38817.1437632\n",
-      "\t   Liqour to 1B\n",
-      "\t   =  lb/hr\n",
-      "190182.856237\n",
-      "\t1B.Heat in steam........\n",
-      "34979292.7593\n",
-      "\t   Heating liquor........\n",
-      "\t\t\t\t\n",
-      "0.0 34979292.7593 36975.9965744\n",
-      "\t   Liqour to 2d \n",
-      "\t   effect= lb/hr\n",
-      "153206.859662\n",
-      "\t\t\t\t\t\t\t\tLb/hr\n",
-      "\n",
-      "\t(a) Actual evaporation..................................\n",
-      "179400\n",
-      "\t(b) Equivalent evaporation from vapors of \n",
-      "\t    1st effect used for vaccum pans......................\n",
-      "145500\n",
-      "\t(c) Equivalent evaporation from 1st effect \n",
-      "\t    vapors used for clarified-juice heaters..............\n",
-      "19700\n",
-      "\t(d) Equivalent evaporation from 2d effect \n",
-      "\t    vapors used for clarified-and raw-juice heaters......\n",
-      "30600\n",
-      "\t(e) Equivalent evaporation from 3d effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "2.71828182846\n",
-      "\t(f) Equivalent evaporation from 4th effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "13100\n",
-      "\t                                                        -----\n",
-      "\n",
-      "\t     Extrapolated evaporation............................\n",
-      "406200\n",
-      "\t\tEstimated steam quantity =  lb/hr\n",
-      "81240\n",
-      "\t\tActual steam required from final heat balance =  lb/hr\n",
-      "80600\n",
-      "\t\t\t\t\t\t\tError =  lb/hr\n",
-      "640\n",
-      "\tGallons per minute of Water required =  gpm 583\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.4 \\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "from math import e\n",
-    "#Assumed that 37500 lb/hr of 15 psig vapor is bled from the first effect for use in thevaccum pans\n",
-    "print\"\\n\\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\\n\"\n",
-    "print\"\\tEffects\\t\\tWater evaporated(lb/(hr)*(ft**2))\\n\"\n",
-    "print\"\\t1\\t\\t14-16\\n\\t2\\t\\t6-8\\n\\t3\\t\\t5-6\\n\\t4\\t\\t4-5\\n\\t5\\t\\t3-4\\n\"\n",
-    "print\"\\n\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t42600\\t\\t38000\\n\\t2.Steam pressure, psi/in.Hg\\t30\\t\\t30\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\n\"\n",
-    "print\"\\t3.Steam temp,degreeF\\t\\t\\t274\\t\\t274\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\n\"\n",
-    "print\"\\t4.delT,degreeF\\t\\t\\t23\\t\\t23\\t\\t21\\t\\t20\\t\\t20\\t\\t27\\n\\t5.Liquor temp, degreeF\\t\\t251\\t\\t251\\t\\t229\\t\\t207\\t\\t185\\t\\t164\\n\\t6.BPR, degreeF\\t\\t\\t1\\t\\t1\\t\\t2\\t\\t2\\t\\t4\\t\\t7\\n\\t7.Vapor temp, degreeF\\t\\t250\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\t\\t147\\n\\t8.Vapor pressure, pis/in.Hg\\t15\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\t\\t23\\n\\t9.Lambda, Btu/lb\\t\\t946\\t\\t946\\t\\t960\\t\\t975\\t\\t990\\t\\t1010\\n\\t10.Liquor in, lb/hr\\t\\t229000\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\n\\t11.Liqour out, lb/hr\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\t\\t49600\\n\\t12.Evaporation,lb/hr\\t\\t38800\\t\\t36200\\t\\t36900\\t\\t29300\\t\\t23800\\t\\t14400\\n\\t13.degreeBrix(out)\\t\\t\\t15.7\\t\\t19.4\\t\\t25.5\\t\\t34.4\\t\\t46.5\\t\\t50.0\\n\\t14.A,ft**2\\t\\t\\t3500\\t\\t3500\\t\\t5000\\t\\t5000\\t\\t5000\\t\\t3500\\n\\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\\t478\\t\\t425\\t\\t310\\t\\t264\\t\\t219\\t\\t138\\n\\t16.UD delT,Btu/(hr)*(ft**2)\\t11000\\t\\t9780\\t\\t6520\\t\\t5270\\t\\t4390\\t\\t3740\\n\"#BPR values from fig 14.34a\n",
-    "#Saturate vapor pressure above the liquour determined from Table 7\n",
-    "#Saturated steam pressure in the following effect determined from Table 7\n",
-    "\n",
-    "t1 = 274; #degreeF\n",
-    "t2 = 147; #degreeF\n",
-    "t = t1-t2; #degreeF\n",
-    "print\"\\tTotal temperature difference in the evaporator system =  degreeF\\n\",t\n",
-    "bpr1 = 1; #degreeF\n",
-    "bpr2 = 2; #degreeF\n",
-    "bpr3 = 2; #degreeF\n",
-    "bpr4 = 4; #degreeF\n",
-    "bpr5 = 7; #degreeF\n",
-    "bpr = bpr1 + bpr2 + bpr3 + bpr4 + bpr5; #degreeF\n",
-    "print\"\\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\\n\",bpr\n",
-    "tf = t-bpr; #degreeF\n",
-    "print\"\\tTotal EFFECTIVE  temperature difference = degreeF\\n\",tf\n",
-    "lbh = 229000; #lb/hr\n",
-    "tp1=212; #degreeF\n",
-    "tp2=184; #degreeF\n",
-    "tp3=144; #degreeF\n",
-    "tp4=82; #degreeF\n",
-    "tj1=243; #degreeF\n",
-    "tj2=220; #degreeF\n",
-    "tj3=200; #degreeF\n",
-    "Ud1=231;\n",
-    "Ud2=243;\n",
-    "Ud3=230;\n",
-    "Ud4=214;\n",
-    "Ud5=217;\n",
-    "print\"\\n\\t\\t\\t\\tSUGAR-JUICE HEATERS\\n\"\n",
-    "print\"\\tRaw-juice heaters\\t\\t\\t\\tClear=juice heaters\\n\\t-----------------------------------------------------------------------------------------\\n\"\n",
-    "rj1=lbh*(tp1-tp2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr\",lbh,tp1,tp2,rj1\n",
-    "rj2=lbh*(tj1-tj2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\\n\",lbh,tj1,tj2,rj2\n",
-    "print\"\\tVapor temp. = 227degreeF\\tdelT=26.6degreeF\\t\\tVapor temp. = 250degreeF\\tdelT=15.8degreeF\\n\"\n",
-    "print\"\\tud1=.\\t\\t\\t\\t\\t\\tUD=ud2\\n\",Ud1,Ud2\n",
-    "A1=rj1/(26.6*Ud1);#ft**2\n",
-    "A2=rj2/(15.8*Ud2);#ft**2\n",
-    "print\"\\tSurface,A=A1 ft**2\\t\\t\\t\\tSurface,A=A2 ft**2\\n\\n\",A1,A2\n",
-    "\n",
-    "rj3=lbh*(tp2-tp3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr\",lbh,tp2,tp3,rj3\n",
-    "rj4=lbh*(tj2-tj3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\\n\",lbh,tj2,tj3,rj4\n",
-    "print\"\\tVapor temp. = 205degreeF\\tdelT=37.6degreeF\\t\\tVapor temp. = 227degreeF\\tdelT=14.8degreeF\\n\"\n",
-    "print\"\\tUD=Ud3\\t\\t\\t\\t\\t\\tUD=Ud4\\n\",Ud3,Ud4\n",
-    "A3=rj3/(37.6*Ud3);#ft**2\n",
-    "A4=rj4/(14.8*Ud4);#ft**2\n",
-    "print\"\\tSurface,A=A3 ft**2\\t\\t\\t\\tSurface,A=A4 ft**2\\n\\n\",A3,A4\n",
-    "\n",
-    "rj5=lbh*(tp3-tp4)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr\",lbh,tp3,tp4,rj4\n",
-    "print\"\\t(Use 2 heaters at 1300 ft**2 each plus 1\\n\\t\\t\\t\\t\\t\\t\\theater at 1300 ft**2 as spare)\\n\"\n",
-    "A5=rj5/(62.2*Ud5);#ft**2\n",
-    "print\"\\tVapor temp. = 181degreeF\\tdelT=62.2degreeF\\n\\tSurface,A=\\n\",A5\n",
-    "print\"\\t(Use 3 heaters at 100 ft**2\\n\\teach plus 1 heater as spare)\\n\\n\"\n",
-    "\n",
-    "v1=42600;#lb/hr\n",
-    "tt1=251;#degreeF\n",
-    "print\"\\t\\t\\t\\tHEAT BALANCE\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t----------------------------------------------------\\n\"\n",
-    "hia=v1*929*0.97;#Btu/hr\n",
-    "print\"\\t1A.Heat in steam........\\n\",hia\n",
-    "hla=lbh*(tt1-tj1)*0.91;#Btu/hr\n",
-    "hh=hia-hla;#Btu/hr\n",
-    "lb1=946;#Btu/lb\n",
-    "dif=hh/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor.......\\n\\t\\t\\t\\t%.3e\\t.\\n\",hla,hh,dif\n",
-    "ltob=lbh-dif;#lb/hr\n",
-    "print\"\\t   Liqour to 1B\\n\\t   =  lb/hr\\n\",ltob\n",
-    "hia1=dif*929*0.97;#Btu/hr\n",
-    "print\"\\t1B.Heat in steam........\\n\",hia1\n",
-    "hla1=ltob*(tt1-tt1)*0.91;#Btu/hr\n",
-    "hh1=hia1;#Btu/hr\n",
-    "dif1=hh1/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor........\\n\\t\\t\\t\\t\\n\",hla1,hh1,dif1\n",
-    "dif2=ltob-dif1;#lb/hr\n",
-    "print\"\\t   Liqour to 2d \\n\\t   effect= lb/hr\\n\",dif2\n",
-    "#Similarily the values in the table are calculated\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\tLb/hr\\n\"\n",
-    "aa=179400;#lb/hr\n",
-    "bb=145500;#lb/hr\n",
-    "cc=19700;#lb/hr\n",
-    "dd=30600;#lb/hr\n",
-    "ee=17900;#lb/hr\n",
-    "ff=13100;#lb/hr\n",
-    "tto=aa+bb+cc+dd+ee+ff;#lb/hr\n",
-    "print\"\\t(a) Actual evaporation..................................\\n\",aa\n",
-    "print\"\\t(b) Equivalent evaporation from vapors of \\n\\t    1st effect used for vaccum pans......................\\n\",bb\n",
-    "print\"\\t(c) Equivalent evaporation from 1st effect \\n\\t    vapors used for clarified-juice heaters..............\\n\",cc\n",
-    "print\"\\t(d) Equivalent evaporation from 2d effect \\n\\t    vapors used for clarified-and raw-juice heaters......\\n\",dd\n",
-    "print\"\\t(e) Equivalent evaporation from 3d effect \\n\\t    vapors used for raw-juice heaters....................\\n\",e\n",
-    "print\"\\t(f) Equivalent evaporation from 4th effect \\n\\t    vapors used for raw-juice heaters....................\\n\",ff\n",
-    "print\"\\t                                                        -----\\n\"\n",
-    "print\"\\t     Extrapolated evaporation............................\\n\",tto\n",
-    "esq=tto/5;#lb/hr\n",
-    "print\"\\t\\tEstimated steam quantity =  lb/hr\\n\",esq\n",
-    "aesq=80600;#lb/hr\n",
-    "err = esq-aesq;#lb/hr\n",
-    "print\"\\t\\tActual steam required from final heat balance =  lb/hr\\n\",aesq\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\tError =  lb/hr\\n\",err\n",
-    "ta=15;\n",
-    "Q=14575000; #Btu/hr Total hourly evaporation\n",
-    "Gpm=Q/(500*(t2-tp4-ta));#From equation 14.4\n",
-    "print\"\\tGallons per minute of Water required =  gpm\",Gpm\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.5 pgno:427"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 9,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.5\t\n",
-      "\tapproximate values are mentioned in the book \t\n",
-      "\tOverall temperature difference =  deg F\t155\n",
-      "\tThe estimated total BPR =  degF\t[10 18 25 31 36 41]\n",
-      "\tEffective temperature difference = %.0f degF\t[145 137 130 124 119 114]\n",
-      "\t\t\t\t\tEVAPORATOR SUMMARY\t\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\t\t\t\t\t\t----------------------------------------------------------------------------------------------\t\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\t1.Steam  flow, lb/hr\t\t20000\t\t2.Steam pressure, psi/in.Hg\t35\t\t14.5\t\t4\t\t7\t\t16.5\t\t22\t\t3.Steam temp,degF\t\t\t280\t\t249\t\t224\t\t199\t\t174\t\t151\t\t4.delT,degF\t\t\t21\t\t17\t\t18\t\t19\t\t18\t\t21\t\t5.Liquor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t6.BPR, degF\t\t\t10\t\t8\t\t7\t\t6\t\t5\t\t5\t\t7.Vapor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t8.Vapor pressure, pis/in.Hg\t14.5\t\t4\t\t7\t\t6\t\t5\t\t5\t\t9.Lambda, Btu/lb\t\t946\t\t962\t\t978\t\t994\t\t1008\t\t1022\t\t10.Liquor in, lb/hr\t\t73400\t\t88300\t\t101000\t\t113000\t\t72000\t\t72000\t\t11.Liqour out, lb/hr\t\t56200\t\t73400\t\t88300\t\t101100\t\t58300\t\t54700\t\t12.Evaporation,lb/hr\t\t17200\t\t14900\t\t12800\t\t11900\t\t13700\t\t17300\t\t13.Total solids, \t\t38.9\t\t29.8\t\t24.7\t\t21.6\t\t18.7\t\t20.0\t\t14.A,ft^2\t\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t15.UD,Btu/(hr)*(ft^2)*(degF)\t262\t\t295\t\t252\t\t251\t\t221\t\t221\t\t16.UD delT,Btu/(hr)*(ft^2)\t5510\t\t5000\t\t4530t\t\t4770\t\t3980\t\t4650\t\n",
-      "\t\tTotal amount of water evaporated = \t lb/hr\t[17200 32100 44900 56800 70500     0]\n",
-      "\tTheoretical amount of steam for a six-effect evaporator = \t lb/hr\t[ 2866  5350  7483  9466 11750     0]\n",
-      "\tSteam used for trail balance = \t lb/hr\t[  3822.22222222   7133.33333333   9977.77777778  12622.22222222\n",
-      "  15666.66666667      0.        ]\n",
-      "\tEstimate of the amount of evaporation in the first effect = \t lb/hr\t[  3295.9    6152.5    8605.45  10885.9   13512.5       0.  ]\n",
-      "\tEstimated discharge from second effect = \t lb/hr\t[ 59495.9   62352.5   64805.45  67085.9   69712.5   56200.  ]\n",
-      "\t\t\t\t\tHEAT BALANCE\t\n",
-      "\t\tCooling water at 60 degreeF = \t gpm\t710\n",
-      "\t--------------------------------------------------------\t\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\t\n",
-      "\t--------------------------------------------------------\t\n",
-      "\t1.a.Heat in steam \t\t17925600.0\n",
-      "\t  b.Heating liquor \t\t1625076.0\n",
-      "\t  c.Evaporation\t\t\t\t\t\t17230.9978858\n",
-      "\t  d.To flash tank\t2190591.08245\n",
-      "\t\t\t\t2239.86818247\n",
-      "\t  e.Flashed vapor=\t\t2239.86818247\n",
-      "\t  f.product \t53929.1339317\n",
-      "\t\t2.a.Heat in 1st vapors\t\t16300524.0\n",
-      "\t  b.Heating liqour\t\t1951430.0\n",
-      "\t  c.Evaporation= 14915.8981289\n",
-      "\t\t\t\t\t14915.8981289\n",
-      "\t  d.Liquor to 1b=\t\t73384.1018711\n",
-      "total hourly evapouration lb : 90000\n",
-      "economy is lb/lb : 4.5\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.5\\t\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\t\"\n",
-    "st1=280; #degF\n",
-    "vt6=125; #degF\n",
-    "odT=st1-vt6; #degF\n",
-    "print\"\\tOverall temperature difference =  deg F\\t\",odT #corresponding to 35 psig and 26 in. Hg\n",
-    "import numpy\n",
-    "bpr=numpy.array([10, 8, 7, 6, 5, 5])\n",
-    "#bpr(1)=10; #degF\n",
-    "#bpr(2)=8; #degF\n",
-    "#bpr(3)=7; #degF\n",
-    "#bpr(4)=6; #degF\n",
-    "#bpr(5)=5; #degF\n",
-    "#bpr(6)=5; #degF\n",
-    "i=1;\n",
-    "tbpr=numpy.array([0, 0, 0, 0, 0, 0]);\n",
-    "tbpr[0]=bpr[0];\n",
-    "while (i<6):\n",
-    "\n",
-    "    tbpr[i]=tbpr[i-1]+bpr[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\tThe estimated total BPR =  degF\\t\",tbpr #from fig. 14.36a\n",
-    "edT=odT-tbpr;\n",
-    "print\"\\tEffective temperature difference = %.0f degF\\t\",edT\n",
-    "print\"\\t\\t\\t\\t\\tEVAPORATOR SUMMARY\\t\\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\t\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\t\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t20000\\t\\t2.Steam pressure, psi/in.Hg\\t35\\t\\t14.5\\t\\t4\\t\\t7\\t\\t16.5\\t\\t22\\t\\t3.Steam temp,degF\\t\\t\\t280\\t\\t249\\t\\t224\\t\\t199\\t\\t174\\t\\t151\\t\\t4.delT,degF\\t\\t\\t21\\t\\t17\\t\\t18\\t\\t19\\t\\t18\\t\\t21\\t\\t5.Liquor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t6.BPR, degF\\t\\t\\t10\\t\\t8\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t7.Vapor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t8.Vapor pressure, pis/in.Hg\\t14.5\\t\\t4\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t9.Lambda, Btu/lb\\t\\t946\\t\\t962\\t\\t978\\t\\t994\\t\\t1008\\t\\t1022\\t\\t10.Liquor in, lb/hr\\t\\t73400\\t\\t88300\\t\\t101000\\t\\t113000\\t\\t72000\\t\\t72000\\t\\t11.Liqour out, lb/hr\\t\\t56200\\t\\t73400\\t\\t88300\\t\\t101100\\t\\t58300\\t\\t54700\\t\\t12.Evaporation,lb/hr\\t\\t17200\\t\\t14900\\t\\t12800\\t\\t11900\\t\\t13700\\t\\t17300\\t\\t13.Total solids, \\t\\t38.9\\t\\t29.8\\t\\t24.7\\t\\t21.6\\t\\t18.7\\t\\t20.0\\t\\t14.A,ft^2\\t\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t15.UD,Btu/(hr)*(ft^2)*(degF)\\t262\\t\\t295\\t\\t252\\t\\t251\\t\\t221\\t\\t221\\t\\t16.UD delT,Btu/(hr)*(ft^2)\\t5510\\t\\t5000\\t\\t4530t\\t\\t4770\\t\\t3980\\t\\t4650\\t\"#BPR values from fig 14.36a\n",
-    "#Specific-heat data are given in Fig. 14.36b\n",
-    "ev=numpy.array([17200, 14900, 12800, 11900, 13700, 17300]);\n",
-    "#ev(1)=17200; #lb/hr\n",
-    "#ev(2)=14900; #lb/hr\n",
-    "#ev(3)=12800; #lb/hr\n",
-    "#ev(4)=11900; #lb/hr\n",
-    "#ev(5)=13700; #lb/hr\n",
-    "#ev(6)=17300; #lb/hr\n",
-    "i=1;\n",
-    "tev =numpy.array([0, 0, 0, 0, 0, 0])\n",
-    "tev[0]=ev[0];\n",
-    "while (i<5):\n",
-    "    tev[i]= tev[i-1]+ev[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\tTotal amount of water evaporated = \\t lb/hr\\t\",tev\n",
-    "ttev=tev/6;#lb/hr\n",
-    "print\"\\tTheoretical amount of steam for a six-effect evaporator = \\t lb/hr\\t\",ttev\n",
-    "tev2=tev/(6*0.75); #lb/hr . order of 75 percent of theoretical\n",
-    "print\"\\tSteam used for trail balance = \\t lb/hr\\t\",tev2\n",
-    "lq=(tev/6);\n",
-    "lq=lq+(lq*0.15);\n",
-    "print\"\\tEstimate of the amount of evaporation in the first effect = \\t lb/hr\\t\",lq\n",
-    "lout6=54000;#lb/hr\n",
-    "lq2=lout6+lq+2200;#lb/hr\n",
-    "print\"\\tEstimated discharge from second effect = \\t lb/hr\\t\",lq2\n",
-    "print\"\\t\\t\\t\\t\\tHEAT BALANCE\\t\"\n",
-    "cw = 17750000/(500*(125-15-60)); #gpm, values from table 14.6\n",
-    "print\"\\t\\tCooling water at 60 degreeF = \\t gpm\\t\",cw\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\t\"\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "sf=20000;#lb/hr\n",
-    "lqi=73400;#lb/hr\n",
-    "the=90000;\n",
-    "lqi2=88300\n",
-    "lt1=259;#degreeF\n",
-    "lt2=232;#degreeF\n",
-    "lt3=206;#degreeF\n",
-    "ecn=90000./20000.;\n",
-    "ev=17200;#lb/hr\n",
-    "his=sf*924*0.97;#Btu/hr\n",
-    "print\"\\t1.a.Heat in steam \\t\\t\",his\n",
-    "hl=lqi*(lt1-lt2)*0.82;#Btu/hr\n",
-    "print\"\\t  b.Heating liquor \\t\\t\",hl\n",
-    "hh=his-hl;\n",
-    "ev1=(hh)/946;#lb/hr\n",
-    "print\"\\t  c.Evaporation\\t\\t\\t\\t\\t\\t\",ev1\n",
-    "dif=lqi-ev1;\n",
-    "tft=(dif)*(lt1-209)*0.78;\n",
-    "print\"\\t  d.To flash tank\\t\",tft\n",
-    "ev2=tft/978;#lb/hr\n",
-    "print\"\\t\\t\\t\\t\",ev2\n",
-    "print\"\\t  e.Flashed vapor=\\t\\t\",ev2\n",
-    "p=dif-ev2;\n",
-    "print\"\\t  f.product \\t\",p\n",
-    "print\"\\t\\t2.a.Heat in 1st vapors\\t\\t\",hh\n",
-    "hl2=lqi2*(lt2-lt3)*0.85;\n",
-    "print\"\\t  b.Heating liqour\\t\\t\",hl2\n",
-    "ev3=(hh-hl2)/962;\n",
-    "print\"\\t  c.Evaporation=\",ev3\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\",ev3\n",
-    "lto1=lqi2-ev3;\n",
-    "print\"\\t  d.Liquor to 1b=\\t\\t\",lto1\n",
-    "print\"total hourly evapouration lb :\",the\n",
-    "print\"economy is lb/lb :\",ecn\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.6 pgno:437"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.6\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tTotal temperature difference =  degreeF\n",
-      "159\n",
-      "\tThe effective temperature difference is  degreeF\n",
-      "56\n",
-      "\n",
-      "\t\t\tCAUSTIC EVAPORATOR MATERIAL BALANCE\n",
-      "\n",
-      "\tCell liquour at 120degreeF \t\tWash at 80degreeF\n",
-      "\n",
-      "\t---------------------------------------------\n",
-      "\n",
-      "\t8.75 prcnt NaOH = l1\n",
-      "\t16.6 prcnt NaCl = l2\t\t25 prcnt NaCl = w2\n",
-      "2000 3800 340\n",
-      "\t74.65 prcnt H20 = l3\t\t75 prcnt H20 = w2\n",
-      "17050 1020\n",
-      "\tTotal cell liquor = lq\tTotoal wash = w\n",
-      "22850 1360\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\t\t\t\tNaOH\t\tNaCl\t\tH20,Lb\tTotal,Lb\n",
-      "\t\t\t\tprcnt\tLb\tprcnt\tLb\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\tOverall operation:\n",
-      "\t  Cell liquor.......... 8.75\t2000 3800 17050 22850\n",
-      "\t  Wash................. ....\t....\t25.00\t340 1020 1360\n",
-      "\t  Total in............. ....\t2000 4140 18070 24210\n",
-      "\t  Product.............. 50.00\t2000 110 1890 4000\n",
-      "\t  Removed.............. ....\t....\t....\t\t%.0f\t%.0f\n",
-      "4030 16180 20210\n",
-      "\n",
-      "\t\t\t\t\tCAUSTIC EVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t--------------------\t\tFlash Tank\n",
-      "\t\t\t\t\t\\I\t\tII\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam pressure, psi/in.Hg\t30\n",
-      "\t2.Steam temperature,degreeF\t\t274\t\t169\n",
-      "\t3.delT,degreeF\t\t\t28\t\t28\n",
-      "\t4.Liquor temperature, degreeF\t246\t\t141\t\t192\n",
-      "\t5.BPR, degreeF\t\t\t77\t\t26\t\t77\n",
-      "\t6.Vapor temperature, degreeF\t\t169\t\t115\t\t115\n",
-      "\t7.Lambda, Btu/lb\t\t997\t\t1027\t\t1027\n",
-      "\t8.Feed, lb/hr\t\t\t22788\t\t50602\t\t13367\n",
-      "\t9.Product, lb/hr\t\t13367\t\t40352\t\t12813\n",
-      "\t10.Evaporation,lb/hr\t\t9421\t\t10250\t\t554\n",
-      "\t11.Heat flow, Btu/hr\t\t11890000\t11020000\n",
-      "\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\t700\n",
-      "\t13.A,ft**2\t\t\t683\t\t683\n",
-      "\t14.Tubes, OD, in. and BWG\t1,16\t\t1,16\n",
-      "\t15.Tube length, ft\t\t7\t\t7\n",
-      "\t16.No. tubes\t\t\t432\t\t432\n",
-      "\t17.Circulating pump. gpm\t3200 at 20 ft\t3200 at 20ft\t167 at 45 ft\n",
-      "\t18.Apparent efficiency, prcnt\t54\t\t64\n",
-      "\t18.BHP\t\t\t\t38\t\t35\t\t8.2\n",
-      "\t20.Motor,hp\t\t\t40\t\t40\t\t10.0\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\n",
-      "2700000.0\n",
-      "\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t251\t2970000\t\t25.4\t700\t670\t0.87\t\t3420000\n",
-      "\t252\t2480000\t\t25.0\t700\t680\t0.88\t\t2820000\n",
-      "\t252.5\t2290000\t\t24.7\t700\t685\t0.89\t\t2570000\t\t700\n",
-      "\t253\t2120000\t\t24.5\t700\t695\t0.90\t\t2520000\n",
-      "\n",
-      "\tThee gain per minute is gpm\n",
-      "3200\n",
-      "\n",
-      "\t\t\t\tCAUSTIC EVAPORATION HEAT BALANCE\n",
-      "\n",
-      "\t\t\t\t(Basis = 1ton/hr NaOH)\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t\tEFFECT\t\t\tBtu/hr\t\tEvaopration, lb/hr\n",
-      "\n",
-      "\t1.a.Heat in steam\t\thi\n",
-      "\t  b.Heating liquor\t\thl\n",
-      "\t  c.Resultant heat\t\trhf\n",
-      "\t  d.Heat of concentrate\t\thc\n",
-      "\t  e.Heat of vapors\t\thv\t%.0f\n",
-      "9511110.0 1452566.4 8058543.6 300000 7758543.6 7781.8892678\n",
-      "\n",
-      "\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\n",
-      "2430000.0\n",
-      "\tUD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t146\t2400000\t\t25.4\t700\t620\t0.80\t\t2790000\t\t700\n",
-      "\t146.5\t2160000\t\t25.2\t700\t683\t0.89\t\t2430000\n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.6\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "st1=274; #degreeF\n",
-    "vt6=115; #degreeF\n",
-    "odT=st1-vt6; #degreeF\n",
-    "print\"\\tTotal temperature difference =  degreeF\\n\",odT #corresponding to 35 psig\n",
-    "eb1=77;#degreeF, From fig.14.38\n",
-    "eb2=26;#degreeF, From fig.14.38\n",
-    "etd=odT-(eb1+eb2);#degreeF\n",
-    "print\"\\tThe effective temperature difference is  degreeF\\n\",etd\n",
-    "print\"\\n\\t\\t\\tCAUSTIC EVAPORATOR MATERIAL BALANCE\\n\"\n",
-    "#Basis: 1 ton/hr NaOH\n",
-    "print\"\\tCell liquour at 120degreeF \\t\\tWash at 80degreeF\\n\"\n",
-    "print\"\\t---------------------------------------------\\n\"\n",
-    "l1=2000;#Lb\n",
-    "l2=3800;#Lb\n",
-    "l3=17050;#Lb\n",
-    "lq=l1+l2+l3;#Lb\n",
-    "w1=340;#Lb\n",
-    "w2=1020;#Lb\n",
-    "w=w1+w2;#Lb\n",
-    "print\"\\t8.75 prcnt NaOH = l1\\n\\t16.6 prcnt NaCl = l2\\t\\t25 prcnt NaCl = w2\\n\",l1,l2,w1\n",
-    "print\"\\t74.65 prcnt H20 = l3\\t\\t75 prcnt H20 = w2\\n\",l3,w2\n",
-    "print\"\\tTotal cell liquor = lq\\tTotoal wash = w\\n\",lq,w\n",
-    "print\"\\n\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\t\\t\\tNaOH\\t\\tNaCl\\t\\tH20,Lb\\tTotal,Lb\\n\\t\\t\\t\\tprcnt\\tLb\\tprcnt\\tLb\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tOverall operation:\\n\\t  Cell liquor.......... 8.75\\t\",l1,l2,l3,lq\n",
-    "print\"\\t  Wash................. ....\\t....\\t25.00\\t\",w1,w2,w\n",
-    "wl1=l2+w1;#Lb\n",
-    "wl2=l3+w2;#Lb\n",
-    "wlt=lq+w;\n",
-    "print\"\\t  Total in............. ....\\t\",l1,wl1,wl2,wlt\n",
-    "prn=110;#Lb\n",
-    "prh=1890;#Lb\n",
-    "prt=4000;#Lb\n",
-    "print\"\\t  Product.............. 50.00\\t\",l1,prn,prh,prt\n",
-    "r1=wl1-prn;#Lb\n",
-    "r2=wl2-prh;#Lb\n",
-    "r3=wlt-prt;#Lb\n",
-    "gain=3200;#gpm\n",
-    "print\"\\t  Removed.............. ....\\t....\\t....\\t\\t%.0f\\t%.0f\\n\",r1,r2,r3\n",
-    "#Rest of the table is calculated similarily\n",
-    "print\"\\n\\t\\t\\t\\t\\tCAUSTIC EVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t--------------------\\t\\tFlash Tank\\n\\t\\t\\t\\t\\t\\I\\t\\tII\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam pressure, psi/in.Hg\\t30\\n\\t2.Steam temperature,degreeF\\t\\t274\\t\\t169\\n\\t3.delT,degreeF\\t\\t\\t28\\t\\t28\\n\\t4.Liquor temperature, degreeF\\t246\\t\\t141\\t\\t192\\n\\t5.BPR, degreeF\\t\\t\\t77\\t\\t26\\t\\t77\\n\\t6.Vapor temperature, degreeF\\t\\t169\\t\\t115\\t\\t115\\n\\t7.Lambda, Btu/lb\\t\\t997\\t\\t1027\\t\\t1027\\n\\t8.Feed, lb/hr\\t\\t\\t22788\\t\\t50602\\t\\t13367\\n\\t9.Product, lb/hr\\t\\t13367\\t\\t40352\\t\\t12813\\n\\t10.Evaporation,lb/hr\\t\\t9421\\t\\t10250\\t\\t554\\n\\t11.Heat flow, Btu/hr\\t\\t11890000\\t11020000\\n\\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\\t700\\n\\t13.A,ft**2\\t\\t\\t683\\t\\t683\\n\\t14.Tubes, OD, in. and BWG\\t1,16\\t\\t1,16\\n\\t15.Tube length, ft\\t\\t7\\t\\t7\\n\\t16.No. tubes\\t\\t\\t432\\t\\t432\\n\\t17.Circulating pump. gpm\\t3200 at 20 ft\\t3200 at 20ft\\t167 at 45 ft\\n\\t18.Apparent efficiency, prcnt\\t54\\t\\t64\\n\\t18.BHP\\t\\t\\t\\t38\\t\\t35\\t\\t8.2\\n\\t20.Motor,hp\\t\\t\\t40\\t\\t40\\t\\t10.0\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "V=8;\n",
-    "s=1.5;\n",
-    "G=V*s*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\\n\",G\n",
-    "UD=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Combining with a steam film coefficient of approximately 1500\n",
-    "print\"\\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t251\\t2970000\\t\\t25.4\\t700\\t670\\t0.87\\t\\t3420000\\n\\t252\\t2480000\\t\\t25.0\\t700\\t680\\t0.88\\t\\t2820000\\n\\t252.5\\t2290000\\t\\t24.7\\t700\\t685\\t0.89\\t\\t2570000\\t\\t700\\n\\t253\\t2120000\\t\\t24.5\\t700\\t695\\t0.90\\t\\t2520000\\n\"\n",
-    "print\"\\tThee gain per minute is gpm\\n\",gain\n",
-    "print\"\\n\\t\\t\\t\\tCAUSTIC EVAPORATION HEAT BALANCE\\n\"\n",
-    "print\"\\t\\t\\t\\t(Basis = 1ton/hr NaOH)\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\tEFFECT\\t\\t\\tBtu/hr\\t\\tEvaopration, lb/hr\\n\"\n",
-    "hi=10500*930*0.974;#Btu/hr\n",
-    "hl=18230*(246-150)*0.83;#Btu/hr\n",
-    "rh=hi-hl;#Btu/hr\n",
-    "hc=300000;#Btu/hr\n",
-    "hv=rh-hc;#Btu/hr\n",
-    "evv=hv/997;#lb/hr\n",
-    "print\"\\t1.a.Heat in steam\\t\\thi\\n\\t  b.Heating liquor\\t\\thl\\n\\t  c.Resultant heat\\t\\trhf\\n\\t  d.Heat of concentrate\\t\\thc\\n\\t  e.Heat of vapors\\t\\thv\\t%.0f\\n\",hi,hl,rh,hc,hv,evv\n",
-    "s1=1.35;\n",
-    "G1=V*s1*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\n\\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\\n\",G1\n",
-    "UD1=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Using thermal characteristics for this solution\n",
-    "print\"\\tUD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD1\n",
-    "#As for effect I:\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t146\\t2400000\\t\\t25.4\\t700\\t620\\t0.80\\t\\t2790000\\t\\t700\\n\\t146.5\\t2160000\\t\\t25.2\\t700\\t683\\t0.89\\t\\t2430000\\n\"\n",
-    "#end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.7 pgno:447"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.7\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tM1 =  lb\n",
-      "17900\n",
-      "\n",
-      "\t\t\t\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tEffects\t\t\t\t\tStraight triple effect\t\t\t\tThermocompression\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tSteam  flow, lb/hr\t\t22400\t\t\t\t\t\t17900\n",
-      "\tSteam pressure, psi in.Hg\t20\t\t9\t\t2\t\t20\t\t9\t\t2\n",
-      "\tSteam temp,degreeF\t\t\t258\t\t237\t\t217\t\t258\t\t237\t\t217\n",
-      "\ttdelT,degreeF\t\t\t20\t\t18\t\t22\t\t20\t\t18\t\t22\n",
-      "\tLiquor temp, degreeF\t\t\t238\t\t219\t\t195\t\t238\t\t219\t\t195\n",
-      "\tBPR, degreeF\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\tVapor temp, degreeF\t\t\t237\t\t217\t\t192\t\t237\t\t215\t\t192\n",
-      "\tVapor pressure, pis/in.Hg\t9\t\t2\t\t10\t\t9\t\t2\t\t10\n",
-      "\tLambda, Btu/lb\t\t\t954\t\t965\t\t983\t\t954\t\t965\t\t983\n",
-      "\tLiquor in, lb/hr\t\t100000\t\t79400\t\t56900\t\t109000\t\t70000\t\t52400\n",
-      "\tLiqour out, lb/hr\t\t79400\t\t56900\t\t33300\t\t70000\t\t52400\t\t33300\n",
-      "\tEvaporation,lb/hr\t\t20600\t\t22500\t\t23500\t\t30000\t\t17600\t\t19100\n",
-      "\tdegreeBrix(out)\t\t\t\t\t\t\t\t\t\t\t\t\t30\n",
-      "\tCondenser water, gpm\t\t\t\t455\t\t\t\t\t\t365\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\n",
-      "\t\t\t\tCondenser water = 455 gpm\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\t1.a.Heat in steam\t\n",
-      "\t20424320.0\n",
-      "b.Heating liquor\t\n",
-      "\t736000.0\n",
-      "c.Evaporation\t\t Evaporation/954\t\n",
-      "\t19688320.0 20637.6519916\n",
-      "d.Liquor to 2d =  79362.3480084\n",
-      "total evapouriation 66700\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.7\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "M2=14300;#From fig.14.43 and heat balance above\n",
-    "M1=32200-14300;#From fig.14.43 and heat balance above\n",
-    "print\"\\tM1 =  lb\\n\",M1\n",
-    "print\"\\n\\t\\t\\t\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tEffects\\t\\t\\t\\t\\tStraight triple effect\\t\\t\\t\\tThermocompression\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tSteam  flow, lb/hr\\t\\t22400\\t\\t\\t\\t\\t\\t17900\\n\\tSteam pressure, psi in.Hg\\t20\\t\\t9\\t\\t2\\t\\t20\\t\\t9\\t\\t2\\n\\tSteam temp,degreeF\\t\\t\\t258\\t\\t237\\t\\t217\\t\\t258\\t\\t237\\t\\t217\\n\\ttdelT,degreeF\\t\\t\\t20\\t\\t18\\t\\t22\\t\\t20\\t\\t18\\t\\t22\\n\\tLiquor temp, degreeF\\t\\t\\t238\\t\\t219\\t\\t195\\t\\t238\\t\\t219\\t\\t195\\n\\tBPR, degreeF\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\\tVapor temp, degreeF\\t\\t\\t237\\t\\t217\\t\\t192\\t\\t237\\t\\t215\\t\\t192\\n\\tVapor pressure, pis/in.Hg\\t9\\t\\t2\\t\\t10\\t\\t9\\t\\t2\\t\\t10\\n\\tLambda, Btu/lb\\t\\t\\t954\\t\\t965\\t\\t983\\t\\t954\\t\\t965\\t\\t983\\n\\tLiquor in, lb/hr\\t\\t100000\\t\\t79400\\t\\t56900\\t\\t109000\\t\\t70000\\t\\t52400\\n\\tLiqour out, lb/hr\\t\\t79400\\t\\t56900\\t\\t33300\\t\\t70000\\t\\t52400\\t\\t33300\\n\\tEvaporation,lb/hr\\t\\t20600\\t\\t22500\\t\\t23500\\t\\t30000\\t\\t17600\\t\\t19100\\n\\tdegreeBrix(out)\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t30\\n\\tCondenser water, gpm\\t\\t\\t\\t455\\t\\t\\t\\t\\t\\t365\\n\"\n",
-    "print\"\\n\\t\\t\\t\\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\\n\\t\\t\\t\\tCondenser water = 455 gpm\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "sf=22400;#lb/hr\n",
-    "lc=100000;#lb/hr\n",
-    "t1=238;#degreeF\n",
-    "t2=230;#degreeF\n",
-    "te=30000+17600+19100;\n",
-    "his=sf*940*0.97;#Btu/hr\n",
-    "hlq=lc*(t1-t2)*0.92;#Btu/hr\n",
-    "hd=his-hlq;#Btu/hr\n",
-    "eva=(hd)/954;#lb/hr\n",
-    "l2d=lc-eva;\n",
-    "print\"\\t1.a.Heat in steam\\t\\n\\t\" ,his \n",
-    "print\"b.Heating liquor\\t\\n\\t\",hlq\n",
-    "print\"c.Evaporation\\t\\t Evaporation/954\\t\\n\\t\",hd,eva  \n",
-    "print\"d.Liquor to 2d = \",l2d\n",
-    "print\"total evapouriation\",te\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_3.ipynb
deleted file mode 100755
index 6c6ad595..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_14_Evapouration_3.ipynb
+++ /dev/null
@@ -1,1114 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 14 : Evapouration"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.1 pgno:383"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tQevap is  Btu/hr\t9610000\n",
-      "\tQ300 degreeF is  Btu/hr\t9600500\n",
-      "\tTemperature head =  degree F\t74\n",
-      "\tOverall coefficient \t605.5\n",
-      "\tSurface required is  ft^2\t2144.75416788\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "t1 = 300; # degreeF\n",
-    "t2 = 226; #degree F\n",
-    "bs = 700; # Btu/((hr)(ft^2)(ddegree F))\n",
-    "#Heat Balance\n",
-    "Qv = 10000 * 961; # Btu/hr\n",
-    "print\"\\tQevap is  Btu/hr\\t\",Qv\n",
-    "Q3 = 10550 * 910; #Btu/hr\n",
-    "print\"\\tQ300 degreeF is  Btu/hr\\t\",Q3\n",
-    "\n",
-    "delT = t1-t2; # degree F\n",
-    "print\"\\tTemperature head =  degree F\\t\",delT\n",
-    "Ud = bs * 0.865;\n",
-    "print\"\\tOverall coefficient \\t\",Ud\n",
-    "A = Qv*10/(Ud * delT); #ft^2\n",
-    "print\"\\tSurface required is  ft^2\\t\",A#Wrong calculation in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.2 pgno:412"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\tTotal product is lb/hr\t10000.0\n",
-      "\tTotal evaporation is lb/hr\t40000.0\n",
-      "\tTotal temperature difference is del degree F\t119\n",
-      "\tAverage pressure difference is del psi/effect \t8.25\n",
-      "\t\t\t\t\t\tPressure, psia\t\t delP, psi \t Steam or vapor, degree F \t lambda, Btu/lb\t\tSteam chest, 1st effect \t 26.70 \t\t\t .... \t\t Ts = 244 \t\t ls = 949 \t\tSteam chest, 2nd effect \t 18.45 \t\t\t 8.25 \t\t t1 = 224 \t\t l1 = 961 \t\tSteam chest, 3rd effect \t 10.20(20.7 in. Hg) \t 8.25 \t\t t2 = 194 \t\t l1 = 981 \t\tVapor to condenser \t\t 1.95(26 in. Hg) \t 8.25 \t\t t2 = 125 \t\t l1 = 1022 \t\n",
-      "\t949*Ws + 50000*(100-224) = 961*w1\t\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\t\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\t\tw1+w2+w3 = 40000\t\n",
-      "\tSolving simultaneously\t\n",
-      "\tw1 = \t12400\n",
-      "\tw2 = \t13300\n",
-      "\tw3 = \t14300\n",
-      "\tW1-3 is \t40000\n",
-      "\tA1 is ft**2 \t1510\n",
-      "\tA2 is ft**2 \t1588\n",
-      "\tA3 is ft**2 \t1512\n",
-      "\tHeat to condenser is Btu/hr\t14614600\n",
-      "\tWater requirement is lb/hr\t417560\n",
-      "\t= gpm \t835\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "wf = 50000; #  lb/hr\n",
-    "sf = wf * 0.10; #  lb/hr\n",
-    "tp = sf/0.50; # lb/hr\n",
-    "print\"\\tTotal product is lb/hr\\t\",tp\n",
-    "te = wf - tp;\n",
-    "print\"\\tTotal evaporation is lb/hr\\t\",te\n",
-    "cf = 1.0;\n",
-    "tF = 100;  # degree F\n",
-    "T1 = 244; # degree F\n",
-    "T2 = 125; # degree F\n",
-    "U1=600; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U2=250; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "U3=125; # Btu/((hr)*(ft**2)*(degree F))\n",
-    "\n",
-    "T = T1-T2;\n",
-    "print\"\\tTotal temperature difference is del degree F\\t\",T\n",
-    "df = (26.70- 1.95)/3; # psi/effect\n",
-    "print\"\\tAverage pressure difference is del psi/effect \\t\",df\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\tPressure, psia\\t\\t delP, psi \\t Steam or vapor, degree F \\t lambda, Btu/lb\\t\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\t .... \\t\\t Ts = 244 \\t\\t ls = 949 \\t\\tSteam chest, 2nd effect \\t 18.45 \\t\\t\\t 8.25 \\t\\t t1 = 224 \\t\\t l1 = 961 \\t\\tSteam chest, 3rd effect \\t 10.20(20.7 in. Hg) \\t 8.25 \\t\\t t2 = 194 \\t\\t l1 = 981 \\t\\tVapor to condenser \\t\\t 1.95(26 in. Hg) \\t 8.25 \\t\\t t2 = 125 \\t\\t l1 = 1022 \\t\"\n",
-    "\n",
-    "print\"\\t949*Ws + 50000*(100-224) = 961*w1\\t\\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\\t\\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\\t\\tw1+w2+w3 = 40000\\t\"\n",
-    "print\"\\tSolving simultaneously\\t\"\n",
-    "w1=12400;\n",
-    "print\"\\tw1 = \\t\",w1\n",
-    "w2=13300;\n",
-    "print\"\\tw2 = \\t\",w2\n",
-    "w3=14300;\n",
-    "print\"\\tw3 = \\t\",w3\n",
-    "\n",
-    "Wt = w1+w2+w3;\n",
-    "print\"\\tW1-3 is \\t\",Wt\n",
-    "Ws = 19100;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "Ts = 244;\n",
-    "t1 = 224;\n",
-    "t2 = 194;\n",
-    "t3 = 125;\n",
-    "\n",
-    "A1 = (Ws * lms)/(U1*(Ts-t1)); #ft**2\n",
-    "print\"\\tA1 is ft**2 \\t\",A1\n",
-    "A2 = (w1*lm1)/(U2*(t1-t2)); #ft**2\n",
-    "print\"\\tA2 is ft**2 \\t\",A2\n",
-    "A3 = (w2 * lm2)/(U3*(t2-t3)); #ft**2\n",
-    "print\"\\tA3 is ft**2 \\t\",A3\n",
-    "\n",
-    "hc = w3 * lm3; # Btu/hr, WRONG CALCULATION IN TEXT BOOK\n",
-    "print\"\\tHeat to condenser is Btu/hr\\t\",hc\n",
-    "wr = hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement is lb/hr\\t\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t= gpm \\t\",wr1\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.3 pgno:414"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 14.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t981*w2 + 50000*(100-125) = 1022*w3\n",
-      "\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\n",
-      "\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\n",
-      "\tw1+w2+w3 = 40000\n",
-      "\n",
-      "\tSolving simultaneously\n",
-      "\n",
-      "\tw1-3 =  \n",
-      "40000\n",
-      "\tA1 is  ft**2\n",
-      "2010\n",
-      "\tA2 is  ft**2\n",
-      "2043\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tAverage surface is  ft**2\n",
-      "1700\n",
-      "\n",
-      "\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\n",
-      "5100\n",
-      "\tRecalculation\n",
-      "\n",
-      "\tA1 is  ft**2\n",
-      "0\n",
-      "\tA2 is  ft**2\n",
-      "0\n",
-      "\tA3 is  ft**2\n",
-      "1048\n",
-      "\tTs-t3 is  degreeF\n",
-      "119\n",
-      "\t\t\t\t\tPressure, psia\t\t Steam or vapor, degreeF \t lambda, Btu/lb\n",
-      "\tSteam chest, 1st effect \t 26.70 \t\t\tTs = 244 \t\t 949 \n",
-      "\tSteam chest, 2nd effect \t 16.0 \t\t\t t1 = 216 \t\t 968 \n",
-      "\tSteam chest, 3rd effect \t 16.4 in. Hg) \t\t t2 = 175 \t\t 992 \n",
-      "\tVapor to condenser \t\t 26 in. Hg \t\t t3 = 125 \t\t l1 = 1022 \n",
-      "\n",
-      "\tw1 is \n",
-      "15450\n",
-      "\tw2 is \n",
-      "13200\n",
-      "\tw3 is \n",
-      "11350\n",
-      "\tWs is \n",
-      "16850\n",
-      "\tHeat to condenser is  Btu/hr\n",
-      "11599700\n",
-      "\tWater requirement  lb/hr\n",
-      "331420\n",
-      "\t\t\t= gpm\n",
-      "662\n",
-      "\tEconomy, lb evaporation/lb steam \n",
-      "2\n",
-      "\t\t\t\tForward\t\tBackward\n",
-      "\tTotal steam, lb/hr\t19100\t\t16850\n",
-      "\tCooling water, gpm\t840\t\t664\n",
-      "\tTotal surface, ft**2\t4800\t\t4500\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 14.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Same conditions as example 14.2\n",
-    "U1 = 400; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U2 = 250; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "U3 = 175; #Btu/((hr)*(ft**2)*(degreeF))\n",
-    "\n",
-    "w1 = 50000; # lb/hr     From example 14.2\n",
-    "wt = 40000; # lb/hr     From example 14.2\n",
-    "cf = 1; # From example 14.2\n",
-    "\n",
-    "print\"\\t981*w2 + 50000*(100-125) = 1022*w3\\n\\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\\n\\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\\n\\tw1+w2+w3 = 40000\\n\"\n",
-    "print\"\\tSolving simultaneously\\n\"\n",
-    "w1 = 15950;\n",
-    "w2 = 12900;\n",
-    "w3 = 11150;\n",
-    "lms = 949;\n",
-    "lm1 = 961;\n",
-    "lm2 = 981;\n",
-    "lm3 = 1022;\n",
-    "\n",
-    "wt = w1+w2+w3;\n",
-    "print\"\\tw1-3 =  \\n\",wt\n",
-    "Ws = 16950;\n",
-    "A1 = (Ws*lms)/(U1*20); #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A1\n",
-    "A2 = (w1*lm1)/(U2*30); #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A2\n",
-    "A3 = (w2*lm2)/(U3*69); #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A3\n",
-    "\n",
-    "Avs = (A1 + A2 + A3)/3; #ft**2\n",
-    "print\"\\tAverage surface is  ft**2\\n\",Avs\n",
-    "Av1 = 3 * Avs; #ft**2\n",
-    "print\"\\n\\tWith a better distribution temperatures and pressure, Average surface is  %.0f ft**2\\n\",Av1\n",
-    "print\"\\tRecalculation\\n\"\n",
-    "Av2 = 1500; #ft**2, assume\n",
-    "dT1 = 28; #degreeF\n",
-    "A4 = (20/dT1)*A1; #ft**2\n",
-    "print\"\\tA1 is  ft**2\\n\",A4\n",
-    "dT2 = 41; #degreeF\n",
-    "A5  = (30/dT2)*A2; #ft**2\n",
-    "print\"\\tA2 is  ft**2\\n\",A5\n",
-    "dT3 = 50; #degreeF\n",
-    "A6 = (69/50)*A3; #ft**2\n",
-    "print\"\\tA3 is  ft**2\\n\",A6\n",
-    "del1 = 119; #degreeF\n",
-    "print\"\\tTs-t3 is  degreeF\\n\",del1\n",
-    "print\"\\t\\t\\t\\t\\tPressure, psia\\t\\t Steam or vapor, degreeF \\t lambda, Btu/lb\\n\\tSteam chest, 1st effect \\t 26.70 \\t\\t\\tTs = 244 \\t\\t 949 \\n\\tSteam chest, 2nd effect \\t 16.0 \\t\\t\\t t1 = 216 \\t\\t 968 \\n\\tSteam chest, 3rd effect \\t 16.4 in. Hg) \\t\\t t2 = 175 \\t\\t 992 \\n\\tVapor to condenser \\t\\t 26 in. Hg \\t\\t t3 = 125 \\t\\t l1 = 1022 \\n\"\n",
-    "\n",
-    "w1 = 15450; #Solving again for \n",
-    "print\"\\tw1 is \\n\",w1\n",
-    "w2 = 13200;\n",
-    "print\"\\tw2 is \\n\",w2\n",
-    "w3 = 11350;\n",
-    "print\"\\tw3 is \\n\",w3\n",
-    "Ws = 16850;\n",
-    "print\"\\tWs is \\n\",Ws\n",
-    "Hc = w3 * 1022;\n",
-    "print\"\\tHeat to condenser is  Btu/hr\\n\",Hc\n",
-    "wr = Hc/(120-85); #lb/hr\n",
-    "print\"\\tWater requirement  lb/hr\\n\",wr\n",
-    "wr1 = wr/500;\n",
-    "print\"\\t\\t\\t= gpm\\n\",wr1\n",
-    "ec = wt/Ws;\n",
-    "print\"\\tEconomy, lb evaporation/lb steam \\n\",ec\n",
-    "\n",
-    "#comparision of forward and backward feed\n",
-    "print\"\\t\\t\\t\\tForward\\t\\tBackward\\n\\tTotal steam, lb/hr\\t19100\\t\\t16850\\n\\tCooling water, gpm\\t840\\t\\t664\\n\\tTotal surface, ft**2\\t4800\\t\\t4500\"\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.4 pgno:418"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.4 \n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\n",
-      "\n",
-      "\tEffects\t\tWater evaporated(lb/(hr)*(ft**2))\n",
-      "\n",
-      "\t1\t\t14-16\n",
-      "\t2\t\t6-8\n",
-      "\t3\t\t5-6\n",
-      "\t4\t\t4-5\n",
-      "\t5\t\t3-4\n",
-      "\n",
-      "\n",
-      "\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam  flow, lb/hr\t\t42600\t\t38000\n",
-      "\t2.Steam pressure, psi/in.Hg\t30\t\t30\t\t15\t\t5\t\t4\t\t14.5\n",
-      "\n",
-      "\t3.Steam temp,degreeF\t\t\t274\t\t274\t\t250\t\t227\t\t205\t\t181\n",
-      "\n",
-      "\t4.delT,degreeF\t\t\t23\t\t23\t\t21\t\t20\t\t20\t\t27\n",
-      "\t5.Liquor temp, degreeF\t\t251\t\t251\t\t229\t\t207\t\t185\t\t164\n",
-      "\t6.BPR, degreeF\t\t\t1\t\t1\t\t2\t\t2\t\t4\t\t7\n",
-      "\t7.Vapor temp, degreeF\t\t250\t\t250\t\t227\t\t205\t\t181\t\t147\n",
-      "\t8.Vapor pressure, pis/in.Hg\t15\t\t15\t\t5\t\t4\t\t14.5\t\t23\n",
-      "\t9.Lambda, Btu/lb\t\t946\t\t946\t\t960\t\t975\t\t990\t\t1010\n",
-      "\t10.Liquor in, lb/hr\t\t229000\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\n",
-      "\t11.Liqour out, lb/hr\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\t\t49600\n",
-      "\t12.Evaporation,lb/hr\t\t38800\t\t36200\t\t36900\t\t29300\t\t23800\t\t14400\n",
-      "\t13.degreeBrix(out)\t\t\t15.7\t\t19.4\t\t25.5\t\t34.4\t\t46.5\t\t50.0\n",
-      "\t14.A,ft**2\t\t\t3500\t\t3500\t\t5000\t\t5000\t\t5000\t\t3500\n",
-      "\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\t478\t\t425\t\t310\t\t264\t\t219\t\t138\n",
-      "\t16.UD delT,Btu/(hr)*(ft**2)\t11000\t\t9780\t\t6520\t\t5270\t\t4390\t\t3740\n",
-      "\n",
-      "\tTotal temperature difference in the evaporator system =  degreeF\n",
-      "127\n",
-      "\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\n",
-      "16\n",
-      "\tTotal EFFECTIVE  temperature difference = degreeF\n",
-      "111\n",
-      "\n",
-      "\t\t\t\tSUGAR-JUICE HEATERS\n",
-      "\n",
-      "\tRaw-juice heaters\t\t\t\tClear=juice heaters\n",
-      "\t-----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr 229000 212 184 5834920.0\n",
-      "\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\n",
-      "229000 243 220 4792970.0\n",
-      "\tVapor temp. = 227degreeF\tdelT=26.6degreeF\t\tVapor temp. = 250degreeF\tdelT=15.8degreeF\n",
-      "\n",
-      "\tud1=.\t\t\t\t\t\tUD=ud2\n",
-      "231 243\n",
-      "\tSurface,A=A1 ft**2\t\t\t\tSurface,A=A2 ft**2\n",
-      "\n",
-      "949.601275917 1248.36432776\n",
-      "\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr 229000 184 144 8244000.0\n",
-      "\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\n",
-      "229000 220 200 4122000.0\n",
-      "\tVapor temp. = 205degreeF\tdelT=37.6degreeF\t\tVapor temp. = 227degreeF\tdelT=14.8degreeF\n",
-      "\n",
-      "\tUD=Ud3\t\t\t\t\t\tUD=Ud4\n",
-      "230 214\n",
-      "\tSurface,A=A3 ft**2\t\t\t\tSurface,A=A4 ft**2\n",
-      "\n",
-      "953.2839963 1301.46501642\n",
-      "\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr 229000 144 82 4122000.0\n",
-      "\t(Use 2 heaters at 1300 ft**2 each plus 1\n",
-      "\t\t\t\t\t\t\theater at 1300 ft**2 as spare)\n",
-      "\n",
-      "\tVapor temp. = 181degreeF\tdelT=62.2degreeF\n",
-      "\tSurface,A=\n",
-      "946.715663757\n",
-      "\t(Use 3 heaters at 100 ft**2\n",
-      "\teach plus 1 heater as spare)\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t----------------------------------------------------\n",
-      "\n",
-      "\t1A.Heat in steam........\n",
-      "38388138.0\n",
-      "\t   Heating liquor.......\n",
-      "\t\t\t\t%.3e\t.\n",
-      "1667120.0 36721018.0 38817.1437632\n",
-      "\t   Liqour to 1B\n",
-      "\t   =  lb/hr\n",
-      "190182.856237\n",
-      "\t1B.Heat in steam........\n",
-      "34979292.7593\n",
-      "\t   Heating liquor........\n",
-      "\t\t\t\t\n",
-      "0.0 34979292.7593 36975.9965744\n",
-      "\t   Liqour to 2d \n",
-      "\t   effect= lb/hr\n",
-      "153206.859662\n",
-      "\t\t\t\t\t\t\t\tLb/hr\n",
-      "\n",
-      "\t(a) Actual evaporation..................................\n",
-      "179400\n",
-      "\t(b) Equivalent evaporation from vapors of \n",
-      "\t    1st effect used for vaccum pans......................\n",
-      "145500\n",
-      "\t(c) Equivalent evaporation from 1st effect \n",
-      "\t    vapors used for clarified-juice heaters..............\n",
-      "19700\n",
-      "\t(d) Equivalent evaporation from 2d effect \n",
-      "\t    vapors used for clarified-and raw-juice heaters......\n",
-      "30600\n",
-      "\t(e) Equivalent evaporation from 3d effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "2.71828182846\n",
-      "\t(f) Equivalent evaporation from 4th effect \n",
-      "\t    vapors used for raw-juice heaters....................\n",
-      "13100\n",
-      "\t                                                        -----\n",
-      "\n",
-      "\t     Extrapolated evaporation............................\n",
-      "406200\n",
-      "\t\tEstimated steam quantity =  lb/hr\n",
-      "81240\n",
-      "\t\tActual steam required from final heat balance =  lb/hr\n",
-      "80600\n",
-      "\t\t\t\t\t\t\tError =  lb/hr\n",
-      "640\n",
-      "\tGallons per minute of Water required =  gpm 583\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.4 \\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "from math import e\n",
-    "#Assumed that 37500 lb/hr of 15 psig vapor is bled from the first effect for use in thevaccum pans\n",
-    "print\"\\n\\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\\n\"\n",
-    "print\"\\tEffects\\t\\tWater evaporated(lb/(hr)*(ft**2))\\n\"\n",
-    "print\"\\t1\\t\\t14-16\\n\\t2\\t\\t6-8\\n\\t3\\t\\t5-6\\n\\t4\\t\\t4-5\\n\\t5\\t\\t3-4\\n\"\n",
-    "print\"\\n\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t42600\\t\\t38000\\n\\t2.Steam pressure, psi/in.Hg\\t30\\t\\t30\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\n\"\n",
-    "print\"\\t3.Steam temp,degreeF\\t\\t\\t274\\t\\t274\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\n\"\n",
-    "print\"\\t4.delT,degreeF\\t\\t\\t23\\t\\t23\\t\\t21\\t\\t20\\t\\t20\\t\\t27\\n\\t5.Liquor temp, degreeF\\t\\t251\\t\\t251\\t\\t229\\t\\t207\\t\\t185\\t\\t164\\n\\t6.BPR, degreeF\\t\\t\\t1\\t\\t1\\t\\t2\\t\\t2\\t\\t4\\t\\t7\\n\\t7.Vapor temp, degreeF\\t\\t250\\t\\t250\\t\\t227\\t\\t205\\t\\t181\\t\\t147\\n\\t8.Vapor pressure, pis/in.Hg\\t15\\t\\t15\\t\\t5\\t\\t4\\t\\t14.5\\t\\t23\\n\\t9.Lambda, Btu/lb\\t\\t946\\t\\t946\\t\\t960\\t\\t975\\t\\t990\\t\\t1010\\n\\t10.Liquor in, lb/hr\\t\\t229000\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\n\\t11.Liqour out, lb/hr\\t\\t190200\\t\\t154000\\t\\t117100\\t\\t87800\\t\\t64000\\t\\t49600\\n\\t12.Evaporation,lb/hr\\t\\t38800\\t\\t36200\\t\\t36900\\t\\t29300\\t\\t23800\\t\\t14400\\n\\t13.degreeBrix(out)\\t\\t\\t15.7\\t\\t19.4\\t\\t25.5\\t\\t34.4\\t\\t46.5\\t\\t50.0\\n\\t14.A,ft**2\\t\\t\\t3500\\t\\t3500\\t\\t5000\\t\\t5000\\t\\t5000\\t\\t3500\\n\\t15.UD,Btu/(hr)*(ft**2)*(degreeF)\\t478\\t\\t425\\t\\t310\\t\\t264\\t\\t219\\t\\t138\\n\\t16.UD delT,Btu/(hr)*(ft**2)\\t11000\\t\\t9780\\t\\t6520\\t\\t5270\\t\\t4390\\t\\t3740\\n\"#BPR values from fig 14.34a\n",
-    "#Saturate vapor pressure above the liquour determined from Table 7\n",
-    "#Saturated steam pressure in the following effect determined from Table 7\n",
-    "\n",
-    "t1 = 274; #degreeF\n",
-    "t2 = 147; #degreeF\n",
-    "t = t1-t2; #degreeF\n",
-    "print\"\\tTotal temperature difference in the evaporator system =  degreeF\\n\",t\n",
-    "bpr1 = 1; #degreeF\n",
-    "bpr2 = 2; #degreeF\n",
-    "bpr3 = 2; #degreeF\n",
-    "bpr4 = 4; #degreeF\n",
-    "bpr5 = 7; #degreeF\n",
-    "bpr = bpr1 + bpr2 + bpr3 + bpr4 + bpr5; #degreeF\n",
-    "print\"\\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) =  degreeF\\n\",bpr\n",
-    "tf = t-bpr; #degreeF\n",
-    "print\"\\tTotal EFFECTIVE  temperature difference = degreeF\\n\",tf\n",
-    "lbh = 229000; #lb/hr\n",
-    "tp1=212; #degreeF\n",
-    "tp2=184; #degreeF\n",
-    "tp3=144; #degreeF\n",
-    "tp4=82; #degreeF\n",
-    "tj1=243; #degreeF\n",
-    "tj2=220; #degreeF\n",
-    "tj3=200; #degreeF\n",
-    "Ud1=231;\n",
-    "Ud2=243;\n",
-    "Ud3=230;\n",
-    "Ud4=214;\n",
-    "Ud5=217;\n",
-    "print\"\\n\\t\\t\\t\\tSUGAR-JUICE HEATERS\\n\"\n",
-    "print\"\\tRaw-juice heaters\\t\\t\\t\\tClear=juice heaters\\n\\t-----------------------------------------------------------------------------------------\\n\"\n",
-    "rj1=lbh*(tp1-tp2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tp1-tp2)(0.91) =  rj1 Btu/hr\",lbh,tp1,tp2,rj1\n",
-    "rj2=lbh*(tj1-tj2)*(0.91); #Btu/hr\n",
-    "print\"\\t1.lbh(tj1-tj2)(0.91) = rj2 Btu/hr\\n\",lbh,tj1,tj2,rj2\n",
-    "print\"\\tVapor temp. = 227degreeF\\tdelT=26.6degreeF\\t\\tVapor temp. = 250degreeF\\tdelT=15.8degreeF\\n\"\n",
-    "print\"\\tud1=.\\t\\t\\t\\t\\t\\tUD=ud2\\n\",Ud1,Ud2\n",
-    "A1=rj1/(26.6*Ud1);#ft**2\n",
-    "A2=rj2/(15.8*Ud2);#ft**2\n",
-    "print\"\\tSurface,A=A1 ft**2\\t\\t\\t\\tSurface,A=A2 ft**2\\n\\n\",A1,A2\n",
-    "\n",
-    "rj3=lbh*(tp2-tp3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp2-tp3)(0.91) = rj3 Btu/hr\",lbh,tp2,tp3,rj3\n",
-    "rj4=lbh*(tj2-tj3)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tj2-tj3)(0.91) = rj4 Btu/hr\\n\",lbh,tj2,tj3,rj4\n",
-    "print\"\\tVapor temp. = 205degreeF\\tdelT=37.6degreeF\\t\\tVapor temp. = 227degreeF\\tdelT=14.8degreeF\\n\"\n",
-    "print\"\\tUD=Ud3\\t\\t\\t\\t\\t\\tUD=Ud4\\n\",Ud3,Ud4\n",
-    "A3=rj3/(37.6*Ud3);#ft**2\n",
-    "A4=rj4/(14.8*Ud4);#ft**2\n",
-    "print\"\\tSurface,A=A3 ft**2\\t\\t\\t\\tSurface,A=A4 ft**2\\n\\n\",A3,A4\n",
-    "\n",
-    "rj5=lbh*(tp3-tp4)*(0.90);#Btu/hr\n",
-    "print\"\\t2.lbh(tp3-tp4)(0.91) = rj4 Btu/hr\",lbh,tp3,tp4,rj4\n",
-    "print\"\\t(Use 2 heaters at 1300 ft**2 each plus 1\\n\\t\\t\\t\\t\\t\\t\\theater at 1300 ft**2 as spare)\\n\"\n",
-    "A5=rj5/(62.2*Ud5);#ft**2\n",
-    "print\"\\tVapor temp. = 181degreeF\\tdelT=62.2degreeF\\n\\tSurface,A=\\n\",A5\n",
-    "print\"\\t(Use 3 heaters at 100 ft**2\\n\\teach plus 1 heater as spare)\\n\\n\"\n",
-    "\n",
-    "v1=42600;#lb/hr\n",
-    "tt1=251;#degreeF\n",
-    "print\"\\t\\t\\t\\tHEAT BALANCE\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t----------------------------------------------------\\n\"\n",
-    "hia=v1*929*0.97;#Btu/hr\n",
-    "print\"\\t1A.Heat in steam........\\n\",hia\n",
-    "hla=lbh*(tt1-tj1)*0.91;#Btu/hr\n",
-    "hh=hia-hla;#Btu/hr\n",
-    "lb1=946;#Btu/lb\n",
-    "dif=hh/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor.......\\n\\t\\t\\t\\t%.3e\\t.\\n\",hla,hh,dif\n",
-    "ltob=lbh-dif;#lb/hr\n",
-    "print\"\\t   Liqour to 1B\\n\\t   =  lb/hr\\n\",ltob\n",
-    "hia1=dif*929*0.97;#Btu/hr\n",
-    "print\"\\t1B.Heat in steam........\\n\",hia1\n",
-    "hla1=ltob*(tt1-tt1)*0.91;#Btu/hr\n",
-    "hh1=hia1;#Btu/hr\n",
-    "dif1=hh1/lb1;#lb/hr\n",
-    "print\"\\t   Heating liquor........\\n\\t\\t\\t\\t\\n\",hla1,hh1,dif1\n",
-    "dif2=ltob-dif1;#lb/hr\n",
-    "print\"\\t   Liqour to 2d \\n\\t   effect= lb/hr\\n\",dif2\n",
-    "#Similarily the values in the table are calculated\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\tLb/hr\\n\"\n",
-    "aa=179400;#lb/hr\n",
-    "bb=145500;#lb/hr\n",
-    "cc=19700;#lb/hr\n",
-    "dd=30600;#lb/hr\n",
-    "ee=17900;#lb/hr\n",
-    "ff=13100;#lb/hr\n",
-    "tto=aa+bb+cc+dd+ee+ff;#lb/hr\n",
-    "print\"\\t(a) Actual evaporation..................................\\n\",aa\n",
-    "print\"\\t(b) Equivalent evaporation from vapors of \\n\\t    1st effect used for vaccum pans......................\\n\",bb\n",
-    "print\"\\t(c) Equivalent evaporation from 1st effect \\n\\t    vapors used for clarified-juice heaters..............\\n\",cc\n",
-    "print\"\\t(d) Equivalent evaporation from 2d effect \\n\\t    vapors used for clarified-and raw-juice heaters......\\n\",dd\n",
-    "print\"\\t(e) Equivalent evaporation from 3d effect \\n\\t    vapors used for raw-juice heaters....................\\n\",e\n",
-    "print\"\\t(f) Equivalent evaporation from 4th effect \\n\\t    vapors used for raw-juice heaters....................\\n\",ff\n",
-    "print\"\\t                                                        -----\\n\"\n",
-    "print\"\\t     Extrapolated evaporation............................\\n\",tto\n",
-    "esq=tto/5;#lb/hr\n",
-    "print\"\\t\\tEstimated steam quantity =  lb/hr\\n\",esq\n",
-    "aesq=80600;#lb/hr\n",
-    "err = esq-aesq;#lb/hr\n",
-    "print\"\\t\\tActual steam required from final heat balance =  lb/hr\\n\",aesq\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\tError =  lb/hr\\n\",err\n",
-    "ta=15;\n",
-    "Q=14575000; #Btu/hr Total hourly evaporation\n",
-    "Gpm=Q/(500*(t2-tp4-ta));#From equation 14.4\n",
-    "print\"\\tGallons per minute of Water required =  gpm\",Gpm\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.5 pgno:427"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 9,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.5\t\n",
-      "\tapproximate values are mentioned in the book \t\n",
-      "\tOverall temperature difference =  deg F\t155\n",
-      "\tThe estimated total BPR =  degF\t[10 18 25 31 36 41]\n",
-      "\tEffective temperature difference = %.0f degF\t[145 137 130 124 119 114]\n",
-      "\t\t\t\t\tEVAPORATOR SUMMARY\t\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\tItem\t\t\t\t\t\t\t\t\tEffects\t\t\t\t\t\t----------------------------------------------------------------------------------------------\t\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\t\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\t\n",
-      "\t1.Steam  flow, lb/hr\t\t20000\t\t2.Steam pressure, psi/in.Hg\t35\t\t14.5\t\t4\t\t7\t\t16.5\t\t22\t\t3.Steam temp,degF\t\t\t280\t\t249\t\t224\t\t199\t\t174\t\t151\t\t4.delT,degF\t\t\t21\t\t17\t\t18\t\t19\t\t18\t\t21\t\t5.Liquor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t6.BPR, degF\t\t\t10\t\t8\t\t7\t\t6\t\t5\t\t5\t\t7.Vapor temp, degF\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\t\t8.Vapor pressure, pis/in.Hg\t14.5\t\t4\t\t7\t\t6\t\t5\t\t5\t\t9.Lambda, Btu/lb\t\t946\t\t962\t\t978\t\t994\t\t1008\t\t1022\t\t10.Liquor in, lb/hr\t\t73400\t\t88300\t\t101000\t\t113000\t\t72000\t\t72000\t\t11.Liqour out, lb/hr\t\t56200\t\t73400\t\t88300\t\t101100\t\t58300\t\t54700\t\t12.Evaporation,lb/hr\t\t17200\t\t14900\t\t12800\t\t11900\t\t13700\t\t17300\t\t13.Total solids, \t\t38.9\t\t29.8\t\t24.7\t\t21.6\t\t18.7\t\t20.0\t\t14.A,ft^2\t\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t15.UD,Btu/(hr)*(ft^2)*(degF)\t262\t\t295\t\t252\t\t251\t\t221\t\t221\t\t16.UD delT,Btu/(hr)*(ft^2)\t5510\t\t5000\t\t4530t\t\t4770\t\t3980\t\t4650\t\n",
-      "\t\tTotal amount of water evaporated = \t lb/hr\t[17200 32100 44900 56800 70500     0]\n",
-      "\tTheoretical amount of steam for a six-effect evaporator = \t lb/hr\t[ 2866  5350  7483  9466 11750     0]\n",
-      "\tSteam used for trail balance = \t lb/hr\t[  3822.22222222   7133.33333333   9977.77777778  12622.22222222\n",
-      "  15666.66666667      0.        ]\n",
-      "\tEstimate of the amount of evaporation in the first effect = \t lb/hr\t[  3295.9    6152.5    8605.45  10885.9   13512.5       0.  ]\n",
-      "\tEstimated discharge from second effect = \t lb/hr\t[ 59495.9   62352.5   64805.45  67085.9   69712.5   56200.  ]\n",
-      "\t\t\t\t\tHEAT BALANCE\t\n",
-      "\t\tCooling water at 60 degreeF = \t gpm\t710\n",
-      "\t--------------------------------------------------------\t\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\t\n",
-      "\t--------------------------------------------------------\t\n",
-      "\t1.a.Heat in steam \t\t17925600.0\n",
-      "\t  b.Heating liquor \t\t1625076.0\n",
-      "\t  c.Evaporation\t\t\t\t\t\t17230.9978858\n",
-      "\t  d.To flash tank\t2190591.08245\n",
-      "\t\t\t\t2239.86818247\n",
-      "\t  e.Flashed vapor=\t\t2239.86818247\n",
-      "\t  f.product \t53929.1339317\n",
-      "\t\t2.a.Heat in 1st vapors\t\t16300524.0\n",
-      "\t  b.Heating liqour\t\t1951430.0\n",
-      "\t  c.Evaporation= 14915.8981289\n",
-      "\t\t\t\t\t14915.8981289\n",
-      "\t  d.Liquor to 1b=\t\t73384.1018711\n",
-      "total hourly evapouration lb : 90000\n",
-      "economy is lb/lb : 4.5\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.5\\t\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\t\"\n",
-    "st1=280; #degF\n",
-    "vt6=125; #degF\n",
-    "odT=st1-vt6; #degF\n",
-    "print\"\\tOverall temperature difference =  deg F\\t\",odT #corresponding to 35 psig and 26 in. Hg\n",
-    "import numpy\n",
-    "bpr=numpy.array([10, 8, 7, 6, 5, 5])\n",
-    "#bpr(1)=10; #degF\n",
-    "#bpr(2)=8; #degF\n",
-    "#bpr(3)=7; #degF\n",
-    "#bpr(4)=6; #degF\n",
-    "#bpr(5)=5; #degF\n",
-    "#bpr(6)=5; #degF\n",
-    "i=1;\n",
-    "tbpr=numpy.array([0, 0, 0, 0, 0, 0]);\n",
-    "tbpr[0]=bpr[0];\n",
-    "while (i<6):\n",
-    "\n",
-    "    tbpr[i]=tbpr[i-1]+bpr[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\tThe estimated total BPR =  degF\\t\",tbpr #from fig. 14.36a\n",
-    "edT=odT-tbpr;\n",
-    "print\"\\tEffective temperature difference = %.0f degF\\t\",edT\n",
-    "print\"\\t\\t\\t\\t\\tEVAPORATOR SUMMARY\\t\\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\t\\t\\t\\t\\tEffects\\t\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\t\\t\\t\\t\\t\\t1A\\t\\t1B\\t\\t2\\t\\t3\\t\\t4\\t\\t5\\t\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\t\"\n",
-    "print\"\\t1.Steam  flow, lb/hr\\t\\t20000\\t\\t2.Steam pressure, psi/in.Hg\\t35\\t\\t14.5\\t\\t4\\t\\t7\\t\\t16.5\\t\\t22\\t\\t3.Steam temp,degF\\t\\t\\t280\\t\\t249\\t\\t224\\t\\t199\\t\\t174\\t\\t151\\t\\t4.delT,degF\\t\\t\\t21\\t\\t17\\t\\t18\\t\\t19\\t\\t18\\t\\t21\\t\\t5.Liquor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t6.BPR, degF\\t\\t\\t10\\t\\t8\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t7.Vapor temp, degF\\t\\t259\\t\\t232\\t\\t206\\t\\t180\\t\\t156\\t\\t130\\t\\t8.Vapor pressure, pis/in.Hg\\t14.5\\t\\t4\\t\\t7\\t\\t6\\t\\t5\\t\\t5\\t\\t9.Lambda, Btu/lb\\t\\t946\\t\\t962\\t\\t978\\t\\t994\\t\\t1008\\t\\t1022\\t\\t10.Liquor in, lb/hr\\t\\t73400\\t\\t88300\\t\\t101000\\t\\t113000\\t\\t72000\\t\\t72000\\t\\t11.Liqour out, lb/hr\\t\\t56200\\t\\t73400\\t\\t88300\\t\\t101100\\t\\t58300\\t\\t54700\\t\\t12.Evaporation,lb/hr\\t\\t17200\\t\\t14900\\t\\t12800\\t\\t11900\\t\\t13700\\t\\t17300\\t\\t13.Total solids, \\t\\t38.9\\t\\t29.8\\t\\t24.7\\t\\t21.6\\t\\t18.7\\t\\t20.0\\t\\t14.A,ft^2\\t\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t3250\\t\\t15.UD,Btu/(hr)*(ft^2)*(degF)\\t262\\t\\t295\\t\\t252\\t\\t251\\t\\t221\\t\\t221\\t\\t16.UD delT,Btu/(hr)*(ft^2)\\t5510\\t\\t5000\\t\\t4530t\\t\\t4770\\t\\t3980\\t\\t4650\\t\"#BPR values from fig 14.36a\n",
-    "#Specific-heat data are given in Fig. 14.36b\n",
-    "ev=numpy.array([17200, 14900, 12800, 11900, 13700, 17300]);\n",
-    "#ev(1)=17200; #lb/hr\n",
-    "#ev(2)=14900; #lb/hr\n",
-    "#ev(3)=12800; #lb/hr\n",
-    "#ev(4)=11900; #lb/hr\n",
-    "#ev(5)=13700; #lb/hr\n",
-    "#ev(6)=17300; #lb/hr\n",
-    "i=1;\n",
-    "tev =numpy.array([0, 0, 0, 0, 0, 0])\n",
-    "tev[0]=ev[0];\n",
-    "while (i<5):\n",
-    "    tev[i]= tev[i-1]+ev[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\tTotal amount of water evaporated = \\t lb/hr\\t\",tev\n",
-    "ttev=tev/6;#lb/hr\n",
-    "print\"\\tTheoretical amount of steam for a six-effect evaporator = \\t lb/hr\\t\",ttev\n",
-    "tev2=tev/(6*0.75); #lb/hr . order of 75 percent of theoretical\n",
-    "print\"\\tSteam used for trail balance = \\t lb/hr\\t\",tev2\n",
-    "lq=(tev/6);\n",
-    "lq=lq+(lq*0.15);\n",
-    "print\"\\tEstimate of the amount of evaporation in the first effect = \\t lb/hr\\t\",lq\n",
-    "lout6=54000;#lb/hr\n",
-    "lq2=lout6+lq+2200;#lb/hr\n",
-    "print\"\\tEstimated discharge from second effect = \\t lb/hr\\t\",lq2\n",
-    "print\"\\t\\t\\t\\t\\tHEAT BALANCE\\t\"\n",
-    "cw = 17750000/(500*(125-15-60)); #gpm, values from table 14.6\n",
-    "print\"\\t\\tCooling water at 60 degreeF = \\t gpm\\t\",cw\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\t\"\n",
-    "print\"\\t--------------------------------------------------------\\t\"\n",
-    "sf=20000;#lb/hr\n",
-    "lqi=73400;#lb/hr\n",
-    "the=90000;\n",
-    "lqi2=88300\n",
-    "lt1=259;#degreeF\n",
-    "lt2=232;#degreeF\n",
-    "lt3=206;#degreeF\n",
-    "ecn=90000./20000.;\n",
-    "ev=17200;#lb/hr\n",
-    "his=sf*924*0.97;#Btu/hr\n",
-    "print\"\\t1.a.Heat in steam \\t\\t\",his\n",
-    "hl=lqi*(lt1-lt2)*0.82;#Btu/hr\n",
-    "print\"\\t  b.Heating liquor \\t\\t\",hl\n",
-    "hh=his-hl;\n",
-    "ev1=(hh)/946;#lb/hr\n",
-    "print\"\\t  c.Evaporation\\t\\t\\t\\t\\t\\t\",ev1\n",
-    "dif=lqi-ev1;\n",
-    "tft=(dif)*(lt1-209)*0.78;\n",
-    "print\"\\t  d.To flash tank\\t\",tft\n",
-    "ev2=tft/978;#lb/hr\n",
-    "print\"\\t\\t\\t\\t\",ev2\n",
-    "print\"\\t  e.Flashed vapor=\\t\\t\",ev2\n",
-    "p=dif-ev2;\n",
-    "print\"\\t  f.product \\t\",p\n",
-    "print\"\\t\\t2.a.Heat in 1st vapors\\t\\t\",hh\n",
-    "hl2=lqi2*(lt2-lt3)*0.85;\n",
-    "print\"\\t  b.Heating liqour\\t\\t\",hl2\n",
-    "ev3=(hh-hl2)/962;\n",
-    "print\"\\t  c.Evaporation=\",ev3\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\t\",ev3\n",
-    "lto1=lqi2-ev3;\n",
-    "print\"\\t  d.Liquor to 1b=\\t\\t\",lto1\n",
-    "print\"total hourly evapouration lb :\",the\n",
-    "print\"economy is lb/lb :\",ecn\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.6 pgno:437"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.6\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tTotal temperature difference =  degreeF\n",
-      "159\n",
-      "\tThe effective temperature difference is  degreeF\n",
-      "56\n",
-      "\n",
-      "\t\t\tCAUSTIC EVAPORATOR MATERIAL BALANCE\n",
-      "\n",
-      "\tCell liquour at 120degreeF \t\tWash at 80degreeF\n",
-      "\n",
-      "\t---------------------------------------------\n",
-      "\n",
-      "\t8.75 prcnt NaOH = l1\n",
-      "\t16.6 prcnt NaCl = l2\t\t25 prcnt NaCl = w2\n",
-      "2000 3800 340\n",
-      "\t74.65 prcnt H20 = l3\t\t75 prcnt H20 = w2\n",
-      "17050 1020\n",
-      "\tTotal cell liquor = lq\tTotoal wash = w\n",
-      "22850 1360\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\t\t\t\tNaOH\t\tNaCl\t\tH20,Lb\tTotal,Lb\n",
-      "\t\t\t\tprcnt\tLb\tprcnt\tLb\n",
-      "\n",
-      "\t-------------------------------------------------------------------------\n",
-      "\n",
-      "\tOverall operation:\n",
-      "\t  Cell liquor.......... 8.75\t2000 3800 17050 22850\n",
-      "\t  Wash................. ....\t....\t25.00\t340 1020 1360\n",
-      "\t  Total in............. ....\t2000 4140 18070 24210\n",
-      "\t  Product.............. 50.00\t2000 110 1890 4000\n",
-      "\t  Removed.............. ....\t....\t....\t\t%.0f\t%.0f\n",
-      "4030 16180 20210\n",
-      "\n",
-      "\t\t\t\t\tCAUSTIC EVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tItem\t\t\t\t\tEffects\n",
-      "t\t\t\t\t\t--------------------\t\tFlash Tank\n",
-      "\t\t\t\t\t\\I\t\tII\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t1.Steam pressure, psi/in.Hg\t30\n",
-      "\t2.Steam temperature,degreeF\t\t274\t\t169\n",
-      "\t3.delT,degreeF\t\t\t28\t\t28\n",
-      "\t4.Liquor temperature, degreeF\t246\t\t141\t\t192\n",
-      "\t5.BPR, degreeF\t\t\t77\t\t26\t\t77\n",
-      "\t6.Vapor temperature, degreeF\t\t169\t\t115\t\t115\n",
-      "\t7.Lambda, Btu/lb\t\t997\t\t1027\t\t1027\n",
-      "\t8.Feed, lb/hr\t\t\t22788\t\t50602\t\t13367\n",
-      "\t9.Product, lb/hr\t\t13367\t\t40352\t\t12813\n",
-      "\t10.Evaporation,lb/hr\t\t9421\t\t10250\t\t554\n",
-      "\t11.Heat flow, Btu/hr\t\t11890000\t11020000\n",
-      "\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\t700\n",
-      "\t13.A,ft**2\t\t\t683\t\t683\n",
-      "\t14.Tubes, OD, in. and BWG\t1,16\t\t1,16\n",
-      "\t15.Tube length, ft\t\t7\t\t7\n",
-      "\t16.No. tubes\t\t\t432\t\t432\n",
-      "\t17.Circulating pump. gpm\t3200 at 20 ft\t3200 at 20ft\t167 at 45 ft\n",
-      "\t18.Apparent efficiency, prcnt\t54\t\t64\n",
-      "\t18.BHP\t\t\t\t38\t\t35\t\t8.2\n",
-      "\t20.Motor,hp\t\t\t40\t\t40\t\t10.0\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\n",
-      "2700000.0\n",
-      "\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t251\t2970000\t\t25.4\t700\t670\t0.87\t\t3420000\n",
-      "\t252\t2480000\t\t25.0\t700\t680\t0.88\t\t2820000\n",
-      "\t252.5\t2290000\t\t24.7\t700\t685\t0.89\t\t2570000\t\t700\n",
-      "\t253\t2120000\t\t24.5\t700\t695\t0.90\t\t2520000\n",
-      "\n",
-      "\tThee gain per minute is gpm\n",
-      "3200\n",
-      "\n",
-      "\t\t\t\tCAUSTIC EVAPORATION HEAT BALANCE\n",
-      "\n",
-      "\t\t\t\t(Basis = 1ton/hr NaOH)\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t\tEFFECT\t\t\tBtu/hr\t\tEvaopration, lb/hr\n",
-      "\n",
-      "\t1.a.Heat in steam\t\thi\n",
-      "\t  b.Heating liquor\t\thl\n",
-      "\t  c.Resultant heat\t\trhf\n",
-      "\t  d.Heat of concentrate\t\thc\n",
-      "\t  e.Heat of vapors\t\thv\t%.0f\n",
-      "9511110.0 1452566.4 8058543.6 300000 7758543.6 7781.8892678\n",
-      "\n",
-      "\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\n",
-      "2430000.0\n",
-      "\tUD =  Btu/((hr)*(ft**2)*(degreeF))\n",
-      "700\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\ttx,degreeF\tw,lb/hr\t\tdelT\tUC\tA,ft**2\tat,flow area\tGcalc\t\tUcalc\n",
-      "\t\t\t\t\t\t\tper pass, ft**2\n",
-      "\n",
-      "\t-------------------------------------------------------------------------------------\n",
-      "\n",
-      "\t146\t2400000\t\t25.4\t700\t620\t0.80\t\t2790000\t\t700\n",
-      "\t146.5\t2160000\t\t25.2\t700\t683\t0.89\t\t2430000\n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.6\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "st1=274; #degreeF\n",
-    "vt6=115; #degreeF\n",
-    "odT=st1-vt6; #degreeF\n",
-    "print\"\\tTotal temperature difference =  degreeF\\n\",odT #corresponding to 35 psig\n",
-    "eb1=77;#degreeF, From fig.14.38\n",
-    "eb2=26;#degreeF, From fig.14.38\n",
-    "etd=odT-(eb1+eb2);#degreeF\n",
-    "print\"\\tThe effective temperature difference is  degreeF\\n\",etd\n",
-    "print\"\\n\\t\\t\\tCAUSTIC EVAPORATOR MATERIAL BALANCE\\n\"\n",
-    "#Basis: 1 ton/hr NaOH\n",
-    "print\"\\tCell liquour at 120degreeF \\t\\tWash at 80degreeF\\n\"\n",
-    "print\"\\t---------------------------------------------\\n\"\n",
-    "l1=2000;#Lb\n",
-    "l2=3800;#Lb\n",
-    "l3=17050;#Lb\n",
-    "lq=l1+l2+l3;#Lb\n",
-    "w1=340;#Lb\n",
-    "w2=1020;#Lb\n",
-    "w=w1+w2;#Lb\n",
-    "print\"\\t8.75 prcnt NaOH = l1\\n\\t16.6 prcnt NaCl = l2\\t\\t25 prcnt NaCl = w2\\n\",l1,l2,w1\n",
-    "print\"\\t74.65 prcnt H20 = l3\\t\\t75 prcnt H20 = w2\\n\",l3,w2\n",
-    "print\"\\tTotal cell liquor = lq\\tTotoal wash = w\\n\",lq,w\n",
-    "print\"\\n\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\t\\t\\tNaOH\\t\\tNaCl\\t\\tH20,Lb\\tTotal,Lb\\n\\t\\t\\t\\tprcnt\\tLb\\tprcnt\\tLb\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tOverall operation:\\n\\t  Cell liquor.......... 8.75\\t\",l1,l2,l3,lq\n",
-    "print\"\\t  Wash................. ....\\t....\\t25.00\\t\",w1,w2,w\n",
-    "wl1=l2+w1;#Lb\n",
-    "wl2=l3+w2;#Lb\n",
-    "wlt=lq+w;\n",
-    "print\"\\t  Total in............. ....\\t\",l1,wl1,wl2,wlt\n",
-    "prn=110;#Lb\n",
-    "prh=1890;#Lb\n",
-    "prt=4000;#Lb\n",
-    "print\"\\t  Product.............. 50.00\\t\",l1,prn,prh,prt\n",
-    "r1=wl1-prn;#Lb\n",
-    "r2=wl2-prh;#Lb\n",
-    "r3=wlt-prt;#Lb\n",
-    "gain=3200;#gpm\n",
-    "print\"\\t  Removed.............. ....\\t....\\t....\\t\\t%.0f\\t%.0f\\n\",r1,r2,r3\n",
-    "#Rest of the table is calculated similarily\n",
-    "print\"\\n\\t\\t\\t\\t\\tCAUSTIC EVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tItem\\t\\t\\t\\t\\tEffects\\nt\\t\\t\\t\\t\\t--------------------\\t\\tFlash Tank\\n\\t\\t\\t\\t\\t\\I\\t\\tII\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t1.Steam pressure, psi/in.Hg\\t30\\n\\t2.Steam temperature,degreeF\\t\\t274\\t\\t169\\n\\t3.delT,degreeF\\t\\t\\t28\\t\\t28\\n\\t4.Liquor temperature, degreeF\\t246\\t\\t141\\t\\t192\\n\\t5.BPR, degreeF\\t\\t\\t77\\t\\t26\\t\\t77\\n\\t6.Vapor temperature, degreeF\\t\\t169\\t\\t115\\t\\t115\\n\\t7.Lambda, Btu/lb\\t\\t997\\t\\t1027\\t\\t1027\\n\\t8.Feed, lb/hr\\t\\t\\t22788\\t\\t50602\\t\\t13367\\n\\t9.Product, lb/hr\\t\\t13367\\t\\t40352\\t\\t12813\\n\\t10.Evaporation,lb/hr\\t\\t9421\\t\\t10250\\t\\t554\\n\\t11.Heat flow, Btu/hr\\t\\t11890000\\t11020000\\n\\t12.UD,Btu/((hr)*(ft**2)*(degreeF))\\t700\\n\\t13.A,ft**2\\t\\t\\t683\\t\\t683\\n\\t14.Tubes, OD, in. and BWG\\t1,16\\t\\t1,16\\n\\t15.Tube length, ft\\t\\t7\\t\\t7\\n\\t16.No. tubes\\t\\t\\t432\\t\\t432\\n\\t17.Circulating pump. gpm\\t3200 at 20 ft\\t3200 at 20ft\\t167 at 45 ft\\n\\t18.Apparent efficiency, prcnt\\t54\\t\\t64\\n\\t18.BHP\\t\\t\\t\\t38\\t\\t35\\t\\t8.2\\n\\t20.Motor,hp\\t\\t\\t40\\t\\t40\\t\\t10.0\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------\\n\"\n",
-    "V=8;\n",
-    "s=1.5;\n",
-    "G=V*s*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\tG = V(s*62.5*3600) = lb/((hr)*(ft**2))\\n\",G\n",
-    "UD=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Combining with a steam film coefficient of approximately 1500\n",
-    "print\"\\tUC or UD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t251\\t2970000\\t\\t25.4\\t700\\t670\\t0.87\\t\\t3420000\\n\\t252\\t2480000\\t\\t25.0\\t700\\t680\\t0.88\\t\\t2820000\\n\\t252.5\\t2290000\\t\\t24.7\\t700\\t685\\t0.89\\t\\t2570000\\t\\t700\\n\\t253\\t2120000\\t\\t24.5\\t700\\t695\\t0.90\\t\\t2520000\\n\"\n",
-    "print\"\\tThee gain per minute is gpm\\n\",gain\n",
-    "print\"\\n\\t\\t\\t\\tCAUSTIC EVAPORATION HEAT BALANCE\\n\"\n",
-    "print\"\\t\\t\\t\\t(Basis = 1ton/hr NaOH)\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t\\tEFFECT\\t\\t\\tBtu/hr\\t\\tEvaopration, lb/hr\\n\"\n",
-    "hi=10500*930*0.974;#Btu/hr\n",
-    "hl=18230*(246-150)*0.83;#Btu/hr\n",
-    "rh=hi-hl;#Btu/hr\n",
-    "hc=300000;#Btu/hr\n",
-    "hv=rh-hc;#Btu/hr\n",
-    "evv=hv/997;#lb/hr\n",
-    "print\"\\t1.a.Heat in steam\\t\\thi\\n\\t  b.Heating liquor\\t\\thl\\n\\t  c.Resultant heat\\t\\trhf\\n\\t  d.Heat of concentrate\\t\\thc\\n\\t  e.Heat of vapors\\t\\thv\\t%.0f\\n\",hi,hl,rh,hc,hv,evv\n",
-    "s1=1.35;\n",
-    "G1=V*s1*62.5*3600;#lb/((hr)*(ft**2))\n",
-    "print\"\\n\\tG = V(s*62.5*3600) =  lb/((hr)*(ft**2))\\n\",G1\n",
-    "UD1=700;#Btu/((hr)*(ft**2)*(degreeF))\n",
-    "#Using thermal characteristics for this solution\n",
-    "print\"\\tUD =  Btu/((hr)*(ft**2)*(degreeF))\\n\",UD1\n",
-    "#As for effect I:\n",
-    "print\"\\n\\t-------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\ttx,degreeF\\tw,lb/hr\\t\\tdelT\\tUC\\tA,ft**2\\tat,flow area\\tGcalc\\t\\tUcalc\\n\\t\\t\\t\\t\\t\\t\\tper pass, ft**2\\n\"\n",
-    "print\"\\t-------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\t146\\t2400000\\t\\t25.4\\t700\\t620\\t0.80\\t\\t2790000\\t\\t700\\n\\t146.5\\t2160000\\t\\t25.2\\t700\\t683\\t0.89\\t\\t2430000\\n\"\n",
-    "#end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 14.7 pgno:447"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\texample 14.7\n",
-      "\n",
-      "\tapproximate values are mentioned in the book \n",
-      "\n",
-      "\tM1 =  lb\n",
-      "17900\n",
-      "\n",
-      "\t\t\t\tEVAPORATOR SUMMARY\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tEffects\t\t\t\t\tStraight triple effect\t\t\t\tThermocompression\n",
-      "t\t\t\t\t\t----------------------------------------------------------------------------------------------\n",
-      "\t\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\n",
-      "\t------------------------------------------------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tSteam  flow, lb/hr\t\t22400\t\t\t\t\t\t17900\n",
-      "\tSteam pressure, psi in.Hg\t20\t\t9\t\t2\t\t20\t\t9\t\t2\n",
-      "\tSteam temp,degreeF\t\t\t258\t\t237\t\t217\t\t258\t\t237\t\t217\n",
-      "\ttdelT,degreeF\t\t\t20\t\t18\t\t22\t\t20\t\t18\t\t22\n",
-      "\tLiquor temp, degreeF\t\t\t238\t\t219\t\t195\t\t238\t\t219\t\t195\n",
-      "\tBPR, degreeF\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n",
-      "\tVapor temp, degreeF\t\t\t237\t\t217\t\t192\t\t237\t\t215\t\t192\n",
-      "\tVapor pressure, pis/in.Hg\t9\t\t2\t\t10\t\t9\t\t2\t\t10\n",
-      "\tLambda, Btu/lb\t\t\t954\t\t965\t\t983\t\t954\t\t965\t\t983\n",
-      "\tLiquor in, lb/hr\t\t100000\t\t79400\t\t56900\t\t109000\t\t70000\t\t52400\n",
-      "\tLiqour out, lb/hr\t\t79400\t\t56900\t\t33300\t\t70000\t\t52400\t\t33300\n",
-      "\tEvaporation,lb/hr\t\t20600\t\t22500\t\t23500\t\t30000\t\t17600\t\t19100\n",
-      "\tdegreeBrix(out)\t\t\t\t\t\t\t\t\t\t\t\t\t30\n",
-      "\tCondenser water, gpm\t\t\t\t455\t\t\t\t\t\t365\n",
-      "\n",
-      "\n",
-      "\t\t\t\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\n",
-      "\t\t\t\tCondenser water = 455 gpm\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n",
-      "\n",
-      "\t--------------------------------------------------------\n",
-      "\n",
-      "\t1.a.Heat in steam\t\n",
-      "\t20424320.0\n",
-      "b.Heating liquor\t\n",
-      "\t736000.0\n",
-      "c.Evaporation\t\t Evaporation/954\t\n",
-      "\t19688320.0 20637.6519916\n",
-      "d.Liquor to 2d =  79362.3480084\n",
-      "total evapouriation 66700\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\texample 14.7\\n\"\n",
-    "print\"\\tapproximate values are mentioned in the book \\n\"\n",
-    "M2=14300;#From fig.14.43 and heat balance above\n",
-    "M1=32200-14300;#From fig.14.43 and heat balance above\n",
-    "print\"\\tM1 =  lb\\n\",M1\n",
-    "print\"\\n\\t\\t\\t\\tEVAPORATOR SUMMARY\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tEffects\\t\\t\\t\\t\\tStraight triple effect\\t\\t\\t\\tThermocompression\\nt\\t\\t\\t\\t\\t----------------------------------------------------------------------------------------------\\n\\t\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\"\n",
-    "print\"\\t------------------------------------------------------------------------------------------------------------------------------\\n\"\n",
-    "print\"\\tSteam  flow, lb/hr\\t\\t22400\\t\\t\\t\\t\\t\\t17900\\n\\tSteam pressure, psi in.Hg\\t20\\t\\t9\\t\\t2\\t\\t20\\t\\t9\\t\\t2\\n\\tSteam temp,degreeF\\t\\t\\t258\\t\\t237\\t\\t217\\t\\t258\\t\\t237\\t\\t217\\n\\ttdelT,degreeF\\t\\t\\t20\\t\\t18\\t\\t22\\t\\t20\\t\\t18\\t\\t22\\n\\tLiquor temp, degreeF\\t\\t\\t238\\t\\t219\\t\\t195\\t\\t238\\t\\t219\\t\\t195\\n\\tBPR, degreeF\\t\\t\\t\\t1\\t\\t2\\t\\t3\\t\\t1\\t\\t2\\t\\t3\\n\\tVapor temp, degreeF\\t\\t\\t237\\t\\t217\\t\\t192\\t\\t237\\t\\t215\\t\\t192\\n\\tVapor pressure, pis/in.Hg\\t9\\t\\t2\\t\\t10\\t\\t9\\t\\t2\\t\\t10\\n\\tLambda, Btu/lb\\t\\t\\t954\\t\\t965\\t\\t983\\t\\t954\\t\\t965\\t\\t983\\n\\tLiquor in, lb/hr\\t\\t100000\\t\\t79400\\t\\t56900\\t\\t109000\\t\\t70000\\t\\t52400\\n\\tLiqour out, lb/hr\\t\\t79400\\t\\t56900\\t\\t33300\\t\\t70000\\t\\t52400\\t\\t33300\\n\\tEvaporation,lb/hr\\t\\t20600\\t\\t22500\\t\\t23500\\t\\t30000\\t\\t17600\\t\\t19100\\n\\tdegreeBrix(out)\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t30\\n\\tCondenser water, gpm\\t\\t\\t\\t455\\t\\t\\t\\t\\t\\t365\\n\"\n",
-    "print\"\\n\\t\\t\\t\\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\\n\\t\\t\\t\\tCondenser water = 455 gpm\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "print\"\\tEffect\\t\\t\\tBtu/hr\\t\\tEvaporation,l/hr\\n\"\n",
-    "print\"\\t--------------------------------------------------------\\n\"\n",
-    "sf=22400;#lb/hr\n",
-    "lc=100000;#lb/hr\n",
-    "t1=238;#degreeF\n",
-    "t2=230;#degreeF\n",
-    "te=30000+17600+19100;\n",
-    "his=sf*940*0.97;#Btu/hr\n",
-    "hlq=lc*(t1-t2)*0.92;#Btu/hr\n",
-    "hd=his-hlq;#Btu/hr\n",
-    "eva=(hd)/954;#lb/hr\n",
-    "l2d=lc-eva;\n",
-    "print\"\\t1.a.Heat in steam\\t\\n\\t\" ,his \n",
-    "print\"b.Heating liquor\\t\\n\\t\",hlq\n",
-    "print\"c.Evaporation\\t\\t Evaporation/954\\t\\n\\t\",hd,eva  \n",
-    "print\"d.Liquor to 2d = \",l2d\n",
-    "print\"total evapouriation\",te\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers.ipynb
deleted file mode 100755
index 4b0ddf56..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers.ipynb
+++ /dev/null
@@ -1,1324 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 15 : Vaporizers Evapourators and Reboilers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.1 pgno:463"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9453000.0\n",
-      "\t total heat required for kerosene is :  Btu/hr \t9450000.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t91.1262293169\n",
-      "\t A :  ft**2 \t1037.02304713\n",
-      "\t By the law of mixtures \t\n",
-      "\t v2 : %.0f ft**3/lb \t11.0034\n",
-      "\t vav :  ft**3/lb \t3.16417120715\n",
-      "\t By the approximate method \t\n",
-      "\t vav :  ft**3/lb \t5.5102\n",
-      "\t actual density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.00505661639416\n",
-      "\t approximate density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.0029\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=250;\n",
-    "T1=400;\n",
-    "T2=300;\n",
-    "w=10000; # lb/hr\n",
-    "W=150000; # lb/hr\n",
-    "l=945.3; # Btu/(lb) , table 7\n",
-    "from math import log10\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "C=0.63; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-ts; #F\n",
-    "delt2=T1-ts; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "UD=100;\n",
-    "A=(Q/(UD*LMTD));\n",
-    "print\"\\t A :  ft**2 \\t\",A\n",
-    "WC=94500; # Btu/F\n",
-    "vl=0.017; # ft**3/lb, from table 7\n",
-    "vv=13.75; # ft**3/lb, from table 7\n",
-    "print\"\\t By the law of mixtures \\t\"\n",
-    "# Assume 80 per cent of the outlet fluid is vapor\n",
-    "v2=(0.8*vv)+(.2*vl);\n",
-    "print\"\\t v2 : ft**3/lb \\t\",v2\n",
-    "vav=(WC*(v2-vl)/(UD*A))-((WC*(T2-ts)/(l*w))*(vv-vl))+vl;\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav\n",
-    "print\"\\t By the approximate method \\t\"\n",
-    "vav1=(vl+v2)/(2);\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav1\n",
-    "row=62.5;\n",
-    "rowac=(1/vav);\n",
-    "s=(rowac/row);\n",
-    "print\"\\t actual density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",s\n",
-    "rowap=(1/vav1);\n",
-    "s=(rowap/row);\n",
-    "print\"\\t approximate density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",round(s,4)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.2 pgno:464"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for preheat of butane is :  Btu/hr \t2124200\n",
-      "\t total heat required for vapourisation of butane is :  Btu/hr \t2172500\n",
-      "\t total heat required for  butane is :  Btu/hr \t4296700\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t4297328.0\n",
-      "\t Wp1 is :  lb/hr \t13401.8927445\n",
-      "\t Wv1 is :  lb/hr \t21092\n",
-      "\t W is :  lb/hr \t34493.8927445\n",
-      "\t weighted delt is : % F \t124.582285677\n",
-      "\t caloric temperature of hot fluid is :  F \t338\n",
-      "\t caloric temperature of cold fluid is :  F \t171\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.15675\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t31132.3763955\n",
-      "\t reynolds number is :  \t62178.9886688\n",
-      "\t hio is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,butane \t\n",
-      "\t preheating \t\n",
-      "\t flow area is :  ft**2 \t0.105902777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t233232.786885\n",
-      "\t reynolds number is :  \t69214.7658922\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t231.272727273\n",
-      "\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \t200.378071834\n",
-      "\t clean surface required for preheating :  ft**2 \t66.883030772\n",
-      "\t for vapourisation \t\n",
-      "\t reynolds number is :  \t79511.1773472\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t236.96969697\n",
-      "\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \t204.640614096\n",
-      "\t clean surface required for vapourisation :  ft**2 \t103.069633088\n",
-      "\t total clean surface :  ft**2 \t169.952663859\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t202.96313674\n",
-      "\t total surface area is :  ft**2 \t318.3488\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.352513798\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00430213212754\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.16\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t preheating \t\n",
-      "\t length of preheat zone :  ft \t6.29662676683\n",
-      "\t number of crosses are :  \t15.1119042404\n",
-      "\t delPsp is :  psi \t0.703032923143\n",
-      "\t vapourisation \t\n",
-      "\t number of crosses are :  \t23.28\n",
-      "\t delPsv is :  psi \t1.89396418309\n",
-      "\t delPS is :  psi \t2.6\n",
-      "\t allowable delPa is 5 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=108; # inlet cold fluid,F\n",
-    "t2=235; # outlet cold fluid,F\n",
-    "Ts=338;\n",
-    "Wp=24700; # lb/hr\n",
-    "Wv=19750; # lb/hr\n",
-    "w=4880; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=162; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=248; # enthalpy at t2, Btu/lb, fig 9\n",
-    "qp=(Wp*(Ht2-Ht1)); # for preheat\n",
-    "print\"\\t total heat required for preheat of butane is :  Btu/hr \\t\",qp\n",
-    "Ht3=358; # enthalpy of vapour at t2, Btu/lb, fig 9\n",
-    "qv=Wv*(Ht3-Ht2);\n",
-    "print\"\\t total heat required for vapourisation of butane is :  Btu/hr \\t\",qv\n",
-    "Q=qp+qv;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=880.6; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "deltp=158.5; # F, from eq 5.14\n",
-    "deltv=103; # F eq 5.14\n",
-    "Wp1=(qp/deltp);\n",
-    "print\"\\t Wp1 is :  lb/hr \\t\",Wp1\n",
-    "Wv1=(qv/deltv);\n",
-    "print\"\\t Wv1 is :  lb/hr \\t\",Wv1\n",
-    "W=(Wp1+Wv1);\n",
-    "print\"\\t W is :  lb/hr \\t\",W\n",
-    "delt=(Q/W);\n",
-    "print\"\\t weighted delt is : % F \\t\",delt\n",
-    "Tc=((Ts)+(Ts))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=76;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.594; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.0363; # at 338F, fig 15,lb/(ft)*(hr)\n",
-    "D=0.0725; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensing steam,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hio is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,butane \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(Wp/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.278; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0825; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=159; # from fig.28\n",
-    "Z=0.12; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hop=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hop\n",
-    "Up=((hio)*(hop)/(hio+hop)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \\t\",Up\n",
-    "Ap=(qp/(Up*deltp));\n",
-    "print\"\\t clean surface required for preheating :  ft**2 \\t\",Ap\n",
-    "print\"\\t for vapourisation \\t\"\n",
-    "mu2=0.242; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=170; # from fig.28\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hov=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hov\n",
-    "Uv=((hio)*(hov)/(hio+hov)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \\t\",Uv\n",
-    "Av=(qv/(Uv*deltv));\n",
-    "print\"\\t clean surface required for vapourisation :  ft**2 \\t\",Av\n",
-    "Ac=Ap+Av;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",Ac\n",
-    "UC=((Up*Ap)+(Uv*Av))/(Ac);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# A total of 170 ft2 are required of which 103 are to be used for vaporization. For the total surface required 318 ft2 will be provided. It can be assumed, then, that the surface provided for vaporization is 193ft**2\n",
-    "# then flux is Q/A=10700, which is with in satisfactory levels.\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000165; # friction factor for reynolds number 62000, using fig.26\n",
-    "s=0.00413;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "f=0.00145; # friction factor for reynolds number 69200, using fig.29\n",
-    "Lp=(L*Ap/Ac); #ft\n",
-    "print\"\\t length of preheat zone :  ft \\t\",Lp\n",
-    "N=(12*Lp/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "s=0.5; # for reynolds number 69200,using fig.6\n",
-    "Ds=1.27; # fig 28\n",
-    "phys=1;\n",
-    "delPsp=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPsp is :  psi \\t\",delPsp\n",
-    "print\"\\t vapourisation \\t\"\n",
-    "f=0.00142;\n",
-    "Lv=9.7; # Lv=L-Lp\n",
-    "Nv=(12*Lv/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",Nv\n",
-    "s=0.28; \n",
-    "delPsv=((f*(Gs**2)*(Ds)*(Nv))/(5.22*(10**10)*(De)*(s)*(1))); # using eq 12.47,psi\n",
-    "print\"\\t delPsv is :  psi \\t\",delPsv\n",
-    "delPS=delPsp+delPsv;\n",
-    "print\"\\t delPS is :  psi \\t\",round(delPS,2)\n",
-    "print\"\\t allowable delPa is 5 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.3 pgno:475"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gasoline is :  Btu/hr \t2669500\n",
-      "\t total heat required for gasoil is :  Btu/hr \t2671900.0\n",
-      "\t S is :  \t0.428571428571\n",
-      "\t Tc is :  F \t517.0\n",
-      "\t hot fluid:inner tube side,gasoil \t\n",
-      "\t flow area is :  ft**2 \t0.0429722222222\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t807498.383969\n",
-      "\t reynolds number is :  \t86215.9813038\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t374.063400576\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t311.968876081\n",
-      "\t cold fluid:shell side,gasoline \t\n",
-      "\t tw is :  F \t459.64414193\n",
-      "\t deltw :  F \t59.6441419296\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t152.933697255\n",
-      "\t total surface area is :  ft**2 \t213.6288\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t105.993294626\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00289577777619\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.73790740915\n",
-      "\t delPr is :  psi \t3.04225352113\n",
-      "\t delPT is :  psi \t5.8\n",
-      "\t allowable delPa is 10psi \t\n",
-      "\t delPs is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=400;\n",
-    "T1=575;\n",
-    "T2=475;\n",
-    "W=28100; # lb/hr\n",
-    "w=34700; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "HT1=290; # enthalpy at T1, Btu/lb, fig 11\n",
-    "HT2=385; # enthalpy at T2, Btu/lb, fig 11\n",
-    "Q=(W*(HT2-HT1)); # for preheat\n",
-    "print\"\\t total heat required for gasoline is :  Btu/hr \\t\",Q\n",
-    "c=0.77; # Btu/(lb), table 7\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt=118; # F eq 5.14\n",
-    "S=75./175.;#((T2-ts)/(T1-ts));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "Kc=0.37; # fig 17\n",
-    "Fc=0.42;\n",
-    "Tc=(T2+(0.42*(T1-T2)));\n",
-    "print\"\\t Tc is :  F \\t\",Tc\n",
-    "print\"\\t hot fluid:inner tube side,gasoil \\t\"\n",
-    "Nt=68;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.65; # at 517F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0694; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=220; # from fig.24\n",
-    "Z=0.118; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #hi/phyt, Hi=()using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "# (mu1/muw)**(0.14) is negligible\n",
-    "print\"\\t cold fluid:shell side,gasoline \\t\"\n",
-    "ho=300; # assumption\n",
-    "tw=(ts)+(((Hio)/(Hio+ho))*(Tc-ts)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-ts);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, ho>300\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=12500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00015; # friction factor for reynolds number 85700, using fig.26\n",
-    "s=0.71;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.09; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10psi \\t\"\n",
-    "print\"\\t delPs is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.4 pgno:482"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.4\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t qv is :  Btu/hr \t3654000\n",
-      "\t qs is :  Btu/hr \t539000\n",
-      "\t total heat required for naphtha is :  Btu/hr \t4193000\n",
-      "\t total heat required for gasoil is :  Btu/hr \t4207500.0\n",
-      "\t delt1 is :  F \t85.0\n",
-      "\t delt2 is :  F \t190.0\n",
-      "\t LMTD is : F \t130.683201952\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.0952380952381\n",
-      "\t FT is 0.97 \t\n",
-      "\t delt is :  F \t126.762705893\n",
-      "\t ratio of two local temperature difference is :  \t0.447368421053\n",
-      "\t caloric temperature of hot fluid is :  F \t451.25\n",
-      "\t caloric temperature of cold fluid is :  F \t323.2\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.0549791666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t927624.100038\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t343.251798561\n",
-      "\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t286.272\n",
-      "\t cold fluid:shell side,naphtha \t\n",
-      "\t tw is :  F \t398.584002369\n",
-      "\t deltw :  F \t75.384002369\n",
-      "\t qv/hv :  \t12180\n",
-      "\t qs/hs :  \t8983\n",
-      "\t A :  \t21163\n",
-      "\t ho :  \t198.813967774\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t117.329454908\n",
-      "\t total surface area is :  ft**2 \t364.4256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t91.0801518561\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00245633150105\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.24018227225\n",
-      "\t delPr is :  psi \t4.82191780822\n",
-      "\t delPT is :  psi \t10.1\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area :  in**2 \t131.70828125\n",
-      "\t wetted perimeter :  in \t236.7325\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20992.3664122\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t delPs is :  psi \t0.25\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.4\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=315.; # inlet cold fluid,F\n",
-    "t2=335.; # outlet cold fluid,F\n",
-    "T1=525.;\n",
-    "T2=400.;\n",
-    "Wv=29000; # lb/hr\n",
-    "Ws=38500; # lb/hr\n",
-    "w=51000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=238; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=252; # enthalpy at t2, Btu/lb, fig 9\n",
-    "Ht3=378; # enthalpy of vapour at t2 \n",
-    "qv=(Wv*(Ht3-Ht2)); # for preheat\n",
-    "print\"\\t qv is :  Btu/hr \\t\",qv\n",
-    "qs=Ws*(Ht2-Ht1);\n",
-    "print\"\\t qs is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qv;\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "c=0.66; # Btu/(lb)(F)\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.97 \\t\" # from fig 18\n",
-    "delt=(0.97*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2)); # fig 17\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.41; # from fig.17\n",
-    "Kc=0.42;\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=116;\n",
-    "n=8; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=1.09; # at 451F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=168; # from fig.24\n",
-    "Z=0.142; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "print\"\\t cold fluid:shell side,naphtha \\t\"\n",
-    "ho1=200; # assumption\n",
-    "tw=(tc)+(((Hio)/(Hio+ho1))*(Tc-tc)); # from eq.5.31, calculation mistake\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-tc);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, hv>300, hs=60\n",
-    "Av=(qv/300);\n",
-    "As=qs/60;\n",
-    "print\"\\t qv/hv :  \\t\",Av\n",
-    "print\"\\t qs/hs :  \\t\",As\n",
-    "A1=As+Av;\n",
-    "print\"\\t A :  \\t\",A1\n",
-    "ho=(Q/A1);\n",
-    "print\"\\t ho :  \\t\",ho\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=11500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000168; # friction factor for reynolds number 59200, using fig.26\n",
-    "s=0.73;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.11; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "Af=(3.14*(21.25**2-(116))/8);\n",
-    "print\"\\t flow area :  in**2 \\t\",Af\n",
-    "As=0.917; # ft**2\n",
-    "p=(3.14*21.25/2)+(3.14*1*116/2)+(21.25)\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=0.186; # ft\n",
-    "Gs=(Ws/(2*As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.435; # at 315F, fig 14,lb/(ft)*(hr)\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "f=0.00028; # using fig.26\n",
-    "row=0.337; # fig 13.14\n",
-    "# soutlet max=0.071,\n",
-    "s=0.35; # using fig.6\n",
-    "phys=1;\n",
-    "delPs=0.25 #((f*(Gs**2)*(L))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.5 pgno:488"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.5\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for butane is :  Btu/hr \t3957600\n",
-      "\t total heat required for steam is : Btu/hr \t3966760\n",
-      "\t trail 1 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t105.068772287\n",
-      "\t total surface area is : ft**2 \t342.3472\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t92.6956025929\n",
-      "\t vapour density : lb/ft**3 \t3.18723589714\n",
-      "\t weight flow of recirculated liquid : lb/hr \t163200\n",
-      "\t volume of liquid : ft**3 \t6071.04\n",
-      "\t volume of vapour : ft**3 \t17952.0\n",
-      "\t total volume out of reboiler : ft**3 \t24023.04\n",
-      "\t vo is : ft**3/lb \t0.11776\n",
-      "\t pressure leg : psi \t1.58756230188\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.228597222222\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t892399.295218\n",
-      "\t reynolds number is : \t190648.940342\n",
-      "\t delPt is : psi \t2.1\n",
-      "negilgable\n",
-      "\t total resisitance : psi \t3.69151627479\n",
-      "\t driving force : psi \t2.98611111111\n",
-      "\t trial 2 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t140.091696383\n",
-      "\t total surface area is : ft**2 \t355.6956\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t89.21695967\n",
-      "\t pressure leg : psi \t1.19067172641\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.316680555556\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t644182.272707\n",
-      "\t reynolds number is : \t137620.75826\n",
-      "\t delPt is : psi \t0.874030618788\n",
-      "\t total resisitance : psi \t2.0647023452\n",
-      "\t driving force : psi \t2.23958333333\n",
-      "\t hot fluid : shell side,steam \t\n",
-      "\t cold fluid:inner tube side, butane \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t734.042553191\n",
-      "\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t248.0\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t212.814645309\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.006537030325\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.5\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "W=40800; # lb/hr\n",
-    "w=4570; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=241; # enthalpy of liquid at 228F, Btu/lb, fig 9\n",
-    "Ht2=338; # enthalpy of vapourat 228F, Btu/lb, fig 9\n",
-    "Q=(W*(Ht2-Ht1));\n",
-    "print\"\\t total heat required for butane is :  Btu/hr \\t\",Q\n",
-    "l=868; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is : Btu/hr \\t\",Q\n",
-    "delt=125; # delt=LMTD, isothermal boiling, eq 5.14\n",
-    "# Tc and tc: Both streams are isuthermal\n",
-    "print\"\\t trail 1 \\t\"\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=109; # assuming one tube passes, 13.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# Assume 4: 1 recirculation ratio\n",
-    "rowv=(58/(359*(688/492)*(14.7/290))); # eq 15.18\n",
-    "print\"\\t vapour density : lb/ft**3 \\t\",rowv\n",
-    "Vv=0.44; \n",
-    "Vl=0.0372; # fig 6\n",
-    "W1=4*W;\n",
-    "print\"\\t weight flow of recirculated liquid : lb/hr \\t\",W1\n",
-    "VL=W1*Vl;\n",
-    "VV=W*Vv;\n",
-    "print\"\\t volume of liquid : ft**3 \\t\",VL\n",
-    "print\"\\t volume of vapour : ft**3 \\t\",VV\n",
-    "V=VL+VV;\n",
-    "print\"\\t total volume out of reboiler : ft**3 \\t\",V\n",
-    "vo=(V/(W1+W));\n",
-    "print\"\\t vo is : ft**3/lb \\t\",vo\n",
-    "Pl=((2.3*16)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=109;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000127; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",round(delPt,2)\n",
-    "P=Pl+delPt;\n",
-    "print\"negilgable\"\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(16*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# The resistances are greater than the hydrostatic head can provide; hence the recirculation ratio will be less than 4: 1\n",
-    "print\"\\t trial 2 \\t\" # Assume 12'0\" tubes and 4:1 recirculation ratio\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=12;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=151; # assuming one tube passes, 15.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Pl=((2.3*12)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=151;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000135; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(12)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",delPt\n",
-    "P=Pl+delPt;\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(12*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# Since the driving force is slightly greater than the resistances, a recirculation ratio better than 4:1 is assured.\n",
-    "print\"\\t hot fluid : shell side,steam \\t\"\n",
-    "ho=1500; # condensing steam\n",
-    "print\"\\t cold fluid:inner tube side, butane \\t\"\n",
-    "jH=330; # from fig.24\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((300)*(0.62/0.75)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "UD=89;\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.6 pgno492"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.6\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat duty : Btu/hr \t5799016.0\n",
-      "\t total heat duty : lb/hr \t37902.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.6\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#20000=WD+WB;\n",
-    "#0.99*WD+(0.05*WB)=(20000*.5);\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "HBl=108; # fig 3 and 12\n",
-    "HDl=85.8; #fig 3 and 12\n",
-    "HDv=253.8; # fig 3 and 12\n",
-    "HFl=92; # fig 3 and 12\n",
-    "l=153; # fig 3 and 12\n",
-    "QR=((2.54+1)*WD*(HDv))-(2.54*WD*HDl)+(WB*HBl)-(20000*HFl);\n",
-    "print\"\\t total heat duty : Btu/hr \\t\",round(QR)\n",
-    "Q=QR/153;\n",
-    "print\"\\t total heat duty : lb/hr \\t\",round(Q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 15.7 pgno:502"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\ttotal Lb/hr is \t20000\n",
-      "\ttotal Mol/hr is \t235.5\n",
-      "\tx1 of C6H6 is \t0.543524416136\n",
-      "\tx1 of C7H8 is \t0.456475583864\n",
-      "\tTotal x1 is \t1.0\n",
-      "\tx1Pp1 of C6H6 is \t750.063694268\n",
-      "\tx1Pp1 of C7H8 is \t262.473460722\n",
-      "\tTotal x1Pp1 is \t1012.53715499\n",
-      "\ty1 of C6H6 is \t0.740776464914\n",
-      "\ty1 of C7H8 is \t0.259223535086\n",
-      "\tTotal y1 is \t1.0\n",
-      "\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\t0.558\n",
-      "\tWR` = %.2f (mol reflux)/(mol distillate)\t1.27\n",
-      "\tAssumed 200 percent of the theoretical minimum reflux as economic\t\tWR = (mol)/(mil distillate)\t2.54\n",
-      "\tThe intercept for the upper operating line = \t0.280225988701\n",
-      "\tConnecting the corresponding line in Fig. 15.23, plates required: \t13\n",
-      "\tFeed plate is th(from top)\t7\n",
-      "\tTotal reflux is \t311.15\n",
-      "\t\t\t\t\tHeat balances\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\tHeat balance \t\taround condenser:\t\n",
-      "\t  Heat in:\t\t  Top plate vapor.......433\t87.3\t\t195\t%.1f\t\t33900 253.8 8603820.0\n",
-      "\t  Heat out:\t\t  Distillate............\n",
-      "122.5\t78.3\t\t195\t\t\t9570 85.8 821106.0\n",
-      "\t  Reflux................\n",
-      "310.5\t78.3\t\t195\t\t\t24330 85.8 2087514.0\n",
-      "\t  Condenser duty, by\t\t  difference........... .....   ....    ......  ..\n",
-      ".     .....   5688000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t8600000\t\t\n",
-      "\tReboiler vapor is  lb/hr\t37908\n",
-      "\tTrapout is  lb/hr\t48338\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\n",
-      "\tHeat in:\t\t  Trapout...............522\t92.8\t\t246\t108.0\t5230000\t48338\n",
-      "\t  Reboiler duty, \t\t  by difference.......  ....    ....    .....   ...     .....   5800000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t11030000\t\t\n",
-      "\t\tReboiler requirements are\t\n",
-      "\t\tTotal liquid to reboiler\t48330 lb/hr\t\t\tVaporization\t\t\t37900 lb/hr\t\t\tTemperature(nearly isothermal)\t246DegF\t\t\tPressure\t\t\t5 psig\t\t\tHeat load\t\t\t5800000 Btu/hr\t\n",
-      "total heat out is btu/hr 7640000\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "#Basis: One hour\n",
-    "#20000=WD+WB , material balance\n",
-    "#0.99*WD+(0.05*WB)=(20000*0.5) , Benzene balance\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "\n",
-    "#Compositions and Boiling Points\n",
-    "#Feed\n",
-    "l1 = 10000; #Lb/hr , C6H4\n",
-    "l2 = 10000; #Lb/hr , C7H8\n",
-    "lb = l1+l2; #Lb/hr\n",
-    "print\"\\ttotal Lb/hr is \\t\",lb\n",
-    "mo1 = 78.1; #Mol. wt., C6H6\n",
-    "mo2 = 93.1; #Mol. wt , C7H8\n",
-    "mh1 = 128.0; #Mol/hr , C6H6\n",
-    "mh2 = 107.5; #Mol/hr , C7H8\n",
-    "mh = mh1 + mh2; # Mol/hr\n",
-    "print\"\\ttotal Mol/hr is \\t\",mh\n",
-    "x1 = mh1/mh;\n",
-    "print\"\\tx1 of C6H6 is \\t\",x1\n",
-    "x2 = mh2/mh;\n",
-    "print\"\\tx1 of C7H8 is \\t\",x2\n",
-    "x = x1+x2;\n",
-    "print\"\\tTotal x1 is \\t\",x\n",
-    "Pp1= 1380; # 214Deg F\n",
-    "Pp2=575; # 214Deg F\n",
-    "xp1 = x1*Pp1;\n",
-    "print\"\\tx1Pp1 of C6H6 is \\t\",xp1\n",
-    "xp2 = x2*Pp2;\n",
-    "print\"\\tx1Pp1 of C7H8 is \\t\",xp2\n",
-    "sxp = xp1 + xp2;\n",
-    "print\"\\tTotal x1Pp1 is \\t\",sxp\n",
-    "y1 = xp1/sxp;\n",
-    "print\"\\ty1 of C6H6 is \\t\",y1\n",
-    "y2 = xp2/sxp;\n",
-    "print\"\\ty1 of C7H8 is \\t\",y2\n",
-    "y = y1+y2;\n",
-    "print\"\\tTotal y1 is \\t\",y\n",
-    "\n",
-    "\n",
-    "w1 = 0.558; #from eq 15.42\n",
-    "print\"\\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\\t\",w1\n",
-    "wD=1;\n",
-    "xD = 0.992;\n",
-    "#V = WR' + WD\n",
-    "# WR'/V = 0.558\n",
-    "#Solving, WR' = (WR' * 0.558) + (0.558 * WD)\n",
-    "Wr = 1.27; # mol reflux/mol distillate\n",
-    "print\"\\tWR` = %.2f (mol reflux)/(mol distillate)\\t\",Wr\n",
-    "Wr1 = Wr * 2; # mol/ mol distillate\n",
-    "print\"\\tAssumed 200 percent of the theoretical minimum reflux as economic\\t\\tWR = (mol)/(mil distillate)\\t\",Wr1\n",
-    "In = (wD * xD)/(Wr1 + 1); #intercept for the upper operating line\n",
-    "print\"\\tThe intercept for the upper operating line = \\t\",In\n",
-    "p = 13; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tConnecting the corresponding line in Fig. 15.23, plates required: \\t\",p\n",
-    "fp = 7; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tFeed plate is th(from top)\\t\",fp\n",
-    "d=122.5;\n",
-    "tf = Wr1 * d;\n",
-    "print\"\\tTotal reflux is \\t\",tf\n",
-    "print\"\\t\\t\\t\\t\\tHeat balances\"\n",
-    "\n",
-    "#Heat Balances\n",
-    "l1 = 33900;\n",
-    "l2 = 9570;\n",
-    "l3 = 24330;\n",
-    "b1 = 253.8;\n",
-    "b2 = 85.8;\n",
-    "b3 = 85.8;\n",
-    "bt1 = b1*l1;\n",
-    "bt2 = b2*l2;\n",
-    "bt3 = b3*l3;\n",
-    "bt4 = 5688000;\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\\tHeat balance \\t\\taround condenser:\\t\"\n",
-    "print\"\\t  Heat in:\\t\\t  Top plate vapor.......433\\t87.3\\t\\t195\\t%.1f\\t\\t\",l1,b1,bt1\n",
-    "print\"\\t  Heat out:\\t\\t  Distillate............\"\n",
-    "print\"122.5\\t78.3\\t\\t195\\t\\t\\t\",l2,b2,bt2\n",
-    "print\"\\t  Reflux................\"\n",
-    "print\"310.5\\t78.3\\t\\t195\\t\\t\\t\",l3,b3,bt3\n",
-    "print\"\\t  Condenser duty, by\\t\\t  difference........... .....   ....    ......  ..\"\n",
-    "print\".     .....   5688000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t8600000\\t\\t\"\n",
-    "tho=7640000;\n",
-    "\n",
-    "lam = 153; # At 246 DegF, Btu/hr\n",
-    "rv = 5800000/153; #Lb/hr\n",
-    "print\"\\tReboiler vapor is  lb/hr\\t\",rv\n",
-    "to = rv + 10430; #Lb/hr\n",
-    "print\"\\tTrapout is  lb/hr\\t\",to\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\"\n",
-    "print\"\\tHeat in:\\t\\t  Trapout...............522\\t92.8\\t\\t246\\t108.0\\t5230000\\t\",to\n",
-    "print\"\\t  Reboiler duty, \\t\\t  by difference.......  ....    ....    .....   ...     .....   5800000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t11030000\\t\\t\"\n",
-    "print\"\\t\\tReboiler requirements are\\t\"\n",
-    "print\"\\t\\tTotal liquid to reboiler\\t48330 lb/hr\\t\\t\\tVaporization\\t\\t\\t37900 lb/hr\\t\\t\\tTemperature(nearly isothermal)\\t246DegF\\t\\t\\tPressure\\t\\t\\t5 psig\\t\\t\\tHeat load\\t\\t\\t5800000 Btu/hr\\t\"\n",
-    "print\"total heat out is btu/hr\",tho \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.8 pgno:506"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\t\tDEW POINT OF OVERHEAD\n",
-      "\n",
-      "\t\tMol/hr\t\tK(148DegF,40 psia)\tV/K\n",
-      "\n",
-      "\t\t--------------------------------------------\n",
-      "\n",
-      "[   6.4  219.7    2.3] [ 2.8   1.01  0.34] [ 17 221  74]\n",
-      "\n",
-      "\t\tBUBBLE POINTS OF BOTTOMS\n",
-      "\n",
-      "\t\tMol/hr\t\tK(330DegF,40psia)\t\tKL\t\tLb/hr\n",
-      "\n",
-      "\t\t--------------------------------------------------------------\n",
-      "\n",
-      "4.1 5.8 23.8 1700\n",
-      "49.3 3.0 148.0 13900\n",
-      "71.9 1.68 120.0 13030\n",
-      "52.5 0.98 51.4 6260\n",
-      "54.7 0.57 31.2 4240\n",
-      "82.5 0.35 28.9 4330\n",
-      "76.6 0.21 16.1 2640\n",
-      "22.4 0.13 2.9 520\n",
-      "\t\t____\t\t\t\t\t____\t\t____\n",
-      "\n",
-      "\t\t[  4  53 124 176 230 312 388 410]\n",
-      "\t\t\t\t\t[23.800000000000001, 171.80000000000001, 291.80000000000001, 343.19999999999999, 374.39999999999998, 403.29999999999995, 419.39999999999998, 422.29999999999995]\n",
-      "\t\t[ 1700 13900 13030  6260  4240  4330  2640   520]\n",
-      "\tAverage mol. wt. \n",
-      "[ 71.42857143  80.9080326   44.65387252  18.24009324  11.32478632\n",
-      "  10.7364245    6.29470672   1.23135212]\n",
-      "\n",
-      "\n",
-      "\t\t\t\t\t\tHEAT BALANCES:\n",
-      "\n",
-      "\t\t\t\tMol/hr\t\tMol.wt.\t\tLb/hr\t\tTemp,DegF\t\tBtu/lb\t\tBtu/hr\n",
-      "\t\n",
-      "\t\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tHeat Balance onCondeser\n",
-      "\t  Heat in:\n",
-      "\t   Top plate vapor......\n",
-      "\n",
-      "\n",
-      "\t\tCALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "\n",
-      "\t\ty*\t\t\tReboiler vapor\t\t\t\tK(300DegF,40psia)\tMol*K\n",
-      "\t\t\t\tV = y*205.7 +\tBottoms\t=\tTrapout\n",
-      "\n",
-      "\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "CALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\n",
-      "              V = y*205.7 +   Bottoms =   Trapout\n",
-      "      ----------------------------------------------------------------------------------------\n",
-      "C5 0.056       11.5        4.1     15.6        4.5     70.29\n",
-      "C6 0.35        72.0        49.3        121.3       2.25        272.91\n",
-      "C7 0.285       58.6        71.9        130.5       1.2     156.63\n",
-      "C8 0.122       25.1        52.5        77.6        0.66        51.21\n",
-      "C9 0.074       15.2        54.7        69.9        0.38        26.57\n",
-      "C10    0.068       14.0        82.5        96.5        0.22        21.23\n",
-      "C11    0.038       7.8     76.6        84.4        0.13        10.97\n",
-      "C12    0.007       1.4     22.4        23.8        0.07        1.67\n",
-      "----------------------------------------------------------------------------------------\n",
-      "1.000      205.7       414.0       619.7               611.5\n",
-      "Reboiler requirements are\n",
-      "      Vaporization lb/hr 22700\n",
-      "      Total liquor to reboiler  lb/hr 78177\n",
-      "      Heat load Btu/hr 4280000\n",
-      "      Temperature range 300-330 def F\n",
-      "      Operating pressure  psi 40\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Dew point of Overhead\n",
-    "import numpy\n",
-    "vc=numpy.array([6.4, 219.7, 2.3])\n",
-    "#vc(1) = 6.4; # Mol/hr\n",
-    "#vc(2) = 219.7; #Mol/hr\n",
-    "#vc(3) = 2.3; #Mol/hr\n",
-    "K=numpy.array([2.8, 1.01, 0.34])\n",
-    "#K(1) = 2.8; #at 148DegF and 40 psia\n",
-    "#K(2) = 1.01; #at 148DegF and 40 psia\n",
-    "#K(3) = 0.34; #at 148DegF and 40 psia\n",
-    "v=numpy.array([0, 0, 0])\n",
-    "i=0;\n",
-    "while (i<3):\n",
-    "    v[0]=vc[0]*K[0];\n",
-    "    v[1]=vc[1]*K[1];\n",
-    "    v[2]=vc[1]*K[2];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "print\"\\n\\t\\tDEW POINT OF OVERHEAD\"\n",
-    "print\"\\n\\t\\tMol/hr\\t\\tK(148DegF,40 psia)\\tV/K\\n\"\n",
-    "print\"\\t\\t--------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print vc,K,v\n",
-    "\n",
-    "bc=numpy.array([4.1, 49.3, 71.9, 52.5, 54.7, 82.5, 76.6, 22.4])\n",
-    "#bc(1)=4.1; #Mol/hr\n",
-    "#bc(2)=49.3; #Mol/hr\n",
-    "#c(3)=71.9; #Mol/hr\n",
-    "#bc(4)=52.5; #Mol/hr\n",
-    "#bc(5)=54.7; #Mol/hr\n",
-    "#bc(6)=82.5; #Mol/hr\n",
-    "#bc(7)=76.6; #Mol/hr\n",
-    "#bc(8)=22.4; #Mol/hr\n",
-    "tbc=numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "tbc[0]=tbc[0]+bc[0];\n",
-    "i=1\n",
-    "while (i<8):\n",
-    "    tbc[i]=tbc[i-1]+bc[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "bK=numpy.array([5.8, 3.0, 1.68, 0.98, 0.57, 0.35, 0.21, 0.13])\n",
-    "#bK(1)=5.8; #at 330DegF, 40 psia\n",
-    "#bK(2)=3.0; #at 330DegF, 40 psia\n",
-    "#bK(3)=1.68; #at 330DegF, 40 psia\n",
-    "#bK(4)=0.98; #at 330DegF, 40 psia\n",
-    "#bK(5)=0.57; #at 330DegF, 40 psia\n",
-    "#bK(6)=0.35; #at 330DegF, 40 psia\n",
-    "#bK(7)=0.21; #at 330DegF, 40 psia\n",
-    "#bK(8)=0.13; #at 330DegF, 40 psia\n",
-    "\n",
-    "KL=numpy.array([23.8, 148.0, 120.0, 51.4, 31.2, 28.9, 16.1, 2.9])\n",
-    "\n",
-    "#KL(1)=23.8;\n",
-    "#KL(2)=148.0;\n",
-    "#KL(3)=120.8;\n",
-    "#KL(4)=51.4;\n",
-    "#KL(5)=31.2;\n",
-    "#KL(6)=28.9;\n",
-    "#KL(7)=16.1;\n",
-    "#KL(8)=2.9;\n",
-    "\n",
-    "tk=([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "i=1;\n",
-    "op=40;\n",
-    "tk[0]=KL[0]\n",
-    "while (i<8):\n",
-    "    tk[i]=tk[i-1]+KL[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "l=numpy.array([1700, 13900, 13030, 6260, 4240, 4330, 2640, 520])    \n",
-    "#l(1)=1700; #Lb/hr\n",
-    "#l(2)=13900; #Lb/hr\n",
-    "#l(3)=13030; #Lb/hr\n",
-    "#l(4)=6260; #Lb/hr\n",
-    "#l(5)=4240; #Lb/hr\n",
-    "#l(6)=4330; #Lb/hr\n",
-    "#l(7)=2640; #Lb/hr\n",
-    "#l(8)=520; #Lb/hr\n",
-    "\n",
-    "tl=numpy.array([0, 0, 0, 0, 0, 0, 0, 0,])\n",
-    "\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "    tl[i]=tl[i]+l[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\n\\t\\tBUBBLE POINTS OF BOTTOMS\\n\"\n",
-    "print\"\\t\\tMol/hr\\t\\tK(330DegF,40psia)\\t\\tKL\\t\\tLb/hr\\n\"\n",
-    "print\"\\t\\t--------------------------------------------------------------\\n\"\n",
-    "tlr=78177;\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "\n",
-    "    print bc[i],bK[i],KL[i],l[i]\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\t____\\t\\t\\t\\t\\t____\\t\\t____\\n\"\n",
-    "\n",
-    "print\"\\t\\t\",tbc \n",
-    "print\"\\t\\t\\t\\t\\t\",tk \n",
-    "print\"\\t\\t\",tl\n",
-    "av = numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "av=tl/tk\n",
-    "hl=4280000;\n",
-    "print\"\\tAverage mol. wt. \\n\",av\n",
-    "\n",
-    "lh=numpy.array([48894, 16298, 32596])\n",
-    "bl=numpy.array([286, 129, 129])\n",
-    "#lh(1)=48894;#Lb/hr\n",
-    "#lh(2)=16298;#Lb/hr\n",
-    "#lh(3)=32596;#Lb/hr\n",
-    "#bl(1)=286;#Btu/hr\n",
-    "#bl(2)=129;#Btu/hr\n",
-    "#bl(3)=129;#Btu/hr\n",
-    "\n",
-    "bh=numpy.array([0, 0, 0])\n",
-    "vap=22700;\n",
-    "i=0;\n",
-    "\n",
-    "while (i<3):\n",
-    "    bh[0]=lh[0]*bl[0];\n",
-    "    i=i+1;\n",
-    "\n",
-    "#Heat Balances\n",
-    "print\"\\n\\n\\t\\t\\t\\t\\t\\tHEAT BALANCES:\"\n",
-    "print\"\\n\\t\\t\\t\\tMol/hr\\t\\tMol.wt.\\t\\tLb/hr\\t\\tTemp,DegF\\t\\tBtu/lb\\t\\tBtu/hr\\n\\t\"\n",
-    "print\"\\t\\t\\t----------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\tHeat Balance onCondeser\\n\\t  Heat in:\\n\\t   Top plate vapor......\"\n",
-    "\n",
-    "#Heat Balances on reboiler\n",
-    "#Assume 30Deg difference between reboiler and bottom plate giving bottom-plate temperature of 300DegF\n",
-    "#Mol/hr from Eq. 15.47\n",
-    "\n",
-    "pc=numpy.array([0.056, 0.35, 0.285, 0.122, 0.074, 0.068, 0.038, 0.007])\n",
-    "#pc(1)=0.056;\n",
-    "#pc(2)=0.350;\n",
-    "##pc(3)=0.285;\n",
-    "#pc(4)=0.122;\n",
-    "#pc(5)=0.074;\n",
-    "#pc(6)=0.068;\n",
-    "#pc(7)=0.038;\n",
-    "#pc(8)=0.007;\n",
-    "\n",
-    "pk=numpy.array([4.5, 2.25, 1.2, 0.66, 0.38, 0.22, 0.13, 0.07])\n",
-    "#pK(1)=4.5;\n",
-    "#pK(2)=2.25;\n",
-    "#pK(3)=1.20;\n",
-    "#pK(4)=0.66;\n",
-    "#pK(5)=0.38;\n",
-    "#pK(6)=0.22;\n",
-    "#pK(7)=0.13;\n",
-    "#pK(8)=0.07;\n",
-    "\n",
-    "print\"\\n\\n\\t\\tCALCULATION OF BOTTOM PLATE TEMPERATURE\\n\"\n",
-    "print\"\\t\\ty*\\t\\t\\tReboiler vapor\\t\\t\\t\\tK(300DegF,40psia)\\tMol*K\\n\\t\\t\\t\\tV = y*205.7 +\\tBottoms\\t=\\tTrapout\\n\"\n",
-    "print\"\\t\\t----------------------------------------------------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print \"CALCULATION OF BOTTOM PLATE TEMPERATURE\"\n",
-    "print\"      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\"\n",
-    "print\"              V = y*205.7 +   Bottoms =   Trapout\"\n",
-    "print\"      ----------------------------------------------------------------------------------------\"\n",
-    "print   \"C5 0.056       11.5        4.1     15.6        4.5     70.29\"\n",
-    "print   \"C6 0.35        72.0        49.3        121.3       2.25        272.91\"\n",
-    "print   \"C7 0.285       58.6        71.9        130.5       1.2     156.63\"\n",
-    "print   \"C8 0.122       25.1        52.5        77.6        0.66        51.21\"\n",
-    "print   \"C9 0.074       15.2        54.7        69.9        0.38        26.57\"\n",
-    "print   \"C10    0.068       14.0        82.5        96.5        0.22        21.23\"\n",
-    "print   \"C11    0.038       7.8     76.6        84.4        0.13        10.97\"\n",
-    "print   \"C12    0.007       1.4     22.4        23.8        0.07        1.67\"\n",
-    "print       \"----------------------------------------------------------------------------------------\"\n",
-    "print       \"1.000      205.7       414.0       619.7               611.5\"\n",
-    "\n",
-    "\n",
-    "print\"Reboiler requirements are\"\n",
-    "print\"      Vaporization lb/hr\",vap\n",
-    "print\"      Total liquor to reboiler  lb/hr\",tlr    \n",
-    "print\"      Heat load Btu/hr\",hl\n",
-    "print\"      Temperature range 300-330 def F\"\n",
-    "print\"      Operating pressure  psi\",op "
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_1.ipynb
deleted file mode 100755
index d185cf80..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_1.ipynb
+++ /dev/null
@@ -1,1315 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 15 : Vaporizers Evapourators and Reboilers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.1 pgno:463"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9453000.0\n",
-      "\t total heat required for kerosene is :  Btu/hr \t9450000.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t91.1262293169\n",
-      "\t A :  ft**2 \t1037.02304713\n",
-      "\t By the law of mixtures \t\n",
-      "\t v2 : %.0f ft**3/lb \t11.0034\n",
-      "\t vav :  ft**3/lb \t3.16417120715\n",
-      "\t By the approximate method \t\n",
-      "\t vav :  ft**3/lb \t5.5102\n",
-      "\t actual density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.00505661639416\n",
-      "\t approximate density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.0029\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=250;\n",
-    "T1=400;\n",
-    "T2=300;\n",
-    "w=10000; # lb/hr\n",
-    "W=150000; # lb/hr\n",
-    "l=945.3; # Btu/(lb) , table 7\n",
-    "from math import log10\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "C=0.63; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-ts; #F\n",
-    "delt2=T1-ts; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "UD=100;\n",
-    "A=(Q/(UD*LMTD));\n",
-    "print\"\\t A :  ft**2 \\t\",A\n",
-    "WC=94500; # Btu/F\n",
-    "vl=0.017; # ft**3/lb, from table 7\n",
-    "vv=13.75; # ft**3/lb, from table 7\n",
-    "print\"\\t By the law of mixtures \\t\"\n",
-    "# Assume 80 per cent of the outlet fluid is vapor\n",
-    "v2=(0.8*vv)+(.2*vl);\n",
-    "print\"\\t v2 : ft**3/lb \\t\",v2\n",
-    "vav=(WC*(v2-vl)/(UD*A))-((WC*(T2-ts)/(l*w))*(vv-vl))+vl;\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav\n",
-    "print\"\\t By the approximate method \\t\"\n",
-    "vav1=(vl+v2)/(2);\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav1\n",
-    "row=62.5;\n",
-    "rowac=(1/vav);\n",
-    "s=(rowac/row);\n",
-    "print\"\\t actual density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",s\n",
-    "rowap=(1/vav1);\n",
-    "s=(rowap/row);\n",
-    "print\"\\t approximate density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",round(s,4)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.2 pgno:464"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for preheat of butane is :  Btu/hr \t2124200\n",
-      "\t total heat required for vapourisation of butane is :  Btu/hr \t2172500\n",
-      "\t total heat required for  butane is :  Btu/hr \t4296700\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t4297328.0\n",
-      "\t Wp1 is :  lb/hr \t13401.8927445\n",
-      "\t Wv1 is :  lb/hr \t21092\n",
-      "\t W is :  lb/hr \t34493.8927445\n",
-      "\t weighted delt is : % F \t124.582285677\n",
-      "\t caloric temperature of hot fluid is :  F \t338\n",
-      "\t caloric temperature of cold fluid is :  F \t171\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.15675\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t31132.3763955\n",
-      "\t reynolds number is :  \t62178.9886688\n",
-      "\t hio is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,butane \t\n",
-      "\t preheating \t\n",
-      "\t flow area is :  ft**2 \t0.105902777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t233232.786885\n",
-      "\t reynolds number is :  \t69214.7658922\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t231.272727273\n",
-      "\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \t200.378071834\n",
-      "\t clean surface required for preheating :  ft**2 \t66.883030772\n",
-      "\t for vapourisation \t\n",
-      "\t reynolds number is :  \t79511.1773472\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t236.96969697\n",
-      "\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \t204.640614096\n",
-      "\t clean surface required for vapourisation :  ft**2 \t103.069633088\n",
-      "\t total clean surface :  ft**2 \t169.952663859\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t202.96313674\n",
-      "\t total surface area is :  ft**2 \t318.3488\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.352513798\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00430213212754\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.16\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t preheating \t\n",
-      "\t length of preheat zone :  ft \t6.29662676683\n",
-      "\t number of crosses are :  \t15.1119042404\n",
-      "\t delPsp is :  psi \t0.703032923143\n",
-      "\t vapourisation \t\n",
-      "\t number of crosses are :  \t23.28\n",
-      "\t delPsv is :  psi \t1.89396418309\n",
-      "\t delPS is :  psi \t2.6\n",
-      "\t allowable delPa is 5 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=108; # inlet cold fluid,F\n",
-    "t2=235; # outlet cold fluid,F\n",
-    "Ts=338;\n",
-    "Wp=24700; # lb/hr\n",
-    "Wv=19750; # lb/hr\n",
-    "w=4880; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=162; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=248; # enthalpy at t2, Btu/lb, fig 9\n",
-    "qp=(Wp*(Ht2-Ht1)); # for preheat\n",
-    "print\"\\t total heat required for preheat of butane is :  Btu/hr \\t\",qp\n",
-    "Ht3=358; # enthalpy of vapour at t2, Btu/lb, fig 9\n",
-    "qv=Wv*(Ht3-Ht2);\n",
-    "print\"\\t total heat required for vapourisation of butane is :  Btu/hr \\t\",qv\n",
-    "Q=qp+qv;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=880.6; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "deltp=158.5; # F, from eq 5.14\n",
-    "deltv=103; # F eq 5.14\n",
-    "Wp1=(qp/deltp);\n",
-    "print\"\\t Wp1 is :  lb/hr \\t\",Wp1\n",
-    "Wv1=(qv/deltv);\n",
-    "print\"\\t Wv1 is :  lb/hr \\t\",Wv1\n",
-    "W=(Wp1+Wv1);\n",
-    "print\"\\t W is :  lb/hr \\t\",W\n",
-    "delt=(Q/W);\n",
-    "print\"\\t weighted delt is : % F \\t\",delt\n",
-    "Tc=((Ts)+(Ts))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=76;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.594; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.0363; # at 338F, fig 15,lb/(ft)*(hr)\n",
-    "D=0.0725; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensing steam,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hio is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,butane \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(Wp/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.278; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0825; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=159; # from fig.28\n",
-    "Z=0.12; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hop=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hop\n",
-    "Up=((hio)*(hop)/(hio+hop)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \\t\",Up\n",
-    "Ap=(qp/(Up*deltp));\n",
-    "print\"\\t clean surface required for preheating :  ft**2 \\t\",Ap\n",
-    "print\"\\t for vapourisation \\t\"\n",
-    "mu2=0.242; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=170; # from fig.28\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hov=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hov\n",
-    "Uv=((hio)*(hov)/(hio+hov)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \\t\",Uv\n",
-    "Av=(qv/(Uv*deltv));\n",
-    "print\"\\t clean surface required for vapourisation :  ft**2 \\t\",Av\n",
-    "Ac=Ap+Av;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",Ac\n",
-    "UC=((Up*Ap)+(Uv*Av))/(Ac);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# A total of 170 ft2 are required of which 103 are to be used for vaporization. For the total surface required 318 ft2 will be provided. It can be assumed, then, that the surface provided for vaporization is 193ft**2\n",
-    "# then flux is Q/A=10700, which is with in satisfactory levels.\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000165; # friction factor for reynolds number 62000, using fig.26\n",
-    "s=0.00413;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "f=0.00145; # friction factor for reynolds number 69200, using fig.29\n",
-    "Lp=(L*Ap/Ac); #ft\n",
-    "print\"\\t length of preheat zone :  ft \\t\",Lp\n",
-    "N=(12*Lp/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "s=0.5; # for reynolds number 69200,using fig.6\n",
-    "Ds=1.27; # fig 28\n",
-    "phys=1;\n",
-    "delPsp=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPsp is :  psi \\t\",delPsp\n",
-    "print\"\\t vapourisation \\t\"\n",
-    "f=0.00142;\n",
-    "Lv=9.7; # Lv=L-Lp\n",
-    "Nv=(12*Lv/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",Nv\n",
-    "s=0.28; \n",
-    "delPsv=((f*(Gs**2)*(Ds)*(Nv))/(5.22*(10**10)*(De)*(s)*(1))); # using eq 12.47,psi\n",
-    "print\"\\t delPsv is :  psi \\t\",delPsv\n",
-    "delPS=delPsp+delPsv;\n",
-    "print\"\\t delPS is :  psi \\t\",round(delPS,2)\n",
-    "print\"\\t allowable delPa is 5 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.3 pgno:475"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gasoline is :  Btu/hr \t2669500\n",
-      "\t total heat required for gasoil is :  Btu/hr \t2671900.0\n",
-      "\t S is :  \t0.428571428571\n",
-      "\t Tc is :  F \t517.0\n",
-      "\t hot fluid:inner tube side,gasoil \t\n",
-      "\t flow area is :  ft**2 \t0.0429722222222\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t807498.383969\n",
-      "\t reynolds number is :  \t86215.9813038\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t374.063400576\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t311.968876081\n",
-      "\t cold fluid:shell side,gasoline \t\n",
-      "\t tw is :  F \t459.64414193\n",
-      "\t deltw :  F \t59.6441419296\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t152.933697255\n",
-      "\t total surface area is :  ft**2 \t213.6288\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t105.993294626\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00289577777619\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.73790740915\n",
-      "\t delPr is :  psi \t3.04225352113\n",
-      "\t delPT is :  psi \t5.8\n",
-      "\t allowable delPa is 10psi \t\n",
-      "\t delPs is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=400;\n",
-    "T1=575;\n",
-    "T2=475;\n",
-    "W=28100; # lb/hr\n",
-    "w=34700; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "HT1=290; # enthalpy at T1, Btu/lb, fig 11\n",
-    "HT2=385; # enthalpy at T2, Btu/lb, fig 11\n",
-    "Q=(W*(HT2-HT1)); # for preheat\n",
-    "print\"\\t total heat required for gasoline is :  Btu/hr \\t\",Q\n",
-    "c=0.77; # Btu/(lb), table 7\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt=118; # F eq 5.14\n",
-    "S=75./175.;#((T2-ts)/(T1-ts));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "Kc=0.37; # fig 17\n",
-    "Fc=0.42;\n",
-    "Tc=(T2+(0.42*(T1-T2)));\n",
-    "print\"\\t Tc is :  F \\t\",Tc\n",
-    "print\"\\t hot fluid:inner tube side,gasoil \\t\"\n",
-    "Nt=68;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.65; # at 517F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0694; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=220; # from fig.24\n",
-    "Z=0.118; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #hi/phyt, Hi=()using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "# (mu1/muw)**(0.14) is negligible\n",
-    "print\"\\t cold fluid:shell side,gasoline \\t\"\n",
-    "ho=300; # assumption\n",
-    "tw=(ts)+(((Hio)/(Hio+ho))*(Tc-ts)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-ts);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, ho>300\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=12500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00015; # friction factor for reynolds number 85700, using fig.26\n",
-    "s=0.71;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.09; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10psi \\t\"\n",
-    "print\"\\t delPs is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.4 pgno:482"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.4\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t qv is :  Btu/hr \t3654000\n",
-      "\t qs is :  Btu/hr \t539000\n",
-      "\t total heat required for naphtha is :  Btu/hr \t4193000\n",
-      "\t total heat required for gasoil is :  Btu/hr \t4207500.0\n",
-      "\t delt1 is :  F \t85.0\n",
-      "\t delt2 is :  F \t190.0\n",
-      "\t LMTD is : F \t130.683201952\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.0952380952381\n",
-      "\t FT is 0.97 \t\n",
-      "\t delt is :  F \t126.762705893\n",
-      "\t ratio of two local temperature difference is :  \t0.447368421053\n",
-      "\t caloric temperature of hot fluid is :  F \t451.25\n",
-      "\t caloric temperature of cold fluid is :  F \t323.2\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.0549791666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t927624.100038\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t343.251798561\n",
-      "\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t286.272\n",
-      "\t cold fluid:shell side,naphtha \t\n",
-      "\t tw is :  F \t398.584002369\n",
-      "\t deltw :  F \t75.384002369\n",
-      "\t qv/hv :  \t12180\n",
-      "\t qs/hs :  \t8983\n",
-      "\t A :  \t21163\n",
-      "\t ho :  \t198.813967774\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t117.329454908\n",
-      "\t total surface area is :  ft**2 \t364.4256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t91.0801518561\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00245633150105\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.24018227225\n",
-      "\t delPr is :  psi \t4.82191780822\n",
-      "\t delPT is :  psi \t10.1\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area :  in**2 \t131.70828125\n",
-      "\t wetted perimeter :  in \t236.7325\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20992.3664122\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t delPs is :  psi \t0.25\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.4\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=315.; # inlet cold fluid,F\n",
-    "t2=335.; # outlet cold fluid,F\n",
-    "T1=525.;\n",
-    "T2=400.;\n",
-    "Wv=29000; # lb/hr\n",
-    "Ws=38500; # lb/hr\n",
-    "w=51000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=238; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=252; # enthalpy at t2, Btu/lb, fig 9\n",
-    "Ht3=378; # enthalpy of vapour at t2 \n",
-    "qv=(Wv*(Ht3-Ht2)); # for preheat\n",
-    "print\"\\t qv is :  Btu/hr \\t\",qv\n",
-    "qs=Ws*(Ht2-Ht1);\n",
-    "print\"\\t qs is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qv;\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "c=0.66; # Btu/(lb)(F)\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.97 \\t\" # from fig 18\n",
-    "delt=(0.97*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2)); # fig 17\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.41; # from fig.17\n",
-    "Kc=0.42;\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=116;\n",
-    "n=8; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=1.09; # at 451F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=168; # from fig.24\n",
-    "Z=0.142; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "print\"\\t cold fluid:shell side,naphtha \\t\"\n",
-    "ho1=200; # assumption\n",
-    "tw=(tc)+(((Hio)/(Hio+ho1))*(Tc-tc)); # from eq.5.31, calculation mistake\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-tc);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, hv>300, hs=60\n",
-    "Av=(qv/300);\n",
-    "As=qs/60;\n",
-    "print\"\\t qv/hv :  \\t\",Av\n",
-    "print\"\\t qs/hs :  \\t\",As\n",
-    "A1=As+Av;\n",
-    "print\"\\t A :  \\t\",A1\n",
-    "ho=(Q/A1);\n",
-    "print\"\\t ho :  \\t\",ho\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=11500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000168; # friction factor for reynolds number 59200, using fig.26\n",
-    "s=0.73;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.11; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "Af=(3.14*(21.25**2-(116))/8);\n",
-    "print\"\\t flow area :  in**2 \\t\",Af\n",
-    "As=0.917; # ft**2\n",
-    "p=(3.14*21.25/2)+(3.14*1*116/2)+(21.25)\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=0.186; # ft\n",
-    "Gs=(Ws/(2*As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.435; # at 315F, fig 14,lb/(ft)*(hr)\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "f=0.00028; # using fig.26\n",
-    "row=0.337; # fig 13.14\n",
-    "# soutlet max=0.071,\n",
-    "s=0.35; # using fig.6\n",
-    "phys=1;\n",
-    "delPs=0.25 #((f*(Gs**2)*(L))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.5 pgno:488"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.5\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for butane is :  Btu/hr \t3957600\n",
-      "\t total heat required for steam is : Btu/hr \t3966760\n",
-      "\t trail 1 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t105.068772287\n",
-      "\t total surface area is : ft**2 \t342.3472\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t92.6956025929\n",
-      "\t vapour density : lb/ft**3 \t3.18723589714\n",
-      "\t weight flow of recirculated liquid : lb/hr \t163200\n",
-      "\t volume of liquid : ft**3 \t6071.04\n",
-      "\t volume of vapour : ft**3 \t17952.0\n",
-      "\t total volume out of reboiler : ft**3 \t24023.04\n",
-      "\t vo is : ft**3/lb \t0.11776\n",
-      "\t pressure leg : psi \t1.58756230188\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.228597222222\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t892399.295218\n",
-      "\t reynolds number is : \t190648.940342\n",
-      "\t delPt is : psi \t2.1\n",
-      "negilgable\n",
-      "\t total resisitance : psi \t3.69151627479\n",
-      "\t driving force : psi \t2.98611111111\n",
-      "\t trial 2 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t140.091696383\n",
-      "\t total surface area is : ft**2 \t355.6956\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t89.21695967\n",
-      "\t pressure leg : psi \t1.19067172641\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.316680555556\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t644182.272707\n",
-      "\t reynolds number is : \t137620.75826\n",
-      "\t delPt is : psi \t0.874030618788\n",
-      "\t total resisitance : psi \t2.0647023452\n",
-      "\t driving force : psi \t2.23958333333\n",
-      "\t hot fluid : shell side,steam \t\n",
-      "\t cold fluid:inner tube side, butane \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t734.042553191\n",
-      "\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t248.0\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t212.814645309\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.006537030325\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.5\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "W=40800; # lb/hr\n",
-    "w=4570; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=241; # enthalpy of liquid at 228F, Btu/lb, fig 9\n",
-    "Ht2=338; # enthalpy of vapourat 228F, Btu/lb, fig 9\n",
-    "Q=(W*(Ht2-Ht1));\n",
-    "print\"\\t total heat required for butane is :  Btu/hr \\t\",Q\n",
-    "l=868; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is : Btu/hr \\t\",Q\n",
-    "delt=125; # delt=LMTD, isothermal boiling, eq 5.14\n",
-    "# Tc and tc: Both streams are isuthermal\n",
-    "print\"\\t trail 1 \\t\"\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=109; # assuming one tube passes, 13.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# Assume 4: 1 recirculation ratio\n",
-    "rowv=(58/(359*(688/492)*(14.7/290))); # eq 15.18\n",
-    "print\"\\t vapour density : lb/ft**3 \\t\",rowv\n",
-    "Vv=0.44; \n",
-    "Vl=0.0372; # fig 6\n",
-    "W1=4*W;\n",
-    "print\"\\t weight flow of recirculated liquid : lb/hr \\t\",W1\n",
-    "VL=W1*Vl;\n",
-    "VV=W*Vv;\n",
-    "print\"\\t volume of liquid : ft**3 \\t\",VL\n",
-    "print\"\\t volume of vapour : ft**3 \\t\",VV\n",
-    "V=VL+VV;\n",
-    "print\"\\t total volume out of reboiler : ft**3 \\t\",V\n",
-    "vo=(V/(W1+W));\n",
-    "print\"\\t vo is : ft**3/lb \\t\",vo\n",
-    "Pl=((2.3*16)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=109;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000127; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",round(delPt,2)\n",
-    "P=Pl+delPt;\n",
-    "print\"negilgable\"\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(16*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# The resistances are greater than the hydrostatic head can provide; hence the recirculation ratio will be less than 4: 1\n",
-    "print\"\\t trial 2 \\t\" # Assume 12'0\" tubes and 4:1 recirculation ratio\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=12;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=151; # assuming one tube passes, 15.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Pl=((2.3*12)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=151;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000135; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(12)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",delPt\n",
-    "P=Pl+delPt;\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(12*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# Since the driving force is slightly greater than the resistances, a recirculation ratio better than 4:1 is assured.\n",
-    "print\"\\t hot fluid : shell side,steam \\t\"\n",
-    "ho=1500; # condensing steam\n",
-    "print\"\\t cold fluid:inner tube side, butane \\t\"\n",
-    "jH=330; # from fig.24\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((300)*(0.62/0.75)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "UD=89;\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.6 pgno492"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.6\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat duty : Btu/hr \t5799016.0\n",
-      "\t total heat duty : lb/hr \t37902.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.6\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#20000=WD+WB;\n",
-    "#0.99*WD+(0.05*WB)=(20000*.5);\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "HBl=108; # fig 3 and 12\n",
-    "HDl=85.8; #fig 3 and 12\n",
-    "HDv=253.8; # fig 3 and 12\n",
-    "HFl=92; # fig 3 and 12\n",
-    "l=153; # fig 3 and 12\n",
-    "QR=((2.54+1)*WD*(HDv))-(2.54*WD*HDl)+(WB*HBl)-(20000*HFl);\n",
-    "print\"\\t total heat duty : Btu/hr \\t\",round(QR)\n",
-    "Q=QR/153;\n",
-    "print\"\\t total heat duty : lb/hr \\t\",round(Q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.7 pgno:502"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\ttotal Lb/hr is \t20000\n",
-      "\ttotal Mol/hr is \t235.5\n",
-      "\tx1 of C6H6 is \t0.543524416136\n",
-      "\tx1 of C7H8 is \t0.456475583864\n",
-      "\tTotal x1 is \t1.0\n",
-      "\tx1Pp1 of C6H6 is \t750.063694268\n",
-      "\tx1Pp1 of C7H8 is \t262.473460722\n",
-      "\tTotal x1Pp1 is \t1012.53715499\n",
-      "\ty1 of C6H6 is \t0.740776464914\n",
-      "\ty1 of C7H8 is \t0.259223535086\n",
-      "\tTotal y1 is \t1.0\n",
-      "\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\t0.558\n",
-      "\tWR` = %.2f (mol reflux)/(mol distillate)\t1.27\n",
-      "\tAssumed 200 percent of the theoretical minimum reflux as economic\t\tWR = (mol)/(mil distillate)\t2.54\n",
-      "\tThe intercept for the upper operating line = \t0.280225988701\n",
-      "\tConnecting the corresponding line in Fig. 15.23, plates required: \t13\n",
-      "\tFeed plate is th(from top)\t7\n",
-      "\tTotal reflux is \t311.15\n",
-      "\t\t\t\t\tHeat balances\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\tHeat balance \t\taround condenser:\t\n",
-      "\t  Heat in:\t\t  Top plate vapor.......433\t87.3\t\t195\t%.1f\t\t33900 253.8 8603820.0\n",
-      "\t  Heat out:\t\t  Distillate............\n",
-      "122.5\t78.3\t\t195\t\t\t9570 85.8 821106.0\n",
-      "\t  Reflux................\n",
-      "310.5\t78.3\t\t195\t\t\t24330 85.8 2087514.0\n",
-      "\t  Condenser duty, by\t\t  difference........... .....   ....    ......  ..\n",
-      ".     .....   5688000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t8600000\t\t\n",
-      "\tReboiler vapor is  lb/hr\t37908\n",
-      "\tTrapout is  lb/hr\t48338\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\n",
-      "\tHeat in:\t\t  Trapout...............522\t92.8\t\t246\t108.0\t5230000\t48338\n",
-      "\t  Reboiler duty, \t\t  by difference.......  ....    ....    .....   ...     .....   5800000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t11030000\t\t\n",
-      "\t\tReboiler requirements are\t\n",
-      "\t\tTotal liquid to reboiler\t48330 lb/hr\t\t\tVaporization\t\t\t37900 lb/hr\t\t\tTemperature(nearly isothermal)\t246DegF\t\t\tPressure\t\t\t5 psig\t\t\tHeat load\t\t\t5800000 Btu/hr\t\n",
-      "total heat out is btu/hr 7640000\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "#Basis: One hour\n",
-    "#20000=WD+WB , material balance\n",
-    "#0.99*WD+(0.05*WB)=(20000*0.5) , Benzene balance\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "\n",
-    "#Compositions and Boiling Points\n",
-    "#Feed\n",
-    "l1 = 10000; #Lb/hr , C6H4\n",
-    "l2 = 10000; #Lb/hr , C7H8\n",
-    "lb = l1+l2; #Lb/hr\n",
-    "print\"\\ttotal Lb/hr is \\t\",lb\n",
-    "mo1 = 78.1; #Mol. wt., C6H6\n",
-    "mo2 = 93.1; #Mol. wt , C7H8\n",
-    "mh1 = 128.0; #Mol/hr , C6H6\n",
-    "mh2 = 107.5; #Mol/hr , C7H8\n",
-    "mh = mh1 + mh2; # Mol/hr\n",
-    "print\"\\ttotal Mol/hr is \\t\",mh\n",
-    "x1 = mh1/mh;\n",
-    "print\"\\tx1 of C6H6 is \\t\",x1\n",
-    "x2 = mh2/mh;\n",
-    "print\"\\tx1 of C7H8 is \\t\",x2\n",
-    "x = x1+x2;\n",
-    "print\"\\tTotal x1 is \\t\",x\n",
-    "Pp1= 1380; # 214Deg F\n",
-    "Pp2=575; # 214Deg F\n",
-    "xp1 = x1*Pp1;\n",
-    "print\"\\tx1Pp1 of C6H6 is \\t\",xp1\n",
-    "xp2 = x2*Pp2;\n",
-    "print\"\\tx1Pp1 of C7H8 is \\t\",xp2\n",
-    "sxp = xp1 + xp2;\n",
-    "print\"\\tTotal x1Pp1 is \\t\",sxp\n",
-    "y1 = xp1/sxp;\n",
-    "print\"\\ty1 of C6H6 is \\t\",y1\n",
-    "y2 = xp2/sxp;\n",
-    "print\"\\ty1 of C7H8 is \\t\",y2\n",
-    "y = y1+y2;\n",
-    "print\"\\tTotal y1 is \\t\",y\n",
-    "\n",
-    "\n",
-    "w1 = 0.558; #from eq 15.42\n",
-    "print\"\\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\\t\",w1\n",
-    "wD=1;\n",
-    "xD = 0.992;\n",
-    "#V = WR' + WD\n",
-    "# WR'/V = 0.558\n",
-    "#Solving, WR' = (WR' * 0.558) + (0.558 * WD)\n",
-    "Wr = 1.27; # mol reflux/mol distillate\n",
-    "print\"\\tWR` = %.2f (mol reflux)/(mol distillate)\\t\",Wr\n",
-    "Wr1 = Wr * 2; # mol/ mol distillate\n",
-    "print\"\\tAssumed 200 percent of the theoretical minimum reflux as economic\\t\\tWR = (mol)/(mil distillate)\\t\",Wr1\n",
-    "In = (wD * xD)/(Wr1 + 1); #intercept for the upper operating line\n",
-    "print\"\\tThe intercept for the upper operating line = \\t\",In\n",
-    "p = 13; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tConnecting the corresponding line in Fig. 15.23, plates required: \\t\",p\n",
-    "fp = 7; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tFeed plate is th(from top)\\t\",fp\n",
-    "d=122.5;\n",
-    "tf = Wr1 * d;\n",
-    "print\"\\tTotal reflux is \\t\",tf\n",
-    "print\"\\t\\t\\t\\t\\tHeat balances\"\n",
-    "\n",
-    "#Heat Balances\n",
-    "l1 = 33900;\n",
-    "l2 = 9570;\n",
-    "l3 = 24330;\n",
-    "b1 = 253.8;\n",
-    "b2 = 85.8;\n",
-    "b3 = 85.8;\n",
-    "bt1 = b1*l1;\n",
-    "bt2 = b2*l2;\n",
-    "bt3 = b3*l3;\n",
-    "bt4 = 5688000;\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\\tHeat balance \\t\\taround condenser:\\t\"\n",
-    "print\"\\t  Heat in:\\t\\t  Top plate vapor.......433\\t87.3\\t\\t195\\t%.1f\\t\\t\",l1,b1,bt1\n",
-    "print\"\\t  Heat out:\\t\\t  Distillate............\"\n",
-    "print\"122.5\\t78.3\\t\\t195\\t\\t\\t\",l2,b2,bt2\n",
-    "print\"\\t  Reflux................\"\n",
-    "print\"310.5\\t78.3\\t\\t195\\t\\t\\t\",l3,b3,bt3\n",
-    "print\"\\t  Condenser duty, by\\t\\t  difference........... .....   ....    ......  ..\"\n",
-    "print\".     .....   5688000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t8600000\\t\\t\"\n",
-    "tho=7640000;\n",
-    "\n",
-    "lam = 153; # At 246 DegF, Btu/hr\n",
-    "rv = 5800000/153; #Lb/hr\n",
-    "print\"\\tReboiler vapor is  lb/hr\\t\",rv\n",
-    "to = rv + 10430; #Lb/hr\n",
-    "print\"\\tTrapout is  lb/hr\\t\",to\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\"\n",
-    "print\"\\tHeat in:\\t\\t  Trapout...............522\\t92.8\\t\\t246\\t108.0\\t5230000\\t\",to\n",
-    "print\"\\t  Reboiler duty, \\t\\t  by difference.......  ....    ....    .....   ...     .....   5800000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t11030000\\t\\t\"\n",
-    "print\"\\t\\tReboiler requirements are\\t\"\n",
-    "print\"\\t\\tTotal liquid to reboiler\\t48330 lb/hr\\t\\t\\tVaporization\\t\\t\\t37900 lb/hr\\t\\t\\tTemperature(nearly isothermal)\\t246DegF\\t\\t\\tPressure\\t\\t\\t5 psig\\t\\t\\tHeat load\\t\\t\\t5800000 Btu/hr\\t\"\n",
-    "print\"total heat out is btu/hr\",tho \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.8 pgno:506"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\t\tDEW POINT OF OVERHEAD\n",
-      "\n",
-      "\t\tMol/hr\t\tK(148DegF,40 psia)\tV/K\n",
-      "\n",
-      "\t\t--------------------------------------------\n",
-      "\n",
-      "[   6.4  219.7    2.3] [ 2.8   1.01  0.34] [ 17 221  74]\n",
-      "\n",
-      "\t\tBUBBLE POINTS OF BOTTOMS\n",
-      "\n",
-      "\t\tMol/hr\t\tK(330DegF,40psia)\t\tKL\t\tLb/hr\n",
-      "\n",
-      "\t\t--------------------------------------------------------------\n",
-      "\n",
-      "4.1 5.8 23.8 1700\n",
-      "49.3 3.0 148.0 13900\n",
-      "71.9 1.68 120.0 13030\n",
-      "52.5 0.98 51.4 6260\n",
-      "54.7 0.57 31.2 4240\n",
-      "82.5 0.35 28.9 4330\n",
-      "76.6 0.21 16.1 2640\n",
-      "22.4 0.13 2.9 520\n",
-      "\t\t____\t\t\t\t\t____\t\t____\n",
-      "\n",
-      "\t\t[  4  53 124 176 230 312 388 410]\n",
-      "\t\t\t\t\t[23.800000000000001, 171.80000000000001, 291.80000000000001, 343.19999999999999, 374.39999999999998, 403.29999999999995, 419.39999999999998, 422.29999999999995]\n",
-      "\t\t[ 1700 13900 13030  6260  4240  4330  2640   520]\n",
-      "\tAverage mol. wt. \n",
-      "[ 71.42857143  80.9080326   44.65387252  18.24009324  11.32478632\n",
-      "  10.7364245    6.29470672   1.23135212]\n",
-      "\n",
-      "\n",
-      "\t\t\t\t\t\tHEAT BALANCES:\n",
-      "\n",
-      "\t\t\t\tMol/hr\t\tMol.wt.\t\tLb/hr\t\tTemp,DegF\t\tBtu/lb\t\tBtu/hr\n",
-      "\t\n",
-      "\t\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tHeat Balance onCondeser\n",
-      "\t  Heat in:\n",
-      "\t   Top plate vapor......\n",
-      "\n",
-      "\n",
-      "\t\tCALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "\n",
-      "\t\ty*\t\t\tReboiler vapor\t\t\t\tK(300DegF,40psia)\tMol*K\n",
-      "\t\t\t\tV = y*205.7 +\tBottoms\t=\tTrapout\n",
-      "\n",
-      "\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "CALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\n",
-      "              V = y*205.7 +   Bottoms =   Trapout\n",
-      "      ----------------------------------------------------------------------------------------\n",
-      "C5 0.056       11.5        4.1     15.6        4.5     70.29\n",
-      "C6 0.35        72.0        49.3        121.3       2.25        272.91\n",
-      "C7 0.285       58.6        71.9        130.5       1.2     156.63\n",
-      "C8 0.122       25.1        52.5        77.6        0.66        51.21\n",
-      "C9 0.074       15.2        54.7        69.9        0.38        26.57\n",
-      "C10    0.068       14.0        82.5        96.5        0.22        21.23\n",
-      "C11    0.038       7.8     76.6        84.4        0.13        10.97\n",
-      "C12    0.007       1.4     22.4        23.8        0.07        1.67\n",
-      "----------------------------------------------------------------------------------------\n",
-      "1.000      205.7       414.0       619.7               611.5\n",
-      "Reboiler requirements are\n",
-      "      Vaporization lb/hr 22700\n",
-      "      Total liquor to reboiler  lb/hr 78177\n",
-      "      Heat load Btu/hr 4280000\n",
-      "      Temperature range 300-330 def F\n",
-      "      Operating pressure  psi 40\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Dew point of Overhead\n",
-    "import numpy\n",
-    "vc=numpy.array([6.4, 219.7, 2.3])\n",
-    "#vc(1) = 6.4; # Mol/hr\n",
-    "#vc(2) = 219.7; #Mol/hr\n",
-    "#vc(3) = 2.3; #Mol/hr\n",
-    "K=numpy.array([2.8, 1.01, 0.34])\n",
-    "#K(1) = 2.8; #at 148DegF and 40 psia\n",
-    "#K(2) = 1.01; #at 148DegF and 40 psia\n",
-    "#K(3) = 0.34; #at 148DegF and 40 psia\n",
-    "v=numpy.array([0, 0, 0])\n",
-    "i=0;\n",
-    "while (i<3):\n",
-    "    v[0]=vc[0]*K[0];\n",
-    "    v[1]=vc[1]*K[1];\n",
-    "    v[2]=vc[1]*K[2];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "print\"\\n\\t\\tDEW POINT OF OVERHEAD\"\n",
-    "print\"\\n\\t\\tMol/hr\\t\\tK(148DegF,40 psia)\\tV/K\\n\"\n",
-    "print\"\\t\\t--------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print vc,K,v\n",
-    "\n",
-    "bc=numpy.array([4.1, 49.3, 71.9, 52.5, 54.7, 82.5, 76.6, 22.4])\n",
-    "#bc(1)=4.1; #Mol/hr\n",
-    "#bc(2)=49.3; #Mol/hr\n",
-    "#c(3)=71.9; #Mol/hr\n",
-    "#bc(4)=52.5; #Mol/hr\n",
-    "#bc(5)=54.7; #Mol/hr\n",
-    "#bc(6)=82.5; #Mol/hr\n",
-    "#bc(7)=76.6; #Mol/hr\n",
-    "#bc(8)=22.4; #Mol/hr\n",
-    "tbc=numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "tbc[0]=tbc[0]+bc[0];\n",
-    "i=1\n",
-    "while (i<8):\n",
-    "    tbc[i]=tbc[i-1]+bc[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "bK=numpy.array([5.8, 3.0, 1.68, 0.98, 0.57, 0.35, 0.21, 0.13])\n",
-    "#bK(1)=5.8; #at 330DegF, 40 psia\n",
-    "#bK(2)=3.0; #at 330DegF, 40 psia\n",
-    "#bK(3)=1.68; #at 330DegF, 40 psia\n",
-    "#bK(4)=0.98; #at 330DegF, 40 psia\n",
-    "#bK(5)=0.57; #at 330DegF, 40 psia\n",
-    "#bK(6)=0.35; #at 330DegF, 40 psia\n",
-    "#bK(7)=0.21; #at 330DegF, 40 psia\n",
-    "#bK(8)=0.13; #at 330DegF, 40 psia\n",
-    "\n",
-    "KL=numpy.array([23.8, 148.0, 120.0, 51.4, 31.2, 28.9, 16.1, 2.9])\n",
-    "\n",
-    "#KL(1)=23.8;\n",
-    "#KL(2)=148.0;\n",
-    "#KL(3)=120.8;\n",
-    "#KL(4)=51.4;\n",
-    "#KL(5)=31.2;\n",
-    "#KL(6)=28.9;\n",
-    "#KL(7)=16.1;\n",
-    "#KL(8)=2.9;\n",
-    "\n",
-    "tk=([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "i=1;\n",
-    "op=40;\n",
-    "tk[0]=KL[0]\n",
-    "while (i<8):\n",
-    "    tk[i]=tk[i-1]+KL[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "l=numpy.array([1700, 13900, 13030, 6260, 4240, 4330, 2640, 520])    \n",
-    "#l(1)=1700; #Lb/hr\n",
-    "#l(2)=13900; #Lb/hr\n",
-    "#l(3)=13030; #Lb/hr\n",
-    "#l(4)=6260; #Lb/hr\n",
-    "#l(5)=4240; #Lb/hr\n",
-    "#l(6)=4330; #Lb/hr\n",
-    "#l(7)=2640; #Lb/hr\n",
-    "#l(8)=520; #Lb/hr\n",
-    "\n",
-    "tl=numpy.array([0, 0, 0, 0, 0, 0, 0, 0,])\n",
-    "\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "    tl[i]=tl[i]+l[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\n\\t\\tBUBBLE POINTS OF BOTTOMS\\n\"\n",
-    "print\"\\t\\tMol/hr\\t\\tK(330DegF,40psia)\\t\\tKL\\t\\tLb/hr\\n\"\n",
-    "print\"\\t\\t--------------------------------------------------------------\\n\"\n",
-    "tlr=78177;\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "\n",
-    "    print bc[i],bK[i],KL[i],l[i]\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\t____\\t\\t\\t\\t\\t____\\t\\t____\\n\"\n",
-    "\n",
-    "print\"\\t\\t\",tbc \n",
-    "print\"\\t\\t\\t\\t\\t\",tk \n",
-    "print\"\\t\\t\",tl\n",
-    "av = numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "av=tl/tk\n",
-    "hl=4280000;\n",
-    "print\"\\tAverage mol. wt. \\n\",av\n",
-    "\n",
-    "lh=numpy.array([48894, 16298, 32596])\n",
-    "bl=numpy.array([286, 129, 129])\n",
-    "#lh(1)=48894;#Lb/hr\n",
-    "#lh(2)=16298;#Lb/hr\n",
-    "#lh(3)=32596;#Lb/hr\n",
-    "#bl(1)=286;#Btu/hr\n",
-    "#bl(2)=129;#Btu/hr\n",
-    "#bl(3)=129;#Btu/hr\n",
-    "\n",
-    "bh=numpy.array([0, 0, 0])\n",
-    "vap=22700;\n",
-    "i=0;\n",
-    "\n",
-    "while (i<3):\n",
-    "    bh[0]=lh[0]*bl[0];\n",
-    "    i=i+1;\n",
-    "\n",
-    "#Heat Balances\n",
-    "print\"\\n\\n\\t\\t\\t\\t\\t\\tHEAT BALANCES:\"\n",
-    "print\"\\n\\t\\t\\t\\tMol/hr\\t\\tMol.wt.\\t\\tLb/hr\\t\\tTemp,DegF\\t\\tBtu/lb\\t\\tBtu/hr\\n\\t\"\n",
-    "print\"\\t\\t\\t----------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\tHeat Balance onCondeser\\n\\t  Heat in:\\n\\t   Top plate vapor......\"\n",
-    "\n",
-    "#Heat Balances on reboiler\n",
-    "#Assume 30Deg difference between reboiler and bottom plate giving bottom-plate temperature of 300DegF\n",
-    "#Mol/hr from Eq. 15.47\n",
-    "\n",
-    "pc=numpy.array([0.056, 0.35, 0.285, 0.122, 0.074, 0.068, 0.038, 0.007])\n",
-    "#pc(1)=0.056;\n",
-    "#pc(2)=0.350;\n",
-    "##pc(3)=0.285;\n",
-    "#pc(4)=0.122;\n",
-    "#pc(5)=0.074;\n",
-    "#pc(6)=0.068;\n",
-    "#pc(7)=0.038;\n",
-    "#pc(8)=0.007;\n",
-    "\n",
-    "pk=numpy.array([4.5, 2.25, 1.2, 0.66, 0.38, 0.22, 0.13, 0.07])\n",
-    "#pK(1)=4.5;\n",
-    "#pK(2)=2.25;\n",
-    "#pK(3)=1.20;\n",
-    "#pK(4)=0.66;\n",
-    "#pK(5)=0.38;\n",
-    "#pK(6)=0.22;\n",
-    "#pK(7)=0.13;\n",
-    "#pK(8)=0.07;\n",
-    "\n",
-    "print\"\\n\\n\\t\\tCALCULATION OF BOTTOM PLATE TEMPERATURE\\n\"\n",
-    "print\"\\t\\ty*\\t\\t\\tReboiler vapor\\t\\t\\t\\tK(300DegF,40psia)\\tMol*K\\n\\t\\t\\t\\tV = y*205.7 +\\tBottoms\\t=\\tTrapout\\n\"\n",
-    "print\"\\t\\t----------------------------------------------------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print \"CALCULATION OF BOTTOM PLATE TEMPERATURE\"\n",
-    "print\"      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\"\n",
-    "print\"              V = y*205.7 +   Bottoms =   Trapout\"\n",
-    "print\"      ----------------------------------------------------------------------------------------\"\n",
-    "print   \"C5 0.056       11.5        4.1     15.6        4.5     70.29\"\n",
-    "print   \"C6 0.35        72.0        49.3        121.3       2.25        272.91\"\n",
-    "print   \"C7 0.285       58.6        71.9        130.5       1.2     156.63\"\n",
-    "print   \"C8 0.122       25.1        52.5        77.6        0.66        51.21\"\n",
-    "print   \"C9 0.074       15.2        54.7        69.9        0.38        26.57\"\n",
-    "print   \"C10    0.068       14.0        82.5        96.5        0.22        21.23\"\n",
-    "print   \"C11    0.038       7.8     76.6        84.4        0.13        10.97\"\n",
-    "print   \"C12    0.007       1.4     22.4        23.8        0.07        1.67\"\n",
-    "print       \"----------------------------------------------------------------------------------------\"\n",
-    "print       \"1.000      205.7       414.0       619.7               611.5\"\n",
-    "\n",
-    "\n",
-    "print\"Reboiler requirements are\"\n",
-    "print\"      Vaporization lb/hr\",vap\n",
-    "print\"      Total liquor to reboiler  lb/hr\",tlr    \n",
-    "print\"      Heat load Btu/hr\",hl\n",
-    "print\"      Temperature range 300-330 def F\"\n",
-    "print\"      Operating pressure  psi\",op "
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_2.ipynb
deleted file mode 100755
index d185cf80..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_2.ipynb
+++ /dev/null
@@ -1,1315 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 15 : Vaporizers Evapourators and Reboilers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.1 pgno:463"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9453000.0\n",
-      "\t total heat required for kerosene is :  Btu/hr \t9450000.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t91.1262293169\n",
-      "\t A :  ft**2 \t1037.02304713\n",
-      "\t By the law of mixtures \t\n",
-      "\t v2 : %.0f ft**3/lb \t11.0034\n",
-      "\t vav :  ft**3/lb \t3.16417120715\n",
-      "\t By the approximate method \t\n",
-      "\t vav :  ft**3/lb \t5.5102\n",
-      "\t actual density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.00505661639416\n",
-      "\t approximate density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.0029\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=250;\n",
-    "T1=400;\n",
-    "T2=300;\n",
-    "w=10000; # lb/hr\n",
-    "W=150000; # lb/hr\n",
-    "l=945.3; # Btu/(lb) , table 7\n",
-    "from math import log10\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "C=0.63; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-ts; #F\n",
-    "delt2=T1-ts; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "UD=100;\n",
-    "A=(Q/(UD*LMTD));\n",
-    "print\"\\t A :  ft**2 \\t\",A\n",
-    "WC=94500; # Btu/F\n",
-    "vl=0.017; # ft**3/lb, from table 7\n",
-    "vv=13.75; # ft**3/lb, from table 7\n",
-    "print\"\\t By the law of mixtures \\t\"\n",
-    "# Assume 80 per cent of the outlet fluid is vapor\n",
-    "v2=(0.8*vv)+(.2*vl);\n",
-    "print\"\\t v2 : ft**3/lb \\t\",v2\n",
-    "vav=(WC*(v2-vl)/(UD*A))-((WC*(T2-ts)/(l*w))*(vv-vl))+vl;\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav\n",
-    "print\"\\t By the approximate method \\t\"\n",
-    "vav1=(vl+v2)/(2);\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav1\n",
-    "row=62.5;\n",
-    "rowac=(1/vav);\n",
-    "s=(rowac/row);\n",
-    "print\"\\t actual density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",s\n",
-    "rowap=(1/vav1);\n",
-    "s=(rowap/row);\n",
-    "print\"\\t approximate density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",round(s,4)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.2 pgno:464"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for preheat of butane is :  Btu/hr \t2124200\n",
-      "\t total heat required for vapourisation of butane is :  Btu/hr \t2172500\n",
-      "\t total heat required for  butane is :  Btu/hr \t4296700\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t4297328.0\n",
-      "\t Wp1 is :  lb/hr \t13401.8927445\n",
-      "\t Wv1 is :  lb/hr \t21092\n",
-      "\t W is :  lb/hr \t34493.8927445\n",
-      "\t weighted delt is : % F \t124.582285677\n",
-      "\t caloric temperature of hot fluid is :  F \t338\n",
-      "\t caloric temperature of cold fluid is :  F \t171\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.15675\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t31132.3763955\n",
-      "\t reynolds number is :  \t62178.9886688\n",
-      "\t hio is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,butane \t\n",
-      "\t preheating \t\n",
-      "\t flow area is :  ft**2 \t0.105902777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t233232.786885\n",
-      "\t reynolds number is :  \t69214.7658922\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t231.272727273\n",
-      "\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \t200.378071834\n",
-      "\t clean surface required for preheating :  ft**2 \t66.883030772\n",
-      "\t for vapourisation \t\n",
-      "\t reynolds number is :  \t79511.1773472\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t236.96969697\n",
-      "\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \t204.640614096\n",
-      "\t clean surface required for vapourisation :  ft**2 \t103.069633088\n",
-      "\t total clean surface :  ft**2 \t169.952663859\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t202.96313674\n",
-      "\t total surface area is :  ft**2 \t318.3488\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.352513798\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00430213212754\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.16\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t preheating \t\n",
-      "\t length of preheat zone :  ft \t6.29662676683\n",
-      "\t number of crosses are :  \t15.1119042404\n",
-      "\t delPsp is :  psi \t0.703032923143\n",
-      "\t vapourisation \t\n",
-      "\t number of crosses are :  \t23.28\n",
-      "\t delPsv is :  psi \t1.89396418309\n",
-      "\t delPS is :  psi \t2.6\n",
-      "\t allowable delPa is 5 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=108; # inlet cold fluid,F\n",
-    "t2=235; # outlet cold fluid,F\n",
-    "Ts=338;\n",
-    "Wp=24700; # lb/hr\n",
-    "Wv=19750; # lb/hr\n",
-    "w=4880; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=162; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=248; # enthalpy at t2, Btu/lb, fig 9\n",
-    "qp=(Wp*(Ht2-Ht1)); # for preheat\n",
-    "print\"\\t total heat required for preheat of butane is :  Btu/hr \\t\",qp\n",
-    "Ht3=358; # enthalpy of vapour at t2, Btu/lb, fig 9\n",
-    "qv=Wv*(Ht3-Ht2);\n",
-    "print\"\\t total heat required for vapourisation of butane is :  Btu/hr \\t\",qv\n",
-    "Q=qp+qv;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=880.6; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "deltp=158.5; # F, from eq 5.14\n",
-    "deltv=103; # F eq 5.14\n",
-    "Wp1=(qp/deltp);\n",
-    "print\"\\t Wp1 is :  lb/hr \\t\",Wp1\n",
-    "Wv1=(qv/deltv);\n",
-    "print\"\\t Wv1 is :  lb/hr \\t\",Wv1\n",
-    "W=(Wp1+Wv1);\n",
-    "print\"\\t W is :  lb/hr \\t\",W\n",
-    "delt=(Q/W);\n",
-    "print\"\\t weighted delt is : % F \\t\",delt\n",
-    "Tc=((Ts)+(Ts))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=76;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.594; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.0363; # at 338F, fig 15,lb/(ft)*(hr)\n",
-    "D=0.0725; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensing steam,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hio is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,butane \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(Wp/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.278; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0825; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=159; # from fig.28\n",
-    "Z=0.12; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hop=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hop\n",
-    "Up=((hio)*(hop)/(hio+hop)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \\t\",Up\n",
-    "Ap=(qp/(Up*deltp));\n",
-    "print\"\\t clean surface required for preheating :  ft**2 \\t\",Ap\n",
-    "print\"\\t for vapourisation \\t\"\n",
-    "mu2=0.242; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=170; # from fig.28\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hov=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hov\n",
-    "Uv=((hio)*(hov)/(hio+hov)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \\t\",Uv\n",
-    "Av=(qv/(Uv*deltv));\n",
-    "print\"\\t clean surface required for vapourisation :  ft**2 \\t\",Av\n",
-    "Ac=Ap+Av;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",Ac\n",
-    "UC=((Up*Ap)+(Uv*Av))/(Ac);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# A total of 170 ft2 are required of which 103 are to be used for vaporization. For the total surface required 318 ft2 will be provided. It can be assumed, then, that the surface provided for vaporization is 193ft**2\n",
-    "# then flux is Q/A=10700, which is with in satisfactory levels.\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000165; # friction factor for reynolds number 62000, using fig.26\n",
-    "s=0.00413;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "f=0.00145; # friction factor for reynolds number 69200, using fig.29\n",
-    "Lp=(L*Ap/Ac); #ft\n",
-    "print\"\\t length of preheat zone :  ft \\t\",Lp\n",
-    "N=(12*Lp/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "s=0.5; # for reynolds number 69200,using fig.6\n",
-    "Ds=1.27; # fig 28\n",
-    "phys=1;\n",
-    "delPsp=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPsp is :  psi \\t\",delPsp\n",
-    "print\"\\t vapourisation \\t\"\n",
-    "f=0.00142;\n",
-    "Lv=9.7; # Lv=L-Lp\n",
-    "Nv=(12*Lv/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",Nv\n",
-    "s=0.28; \n",
-    "delPsv=((f*(Gs**2)*(Ds)*(Nv))/(5.22*(10**10)*(De)*(s)*(1))); # using eq 12.47,psi\n",
-    "print\"\\t delPsv is :  psi \\t\",delPsv\n",
-    "delPS=delPsp+delPsv;\n",
-    "print\"\\t delPS is :  psi \\t\",round(delPS,2)\n",
-    "print\"\\t allowable delPa is 5 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.3 pgno:475"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gasoline is :  Btu/hr \t2669500\n",
-      "\t total heat required for gasoil is :  Btu/hr \t2671900.0\n",
-      "\t S is :  \t0.428571428571\n",
-      "\t Tc is :  F \t517.0\n",
-      "\t hot fluid:inner tube side,gasoil \t\n",
-      "\t flow area is :  ft**2 \t0.0429722222222\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t807498.383969\n",
-      "\t reynolds number is :  \t86215.9813038\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t374.063400576\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t311.968876081\n",
-      "\t cold fluid:shell side,gasoline \t\n",
-      "\t tw is :  F \t459.64414193\n",
-      "\t deltw :  F \t59.6441419296\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t152.933697255\n",
-      "\t total surface area is :  ft**2 \t213.6288\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t105.993294626\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00289577777619\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.73790740915\n",
-      "\t delPr is :  psi \t3.04225352113\n",
-      "\t delPT is :  psi \t5.8\n",
-      "\t allowable delPa is 10psi \t\n",
-      "\t delPs is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=400;\n",
-    "T1=575;\n",
-    "T2=475;\n",
-    "W=28100; # lb/hr\n",
-    "w=34700; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "HT1=290; # enthalpy at T1, Btu/lb, fig 11\n",
-    "HT2=385; # enthalpy at T2, Btu/lb, fig 11\n",
-    "Q=(W*(HT2-HT1)); # for preheat\n",
-    "print\"\\t total heat required for gasoline is :  Btu/hr \\t\",Q\n",
-    "c=0.77; # Btu/(lb), table 7\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt=118; # F eq 5.14\n",
-    "S=75./175.;#((T2-ts)/(T1-ts));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "Kc=0.37; # fig 17\n",
-    "Fc=0.42;\n",
-    "Tc=(T2+(0.42*(T1-T2)));\n",
-    "print\"\\t Tc is :  F \\t\",Tc\n",
-    "print\"\\t hot fluid:inner tube side,gasoil \\t\"\n",
-    "Nt=68;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.65; # at 517F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0694; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=220; # from fig.24\n",
-    "Z=0.118; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #hi/phyt, Hi=()using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "# (mu1/muw)**(0.14) is negligible\n",
-    "print\"\\t cold fluid:shell side,gasoline \\t\"\n",
-    "ho=300; # assumption\n",
-    "tw=(ts)+(((Hio)/(Hio+ho))*(Tc-ts)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-ts);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, ho>300\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=12500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00015; # friction factor for reynolds number 85700, using fig.26\n",
-    "s=0.71;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.09; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10psi \\t\"\n",
-    "print\"\\t delPs is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.4 pgno:482"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.4\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t qv is :  Btu/hr \t3654000\n",
-      "\t qs is :  Btu/hr \t539000\n",
-      "\t total heat required for naphtha is :  Btu/hr \t4193000\n",
-      "\t total heat required for gasoil is :  Btu/hr \t4207500.0\n",
-      "\t delt1 is :  F \t85.0\n",
-      "\t delt2 is :  F \t190.0\n",
-      "\t LMTD is : F \t130.683201952\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.0952380952381\n",
-      "\t FT is 0.97 \t\n",
-      "\t delt is :  F \t126.762705893\n",
-      "\t ratio of two local temperature difference is :  \t0.447368421053\n",
-      "\t caloric temperature of hot fluid is :  F \t451.25\n",
-      "\t caloric temperature of cold fluid is :  F \t323.2\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.0549791666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t927624.100038\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t343.251798561\n",
-      "\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t286.272\n",
-      "\t cold fluid:shell side,naphtha \t\n",
-      "\t tw is :  F \t398.584002369\n",
-      "\t deltw :  F \t75.384002369\n",
-      "\t qv/hv :  \t12180\n",
-      "\t qs/hs :  \t8983\n",
-      "\t A :  \t21163\n",
-      "\t ho :  \t198.813967774\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t117.329454908\n",
-      "\t total surface area is :  ft**2 \t364.4256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t91.0801518561\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00245633150105\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.24018227225\n",
-      "\t delPr is :  psi \t4.82191780822\n",
-      "\t delPT is :  psi \t10.1\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area :  in**2 \t131.70828125\n",
-      "\t wetted perimeter :  in \t236.7325\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20992.3664122\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t delPs is :  psi \t0.25\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.4\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=315.; # inlet cold fluid,F\n",
-    "t2=335.; # outlet cold fluid,F\n",
-    "T1=525.;\n",
-    "T2=400.;\n",
-    "Wv=29000; # lb/hr\n",
-    "Ws=38500; # lb/hr\n",
-    "w=51000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=238; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=252; # enthalpy at t2, Btu/lb, fig 9\n",
-    "Ht3=378; # enthalpy of vapour at t2 \n",
-    "qv=(Wv*(Ht3-Ht2)); # for preheat\n",
-    "print\"\\t qv is :  Btu/hr \\t\",qv\n",
-    "qs=Ws*(Ht2-Ht1);\n",
-    "print\"\\t qs is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qv;\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "c=0.66; # Btu/(lb)(F)\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.97 \\t\" # from fig 18\n",
-    "delt=(0.97*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2)); # fig 17\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.41; # from fig.17\n",
-    "Kc=0.42;\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=116;\n",
-    "n=8; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=1.09; # at 451F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=168; # from fig.24\n",
-    "Z=0.142; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "print\"\\t cold fluid:shell side,naphtha \\t\"\n",
-    "ho1=200; # assumption\n",
-    "tw=(tc)+(((Hio)/(Hio+ho1))*(Tc-tc)); # from eq.5.31, calculation mistake\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-tc);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, hv>300, hs=60\n",
-    "Av=(qv/300);\n",
-    "As=qs/60;\n",
-    "print\"\\t qv/hv :  \\t\",Av\n",
-    "print\"\\t qs/hs :  \\t\",As\n",
-    "A1=As+Av;\n",
-    "print\"\\t A :  \\t\",A1\n",
-    "ho=(Q/A1);\n",
-    "print\"\\t ho :  \\t\",ho\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=11500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000168; # friction factor for reynolds number 59200, using fig.26\n",
-    "s=0.73;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.11; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "Af=(3.14*(21.25**2-(116))/8);\n",
-    "print\"\\t flow area :  in**2 \\t\",Af\n",
-    "As=0.917; # ft**2\n",
-    "p=(3.14*21.25/2)+(3.14*1*116/2)+(21.25)\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=0.186; # ft\n",
-    "Gs=(Ws/(2*As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.435; # at 315F, fig 14,lb/(ft)*(hr)\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "f=0.00028; # using fig.26\n",
-    "row=0.337; # fig 13.14\n",
-    "# soutlet max=0.071,\n",
-    "s=0.35; # using fig.6\n",
-    "phys=1;\n",
-    "delPs=0.25 #((f*(Gs**2)*(L))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.5 pgno:488"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.5\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for butane is :  Btu/hr \t3957600\n",
-      "\t total heat required for steam is : Btu/hr \t3966760\n",
-      "\t trail 1 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t105.068772287\n",
-      "\t total surface area is : ft**2 \t342.3472\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t92.6956025929\n",
-      "\t vapour density : lb/ft**3 \t3.18723589714\n",
-      "\t weight flow of recirculated liquid : lb/hr \t163200\n",
-      "\t volume of liquid : ft**3 \t6071.04\n",
-      "\t volume of vapour : ft**3 \t17952.0\n",
-      "\t total volume out of reboiler : ft**3 \t24023.04\n",
-      "\t vo is : ft**3/lb \t0.11776\n",
-      "\t pressure leg : psi \t1.58756230188\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.228597222222\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t892399.295218\n",
-      "\t reynolds number is : \t190648.940342\n",
-      "\t delPt is : psi \t2.1\n",
-      "negilgable\n",
-      "\t total resisitance : psi \t3.69151627479\n",
-      "\t driving force : psi \t2.98611111111\n",
-      "\t trial 2 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t140.091696383\n",
-      "\t total surface area is : ft**2 \t355.6956\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t89.21695967\n",
-      "\t pressure leg : psi \t1.19067172641\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.316680555556\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t644182.272707\n",
-      "\t reynolds number is : \t137620.75826\n",
-      "\t delPt is : psi \t0.874030618788\n",
-      "\t total resisitance : psi \t2.0647023452\n",
-      "\t driving force : psi \t2.23958333333\n",
-      "\t hot fluid : shell side,steam \t\n",
-      "\t cold fluid:inner tube side, butane \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t734.042553191\n",
-      "\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t248.0\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t212.814645309\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.006537030325\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.5\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "W=40800; # lb/hr\n",
-    "w=4570; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=241; # enthalpy of liquid at 228F, Btu/lb, fig 9\n",
-    "Ht2=338; # enthalpy of vapourat 228F, Btu/lb, fig 9\n",
-    "Q=(W*(Ht2-Ht1));\n",
-    "print\"\\t total heat required for butane is :  Btu/hr \\t\",Q\n",
-    "l=868; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is : Btu/hr \\t\",Q\n",
-    "delt=125; # delt=LMTD, isothermal boiling, eq 5.14\n",
-    "# Tc and tc: Both streams are isuthermal\n",
-    "print\"\\t trail 1 \\t\"\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=109; # assuming one tube passes, 13.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# Assume 4: 1 recirculation ratio\n",
-    "rowv=(58/(359*(688/492)*(14.7/290))); # eq 15.18\n",
-    "print\"\\t vapour density : lb/ft**3 \\t\",rowv\n",
-    "Vv=0.44; \n",
-    "Vl=0.0372; # fig 6\n",
-    "W1=4*W;\n",
-    "print\"\\t weight flow of recirculated liquid : lb/hr \\t\",W1\n",
-    "VL=W1*Vl;\n",
-    "VV=W*Vv;\n",
-    "print\"\\t volume of liquid : ft**3 \\t\",VL\n",
-    "print\"\\t volume of vapour : ft**3 \\t\",VV\n",
-    "V=VL+VV;\n",
-    "print\"\\t total volume out of reboiler : ft**3 \\t\",V\n",
-    "vo=(V/(W1+W));\n",
-    "print\"\\t vo is : ft**3/lb \\t\",vo\n",
-    "Pl=((2.3*16)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=109;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000127; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",round(delPt,2)\n",
-    "P=Pl+delPt;\n",
-    "print\"negilgable\"\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(16*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# The resistances are greater than the hydrostatic head can provide; hence the recirculation ratio will be less than 4: 1\n",
-    "print\"\\t trial 2 \\t\" # Assume 12'0\" tubes and 4:1 recirculation ratio\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=12;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=151; # assuming one tube passes, 15.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Pl=((2.3*12)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=151;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000135; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(12)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",delPt\n",
-    "P=Pl+delPt;\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(12*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# Since the driving force is slightly greater than the resistances, a recirculation ratio better than 4:1 is assured.\n",
-    "print\"\\t hot fluid : shell side,steam \\t\"\n",
-    "ho=1500; # condensing steam\n",
-    "print\"\\t cold fluid:inner tube side, butane \\t\"\n",
-    "jH=330; # from fig.24\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((300)*(0.62/0.75)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "UD=89;\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.6 pgno492"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.6\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat duty : Btu/hr \t5799016.0\n",
-      "\t total heat duty : lb/hr \t37902.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.6\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#20000=WD+WB;\n",
-    "#0.99*WD+(0.05*WB)=(20000*.5);\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "HBl=108; # fig 3 and 12\n",
-    "HDl=85.8; #fig 3 and 12\n",
-    "HDv=253.8; # fig 3 and 12\n",
-    "HFl=92; # fig 3 and 12\n",
-    "l=153; # fig 3 and 12\n",
-    "QR=((2.54+1)*WD*(HDv))-(2.54*WD*HDl)+(WB*HBl)-(20000*HFl);\n",
-    "print\"\\t total heat duty : Btu/hr \\t\",round(QR)\n",
-    "Q=QR/153;\n",
-    "print\"\\t total heat duty : lb/hr \\t\",round(Q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.7 pgno:502"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\ttotal Lb/hr is \t20000\n",
-      "\ttotal Mol/hr is \t235.5\n",
-      "\tx1 of C6H6 is \t0.543524416136\n",
-      "\tx1 of C7H8 is \t0.456475583864\n",
-      "\tTotal x1 is \t1.0\n",
-      "\tx1Pp1 of C6H6 is \t750.063694268\n",
-      "\tx1Pp1 of C7H8 is \t262.473460722\n",
-      "\tTotal x1Pp1 is \t1012.53715499\n",
-      "\ty1 of C6H6 is \t0.740776464914\n",
-      "\ty1 of C7H8 is \t0.259223535086\n",
-      "\tTotal y1 is \t1.0\n",
-      "\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\t0.558\n",
-      "\tWR` = %.2f (mol reflux)/(mol distillate)\t1.27\n",
-      "\tAssumed 200 percent of the theoretical minimum reflux as economic\t\tWR = (mol)/(mil distillate)\t2.54\n",
-      "\tThe intercept for the upper operating line = \t0.280225988701\n",
-      "\tConnecting the corresponding line in Fig. 15.23, plates required: \t13\n",
-      "\tFeed plate is th(from top)\t7\n",
-      "\tTotal reflux is \t311.15\n",
-      "\t\t\t\t\tHeat balances\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\tHeat balance \t\taround condenser:\t\n",
-      "\t  Heat in:\t\t  Top plate vapor.......433\t87.3\t\t195\t%.1f\t\t33900 253.8 8603820.0\n",
-      "\t  Heat out:\t\t  Distillate............\n",
-      "122.5\t78.3\t\t195\t\t\t9570 85.8 821106.0\n",
-      "\t  Reflux................\n",
-      "310.5\t78.3\t\t195\t\t\t24330 85.8 2087514.0\n",
-      "\t  Condenser duty, by\t\t  difference........... .....   ....    ......  ..\n",
-      ".     .....   5688000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t8600000\t\t\n",
-      "\tReboiler vapor is  lb/hr\t37908\n",
-      "\tTrapout is  lb/hr\t48338\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\n",
-      "\tHeat in:\t\t  Trapout...............522\t92.8\t\t246\t108.0\t5230000\t48338\n",
-      "\t  Reboiler duty, \t\t  by difference.......  ....    ....    .....   ...     .....   5800000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t11030000\t\t\n",
-      "\t\tReboiler requirements are\t\n",
-      "\t\tTotal liquid to reboiler\t48330 lb/hr\t\t\tVaporization\t\t\t37900 lb/hr\t\t\tTemperature(nearly isothermal)\t246DegF\t\t\tPressure\t\t\t5 psig\t\t\tHeat load\t\t\t5800000 Btu/hr\t\n",
-      "total heat out is btu/hr 7640000\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "#Basis: One hour\n",
-    "#20000=WD+WB , material balance\n",
-    "#0.99*WD+(0.05*WB)=(20000*0.5) , Benzene balance\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "\n",
-    "#Compositions and Boiling Points\n",
-    "#Feed\n",
-    "l1 = 10000; #Lb/hr , C6H4\n",
-    "l2 = 10000; #Lb/hr , C7H8\n",
-    "lb = l1+l2; #Lb/hr\n",
-    "print\"\\ttotal Lb/hr is \\t\",lb\n",
-    "mo1 = 78.1; #Mol. wt., C6H6\n",
-    "mo2 = 93.1; #Mol. wt , C7H8\n",
-    "mh1 = 128.0; #Mol/hr , C6H6\n",
-    "mh2 = 107.5; #Mol/hr , C7H8\n",
-    "mh = mh1 + mh2; # Mol/hr\n",
-    "print\"\\ttotal Mol/hr is \\t\",mh\n",
-    "x1 = mh1/mh;\n",
-    "print\"\\tx1 of C6H6 is \\t\",x1\n",
-    "x2 = mh2/mh;\n",
-    "print\"\\tx1 of C7H8 is \\t\",x2\n",
-    "x = x1+x2;\n",
-    "print\"\\tTotal x1 is \\t\",x\n",
-    "Pp1= 1380; # 214Deg F\n",
-    "Pp2=575; # 214Deg F\n",
-    "xp1 = x1*Pp1;\n",
-    "print\"\\tx1Pp1 of C6H6 is \\t\",xp1\n",
-    "xp2 = x2*Pp2;\n",
-    "print\"\\tx1Pp1 of C7H8 is \\t\",xp2\n",
-    "sxp = xp1 + xp2;\n",
-    "print\"\\tTotal x1Pp1 is \\t\",sxp\n",
-    "y1 = xp1/sxp;\n",
-    "print\"\\ty1 of C6H6 is \\t\",y1\n",
-    "y2 = xp2/sxp;\n",
-    "print\"\\ty1 of C7H8 is \\t\",y2\n",
-    "y = y1+y2;\n",
-    "print\"\\tTotal y1 is \\t\",y\n",
-    "\n",
-    "\n",
-    "w1 = 0.558; #from eq 15.42\n",
-    "print\"\\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\\t\",w1\n",
-    "wD=1;\n",
-    "xD = 0.992;\n",
-    "#V = WR' + WD\n",
-    "# WR'/V = 0.558\n",
-    "#Solving, WR' = (WR' * 0.558) + (0.558 * WD)\n",
-    "Wr = 1.27; # mol reflux/mol distillate\n",
-    "print\"\\tWR` = %.2f (mol reflux)/(mol distillate)\\t\",Wr\n",
-    "Wr1 = Wr * 2; # mol/ mol distillate\n",
-    "print\"\\tAssumed 200 percent of the theoretical minimum reflux as economic\\t\\tWR = (mol)/(mil distillate)\\t\",Wr1\n",
-    "In = (wD * xD)/(Wr1 + 1); #intercept for the upper operating line\n",
-    "print\"\\tThe intercept for the upper operating line = \\t\",In\n",
-    "p = 13; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tConnecting the corresponding line in Fig. 15.23, plates required: \\t\",p\n",
-    "fp = 7; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tFeed plate is th(from top)\\t\",fp\n",
-    "d=122.5;\n",
-    "tf = Wr1 * d;\n",
-    "print\"\\tTotal reflux is \\t\",tf\n",
-    "print\"\\t\\t\\t\\t\\tHeat balances\"\n",
-    "\n",
-    "#Heat Balances\n",
-    "l1 = 33900;\n",
-    "l2 = 9570;\n",
-    "l3 = 24330;\n",
-    "b1 = 253.8;\n",
-    "b2 = 85.8;\n",
-    "b3 = 85.8;\n",
-    "bt1 = b1*l1;\n",
-    "bt2 = b2*l2;\n",
-    "bt3 = b3*l3;\n",
-    "bt4 = 5688000;\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\\tHeat balance \\t\\taround condenser:\\t\"\n",
-    "print\"\\t  Heat in:\\t\\t  Top plate vapor.......433\\t87.3\\t\\t195\\t%.1f\\t\\t\",l1,b1,bt1\n",
-    "print\"\\t  Heat out:\\t\\t  Distillate............\"\n",
-    "print\"122.5\\t78.3\\t\\t195\\t\\t\\t\",l2,b2,bt2\n",
-    "print\"\\t  Reflux................\"\n",
-    "print\"310.5\\t78.3\\t\\t195\\t\\t\\t\",l3,b3,bt3\n",
-    "print\"\\t  Condenser duty, by\\t\\t  difference........... .....   ....    ......  ..\"\n",
-    "print\".     .....   5688000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t8600000\\t\\t\"\n",
-    "tho=7640000;\n",
-    "\n",
-    "lam = 153; # At 246 DegF, Btu/hr\n",
-    "rv = 5800000/153; #Lb/hr\n",
-    "print\"\\tReboiler vapor is  lb/hr\\t\",rv\n",
-    "to = rv + 10430; #Lb/hr\n",
-    "print\"\\tTrapout is  lb/hr\\t\",to\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\"\n",
-    "print\"\\tHeat in:\\t\\t  Trapout...............522\\t92.8\\t\\t246\\t108.0\\t5230000\\t\",to\n",
-    "print\"\\t  Reboiler duty, \\t\\t  by difference.......  ....    ....    .....   ...     .....   5800000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t11030000\\t\\t\"\n",
-    "print\"\\t\\tReboiler requirements are\\t\"\n",
-    "print\"\\t\\tTotal liquid to reboiler\\t48330 lb/hr\\t\\t\\tVaporization\\t\\t\\t37900 lb/hr\\t\\t\\tTemperature(nearly isothermal)\\t246DegF\\t\\t\\tPressure\\t\\t\\t5 psig\\t\\t\\tHeat load\\t\\t\\t5800000 Btu/hr\\t\"\n",
-    "print\"total heat out is btu/hr\",tho \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.8 pgno:506"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\t\tDEW POINT OF OVERHEAD\n",
-      "\n",
-      "\t\tMol/hr\t\tK(148DegF,40 psia)\tV/K\n",
-      "\n",
-      "\t\t--------------------------------------------\n",
-      "\n",
-      "[   6.4  219.7    2.3] [ 2.8   1.01  0.34] [ 17 221  74]\n",
-      "\n",
-      "\t\tBUBBLE POINTS OF BOTTOMS\n",
-      "\n",
-      "\t\tMol/hr\t\tK(330DegF,40psia)\t\tKL\t\tLb/hr\n",
-      "\n",
-      "\t\t--------------------------------------------------------------\n",
-      "\n",
-      "4.1 5.8 23.8 1700\n",
-      "49.3 3.0 148.0 13900\n",
-      "71.9 1.68 120.0 13030\n",
-      "52.5 0.98 51.4 6260\n",
-      "54.7 0.57 31.2 4240\n",
-      "82.5 0.35 28.9 4330\n",
-      "76.6 0.21 16.1 2640\n",
-      "22.4 0.13 2.9 520\n",
-      "\t\t____\t\t\t\t\t____\t\t____\n",
-      "\n",
-      "\t\t[  4  53 124 176 230 312 388 410]\n",
-      "\t\t\t\t\t[23.800000000000001, 171.80000000000001, 291.80000000000001, 343.19999999999999, 374.39999999999998, 403.29999999999995, 419.39999999999998, 422.29999999999995]\n",
-      "\t\t[ 1700 13900 13030  6260  4240  4330  2640   520]\n",
-      "\tAverage mol. wt. \n",
-      "[ 71.42857143  80.9080326   44.65387252  18.24009324  11.32478632\n",
-      "  10.7364245    6.29470672   1.23135212]\n",
-      "\n",
-      "\n",
-      "\t\t\t\t\t\tHEAT BALANCES:\n",
-      "\n",
-      "\t\t\t\tMol/hr\t\tMol.wt.\t\tLb/hr\t\tTemp,DegF\t\tBtu/lb\t\tBtu/hr\n",
-      "\t\n",
-      "\t\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tHeat Balance onCondeser\n",
-      "\t  Heat in:\n",
-      "\t   Top plate vapor......\n",
-      "\n",
-      "\n",
-      "\t\tCALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "\n",
-      "\t\ty*\t\t\tReboiler vapor\t\t\t\tK(300DegF,40psia)\tMol*K\n",
-      "\t\t\t\tV = y*205.7 +\tBottoms\t=\tTrapout\n",
-      "\n",
-      "\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "CALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\n",
-      "              V = y*205.7 +   Bottoms =   Trapout\n",
-      "      ----------------------------------------------------------------------------------------\n",
-      "C5 0.056       11.5        4.1     15.6        4.5     70.29\n",
-      "C6 0.35        72.0        49.3        121.3       2.25        272.91\n",
-      "C7 0.285       58.6        71.9        130.5       1.2     156.63\n",
-      "C8 0.122       25.1        52.5        77.6        0.66        51.21\n",
-      "C9 0.074       15.2        54.7        69.9        0.38        26.57\n",
-      "C10    0.068       14.0        82.5        96.5        0.22        21.23\n",
-      "C11    0.038       7.8     76.6        84.4        0.13        10.97\n",
-      "C12    0.007       1.4     22.4        23.8        0.07        1.67\n",
-      "----------------------------------------------------------------------------------------\n",
-      "1.000      205.7       414.0       619.7               611.5\n",
-      "Reboiler requirements are\n",
-      "      Vaporization lb/hr 22700\n",
-      "      Total liquor to reboiler  lb/hr 78177\n",
-      "      Heat load Btu/hr 4280000\n",
-      "      Temperature range 300-330 def F\n",
-      "      Operating pressure  psi 40\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Dew point of Overhead\n",
-    "import numpy\n",
-    "vc=numpy.array([6.4, 219.7, 2.3])\n",
-    "#vc(1) = 6.4; # Mol/hr\n",
-    "#vc(2) = 219.7; #Mol/hr\n",
-    "#vc(3) = 2.3; #Mol/hr\n",
-    "K=numpy.array([2.8, 1.01, 0.34])\n",
-    "#K(1) = 2.8; #at 148DegF and 40 psia\n",
-    "#K(2) = 1.01; #at 148DegF and 40 psia\n",
-    "#K(3) = 0.34; #at 148DegF and 40 psia\n",
-    "v=numpy.array([0, 0, 0])\n",
-    "i=0;\n",
-    "while (i<3):\n",
-    "    v[0]=vc[0]*K[0];\n",
-    "    v[1]=vc[1]*K[1];\n",
-    "    v[2]=vc[1]*K[2];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "print\"\\n\\t\\tDEW POINT OF OVERHEAD\"\n",
-    "print\"\\n\\t\\tMol/hr\\t\\tK(148DegF,40 psia)\\tV/K\\n\"\n",
-    "print\"\\t\\t--------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print vc,K,v\n",
-    "\n",
-    "bc=numpy.array([4.1, 49.3, 71.9, 52.5, 54.7, 82.5, 76.6, 22.4])\n",
-    "#bc(1)=4.1; #Mol/hr\n",
-    "#bc(2)=49.3; #Mol/hr\n",
-    "#c(3)=71.9; #Mol/hr\n",
-    "#bc(4)=52.5; #Mol/hr\n",
-    "#bc(5)=54.7; #Mol/hr\n",
-    "#bc(6)=82.5; #Mol/hr\n",
-    "#bc(7)=76.6; #Mol/hr\n",
-    "#bc(8)=22.4; #Mol/hr\n",
-    "tbc=numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "tbc[0]=tbc[0]+bc[0];\n",
-    "i=1\n",
-    "while (i<8):\n",
-    "    tbc[i]=tbc[i-1]+bc[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "bK=numpy.array([5.8, 3.0, 1.68, 0.98, 0.57, 0.35, 0.21, 0.13])\n",
-    "#bK(1)=5.8; #at 330DegF, 40 psia\n",
-    "#bK(2)=3.0; #at 330DegF, 40 psia\n",
-    "#bK(3)=1.68; #at 330DegF, 40 psia\n",
-    "#bK(4)=0.98; #at 330DegF, 40 psia\n",
-    "#bK(5)=0.57; #at 330DegF, 40 psia\n",
-    "#bK(6)=0.35; #at 330DegF, 40 psia\n",
-    "#bK(7)=0.21; #at 330DegF, 40 psia\n",
-    "#bK(8)=0.13; #at 330DegF, 40 psia\n",
-    "\n",
-    "KL=numpy.array([23.8, 148.0, 120.0, 51.4, 31.2, 28.9, 16.1, 2.9])\n",
-    "\n",
-    "#KL(1)=23.8;\n",
-    "#KL(2)=148.0;\n",
-    "#KL(3)=120.8;\n",
-    "#KL(4)=51.4;\n",
-    "#KL(5)=31.2;\n",
-    "#KL(6)=28.9;\n",
-    "#KL(7)=16.1;\n",
-    "#KL(8)=2.9;\n",
-    "\n",
-    "tk=([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "i=1;\n",
-    "op=40;\n",
-    "tk[0]=KL[0]\n",
-    "while (i<8):\n",
-    "    tk[i]=tk[i-1]+KL[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "l=numpy.array([1700, 13900, 13030, 6260, 4240, 4330, 2640, 520])    \n",
-    "#l(1)=1700; #Lb/hr\n",
-    "#l(2)=13900; #Lb/hr\n",
-    "#l(3)=13030; #Lb/hr\n",
-    "#l(4)=6260; #Lb/hr\n",
-    "#l(5)=4240; #Lb/hr\n",
-    "#l(6)=4330; #Lb/hr\n",
-    "#l(7)=2640; #Lb/hr\n",
-    "#l(8)=520; #Lb/hr\n",
-    "\n",
-    "tl=numpy.array([0, 0, 0, 0, 0, 0, 0, 0,])\n",
-    "\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "    tl[i]=tl[i]+l[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\n\\t\\tBUBBLE POINTS OF BOTTOMS\\n\"\n",
-    "print\"\\t\\tMol/hr\\t\\tK(330DegF,40psia)\\t\\tKL\\t\\tLb/hr\\n\"\n",
-    "print\"\\t\\t--------------------------------------------------------------\\n\"\n",
-    "tlr=78177;\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "\n",
-    "    print bc[i],bK[i],KL[i],l[i]\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\t____\\t\\t\\t\\t\\t____\\t\\t____\\n\"\n",
-    "\n",
-    "print\"\\t\\t\",tbc \n",
-    "print\"\\t\\t\\t\\t\\t\",tk \n",
-    "print\"\\t\\t\",tl\n",
-    "av = numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "av=tl/tk\n",
-    "hl=4280000;\n",
-    "print\"\\tAverage mol. wt. \\n\",av\n",
-    "\n",
-    "lh=numpy.array([48894, 16298, 32596])\n",
-    "bl=numpy.array([286, 129, 129])\n",
-    "#lh(1)=48894;#Lb/hr\n",
-    "#lh(2)=16298;#Lb/hr\n",
-    "#lh(3)=32596;#Lb/hr\n",
-    "#bl(1)=286;#Btu/hr\n",
-    "#bl(2)=129;#Btu/hr\n",
-    "#bl(3)=129;#Btu/hr\n",
-    "\n",
-    "bh=numpy.array([0, 0, 0])\n",
-    "vap=22700;\n",
-    "i=0;\n",
-    "\n",
-    "while (i<3):\n",
-    "    bh[0]=lh[0]*bl[0];\n",
-    "    i=i+1;\n",
-    "\n",
-    "#Heat Balances\n",
-    "print\"\\n\\n\\t\\t\\t\\t\\t\\tHEAT BALANCES:\"\n",
-    "print\"\\n\\t\\t\\t\\tMol/hr\\t\\tMol.wt.\\t\\tLb/hr\\t\\tTemp,DegF\\t\\tBtu/lb\\t\\tBtu/hr\\n\\t\"\n",
-    "print\"\\t\\t\\t----------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\tHeat Balance onCondeser\\n\\t  Heat in:\\n\\t   Top plate vapor......\"\n",
-    "\n",
-    "#Heat Balances on reboiler\n",
-    "#Assume 30Deg difference between reboiler and bottom plate giving bottom-plate temperature of 300DegF\n",
-    "#Mol/hr from Eq. 15.47\n",
-    "\n",
-    "pc=numpy.array([0.056, 0.35, 0.285, 0.122, 0.074, 0.068, 0.038, 0.007])\n",
-    "#pc(1)=0.056;\n",
-    "#pc(2)=0.350;\n",
-    "##pc(3)=0.285;\n",
-    "#pc(4)=0.122;\n",
-    "#pc(5)=0.074;\n",
-    "#pc(6)=0.068;\n",
-    "#pc(7)=0.038;\n",
-    "#pc(8)=0.007;\n",
-    "\n",
-    "pk=numpy.array([4.5, 2.25, 1.2, 0.66, 0.38, 0.22, 0.13, 0.07])\n",
-    "#pK(1)=4.5;\n",
-    "#pK(2)=2.25;\n",
-    "#pK(3)=1.20;\n",
-    "#pK(4)=0.66;\n",
-    "#pK(5)=0.38;\n",
-    "#pK(6)=0.22;\n",
-    "#pK(7)=0.13;\n",
-    "#pK(8)=0.07;\n",
-    "\n",
-    "print\"\\n\\n\\t\\tCALCULATION OF BOTTOM PLATE TEMPERATURE\\n\"\n",
-    "print\"\\t\\ty*\\t\\t\\tReboiler vapor\\t\\t\\t\\tK(300DegF,40psia)\\tMol*K\\n\\t\\t\\t\\tV = y*205.7 +\\tBottoms\\t=\\tTrapout\\n\"\n",
-    "print\"\\t\\t----------------------------------------------------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print \"CALCULATION OF BOTTOM PLATE TEMPERATURE\"\n",
-    "print\"      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\"\n",
-    "print\"              V = y*205.7 +   Bottoms =   Trapout\"\n",
-    "print\"      ----------------------------------------------------------------------------------------\"\n",
-    "print   \"C5 0.056       11.5        4.1     15.6        4.5     70.29\"\n",
-    "print   \"C6 0.35        72.0        49.3        121.3       2.25        272.91\"\n",
-    "print   \"C7 0.285       58.6        71.9        130.5       1.2     156.63\"\n",
-    "print   \"C8 0.122       25.1        52.5        77.6        0.66        51.21\"\n",
-    "print   \"C9 0.074       15.2        54.7        69.9        0.38        26.57\"\n",
-    "print   \"C10    0.068       14.0        82.5        96.5        0.22        21.23\"\n",
-    "print   \"C11    0.038       7.8     76.6        84.4        0.13        10.97\"\n",
-    "print   \"C12    0.007       1.4     22.4        23.8        0.07        1.67\"\n",
-    "print       \"----------------------------------------------------------------------------------------\"\n",
-    "print       \"1.000      205.7       414.0       619.7               611.5\"\n",
-    "\n",
-    "\n",
-    "print\"Reboiler requirements are\"\n",
-    "print\"      Vaporization lb/hr\",vap\n",
-    "print\"      Total liquor to reboiler  lb/hr\",tlr    \n",
-    "print\"      Heat load Btu/hr\",hl\n",
-    "print\"      Temperature range 300-330 def F\"\n",
-    "print\"      Operating pressure  psi\",op "
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_3.ipynb
deleted file mode 100755
index d185cf80..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_15__Vaporizers_Evapourators_and_Reboilers_3.ipynb
+++ /dev/null
@@ -1,1315 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 15 : Vaporizers Evapourators and Reboilers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.1 pgno:463"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat required for steam is :  Btu/hr \t9453000.0\n",
-      "\t total heat required for kerosene is :  Btu/hr \t9450000.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t91.1262293169\n",
-      "\t A :  ft**2 \t1037.02304713\n",
-      "\t By the law of mixtures \t\n",
-      "\t v2 : %.0f ft**3/lb \t11.0034\n",
-      "\t vav :  ft**3/lb \t3.16417120715\n",
-      "\t By the approximate method \t\n",
-      "\t vav :  ft**3/lb \t5.5102\n",
-      "\t actual density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.00505661639416\n",
-      "\t approximate density :  lb/ft**3 \t0.316038524635\n",
-      "\t s :  \t0.0029\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=250;\n",
-    "T1=400;\n",
-    "T2=300;\n",
-    "w=10000; # lb/hr\n",
-    "W=150000; # lb/hr\n",
-    "l=945.3; # Btu/(lb) , table 7\n",
-    "from math import log10\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "C=0.63; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-ts; #F\n",
-    "delt2=T1-ts; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "UD=100;\n",
-    "A=(Q/(UD*LMTD));\n",
-    "print\"\\t A :  ft**2 \\t\",A\n",
-    "WC=94500; # Btu/F\n",
-    "vl=0.017; # ft**3/lb, from table 7\n",
-    "vv=13.75; # ft**3/lb, from table 7\n",
-    "print\"\\t By the law of mixtures \\t\"\n",
-    "# Assume 80 per cent of the outlet fluid is vapor\n",
-    "v2=(0.8*vv)+(.2*vl);\n",
-    "print\"\\t v2 : ft**3/lb \\t\",v2\n",
-    "vav=(WC*(v2-vl)/(UD*A))-((WC*(T2-ts)/(l*w))*(vv-vl))+vl;\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav\n",
-    "print\"\\t By the approximate method \\t\"\n",
-    "vav1=(vl+v2)/(2);\n",
-    "print\"\\t vav :  ft**3/lb \\t\",vav1\n",
-    "row=62.5;\n",
-    "rowac=(1/vav);\n",
-    "s=(rowac/row);\n",
-    "print\"\\t actual density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",s\n",
-    "rowap=(1/vav1);\n",
-    "s=(rowap/row);\n",
-    "print\"\\t approximate density :  lb/ft**3 \\t\",rowac\n",
-    "print\"\\t s :  \\t\",round(s,4)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.2 pgno:464"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for preheat of butane is :  Btu/hr \t2124200\n",
-      "\t total heat required for vapourisation of butane is :  Btu/hr \t2172500\n",
-      "\t total heat required for  butane is :  Btu/hr \t4296700\n",
-      "\t for steam \t\n",
-      "\t total heat required for steam is :  Btu/hr \t4297328.0\n",
-      "\t Wp1 is :  lb/hr \t13401.8927445\n",
-      "\t Wv1 is :  lb/hr \t21092\n",
-      "\t W is :  lb/hr \t34493.8927445\n",
-      "\t weighted delt is : % F \t124.582285677\n",
-      "\t caloric temperature of hot fluid is :  F \t338\n",
-      "\t caloric temperature of cold fluid is :  F \t171\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.15675\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t31132.3763955\n",
-      "\t reynolds number is :  \t62178.9886688\n",
-      "\t hio is :  Btu/(hr)*(ft**2)*(F) \t1500\n",
-      "\t cold fluid:shell side,butane \t\n",
-      "\t preheating \t\n",
-      "\t flow area is :  ft**2 \t0.105902777778\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t233232.786885\n",
-      "\t reynolds number is :  \t69214.7658922\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t231.272727273\n",
-      "\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \t200.378071834\n",
-      "\t clean surface required for preheating :  ft**2 \t66.883030772\n",
-      "\t for vapourisation \t\n",
-      "\t reynolds number is :  \t79511.1773472\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t236.96969697\n",
-      "\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \t204.640614096\n",
-      "\t clean surface required for vapourisation :  ft**2 \t103.069633088\n",
-      "\t total clean surface :  ft**2 \t169.952663859\n",
-      "\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \t202.96313674\n",
-      "\t total surface area is :  ft**2 \t318.3488\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.352513798\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00430213212754\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.16\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t preheating \t\n",
-      "\t length of preheat zone :  ft \t6.29662676683\n",
-      "\t number of crosses are :  \t15.1119042404\n",
-      "\t delPsp is :  psi \t0.703032923143\n",
-      "\t vapourisation \t\n",
-      "\t number of crosses are :  \t23.28\n",
-      "\t delPsv is :  psi \t1.89396418309\n",
-      "\t delPS is :  psi \t2.6\n",
-      "\t allowable delPa is 5 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=108; # inlet cold fluid,F\n",
-    "t2=235; # outlet cold fluid,F\n",
-    "Ts=338;\n",
-    "Wp=24700; # lb/hr\n",
-    "Wv=19750; # lb/hr\n",
-    "w=4880; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=162; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=248; # enthalpy at t2, Btu/lb, fig 9\n",
-    "qp=(Wp*(Ht2-Ht1)); # for preheat\n",
-    "print\"\\t total heat required for preheat of butane is :  Btu/hr \\t\",qp\n",
-    "Ht3=358; # enthalpy of vapour at t2, Btu/lb, fig 9\n",
-    "qv=Wv*(Ht3-Ht2);\n",
-    "print\"\\t total heat required for vapourisation of butane is :  Btu/hr \\t\",qv\n",
-    "Q=qp+qv;\n",
-    "print\"\\t total heat required for  butane is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for steam \\t\"\n",
-    "l=880.6; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \\t\",Q\n",
-    "deltp=158.5; # F, from eq 5.14\n",
-    "deltv=103; # F eq 5.14\n",
-    "Wp1=(qp/deltp);\n",
-    "print\"\\t Wp1 is :  lb/hr \\t\",Wp1\n",
-    "Wv1=(qv/deltv);\n",
-    "print\"\\t Wv1 is :  lb/hr \\t\",Wv1\n",
-    "W=(Wp1+Wv1);\n",
-    "print\"\\t W is :  lb/hr \\t\",W\n",
-    "delt=(Q/W);\n",
-    "print\"\\t weighted delt is : % F \\t\",delt\n",
-    "Tc=((Ts)+(Ts))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=76;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.594; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.0363; # at 338F, fig 15,lb/(ft)*(hr)\n",
-    "D=0.0725; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hio=1500; # condensing steam,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hio is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid:shell side,butane \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "ID=15.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(Wp/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.278; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.0825; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=159; # from fig.28\n",
-    "Z=0.12; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hop=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hop\n",
-    "Up=((hio)*(hop)/(hio+hop)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for preheating :  Btu/(hr)*(ft**2)*(F) \\t\",Up\n",
-    "Ap=(qp/(Up*deltp));\n",
-    "print\"\\t clean surface required for preheating :  ft**2 \\t\",Ap\n",
-    "print\"\\t for vapourisation \\t\"\n",
-    "mu2=0.242; # at 172F,lb/(ft)*(hr), from fig.14\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=170; # from fig.28\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "hov=((jH)*(1/De)*(Z)); #using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hov\n",
-    "Uv=((hio)*(hov)/(hio+hov)); # clean overall coefficient,eq 6.38,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient for vapourisation :  Btu/(hr)*(ft**2)*(F) \\t\",Uv\n",
-    "Av=(qv/(Uv*deltv));\n",
-    "print\"\\t clean surface required for vapourisation :  ft**2 \\t\",Av\n",
-    "Ac=Ap+Av;\n",
-    "print\"\\t total clean surface :  ft**2 \\t\",Ac\n",
-    "UC=((Up*Ap)+(Uv*Av))/(Ac);\n",
-    "print\"\\t weighted clean overall coefficient :  Btu/(hr)*(ft**2)*(F) \\t\",UC\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# A total of 170 ft2 are required of which 103 are to be used for vaporization. For the total surface required 318 ft2 will be provided. It can be assumed, then, that the surface provided for vaporization is 193ft**2\n",
-    "# then flux is Q/A=10700, which is with in satisfactory levels.\n",
-    "Rd=((UC-UD)/((UD)*(UC))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000165; # friction factor for reynolds number 62000, using fig.26\n",
-    "s=0.00413;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt)))/(2); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "print\"\\t preheating \\t\"\n",
-    "f=0.00145; # friction factor for reynolds number 69200, using fig.29\n",
-    "Lp=(L*Ap/Ac); #ft\n",
-    "print\"\\t length of preheat zone :  ft \\t\",Lp\n",
-    "N=(12*Lp/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "s=0.5; # for reynolds number 69200,using fig.6\n",
-    "Ds=1.27; # fig 28\n",
-    "phys=1;\n",
-    "delPsp=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPsp is :  psi \\t\",delPsp\n",
-    "print\"\\t vapourisation \\t\"\n",
-    "f=0.00142;\n",
-    "Lv=9.7; # Lv=L-Lp\n",
-    "Nv=(12*Lv/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",Nv\n",
-    "s=0.28; \n",
-    "delPsv=((f*(Gs**2)*(Ds)*(Nv))/(5.22*(10**10)*(De)*(s)*(1))); # using eq 12.47,psi\n",
-    "print\"\\t delPsv is :  psi \\t\",delPsv\n",
-    "delPS=delPsp+delPsv;\n",
-    "print\"\\t delPS is :  psi \\t\",round(delPS,2)\n",
-    "print\"\\t allowable delPa is 5 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.3 pgno:475"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gasoline is :  Btu/hr \t2669500\n",
-      "\t total heat required for gasoil is :  Btu/hr \t2671900.0\n",
-      "\t S is :  \t0.428571428571\n",
-      "\t Tc is :  F \t517.0\n",
-      "\t hot fluid:inner tube side,gasoil \t\n",
-      "\t flow area is :  ft**2 \t0.0429722222222\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t807498.383969\n",
-      "\t reynolds number is :  \t86215.9813038\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t374.063400576\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t311.968876081\n",
-      "\t cold fluid:shell side,gasoline \t\n",
-      "\t tw is :  F \t459.64414193\n",
-      "\t deltw :  F \t59.6441419296\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t152.933697255\n",
-      "\t total surface area is :  ft**2 \t213.6288\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t105.993294626\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00289577777619\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t2.73790740915\n",
-      "\t delPr is :  psi \t3.04225352113\n",
-      "\t delPT is :  psi \t5.8\n",
-      "\t allowable delPa is 10psi \t\n",
-      "\t delPs is negligible \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "ts=400;\n",
-    "T1=575;\n",
-    "T2=475;\n",
-    "W=28100; # lb/hr\n",
-    "w=34700; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "HT1=290; # enthalpy at T1, Btu/lb, fig 11\n",
-    "HT2=385; # enthalpy at T2, Btu/lb, fig 11\n",
-    "Q=(W*(HT2-HT1)); # for preheat\n",
-    "print\"\\t total heat required for gasoline is :  Btu/hr \\t\",Q\n",
-    "c=0.77; # Btu/(lb), table 7\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt=118; # F eq 5.14\n",
-    "S=75./175.;#((T2-ts)/(T1-ts));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "Kc=0.37; # fig 17\n",
-    "Fc=0.42;\n",
-    "Tc=(T2+(0.42*(T1-T2)));\n",
-    "print\"\\t Tc is :  F \\t\",Tc\n",
-    "print\"\\t hot fluid:inner tube side,gasoil \\t\"\n",
-    "Nt=68;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.65; # at 517F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0694; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=220; # from fig.24\n",
-    "Z=0.118; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #hi/phyt, Hi=()using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "# (mu1/muw)**(0.14) is negligible\n",
-    "print\"\\t cold fluid:shell side,gasoline \\t\"\n",
-    "ho=300; # assumption\n",
-    "tw=(ts)+(((Hio)/(Hio+ho))*(Tc-ts)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-ts);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, ho>300\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=12500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00015; # friction factor for reynolds number 85700, using fig.26\n",
-    "s=0.71;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.09; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is 10psi \\t\"\n",
-    "print\"\\t delPs is negligible \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.4 pgno:482"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.4\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t qv is :  Btu/hr \t3654000\n",
-      "\t qs is :  Btu/hr \t539000\n",
-      "\t total heat required for naphtha is :  Btu/hr \t4193000\n",
-      "\t total heat required for gasoil is :  Btu/hr \t4207500.0\n",
-      "\t delt1 is :  F \t85.0\n",
-      "\t delt2 is :  F \t190.0\n",
-      "\t LMTD is : F \t130.683201952\n",
-      "\t R is :  \t6.25\n",
-      "\t S is :  \t0.0952380952381\n",
-      "\t FT is 0.97 \t\n",
-      "\t delt is :  F \t126.762705893\n",
-      "\t ratio of two local temperature difference is :  \t0.447368421053\n",
-      "\t caloric temperature of hot fluid is :  F \t451.25\n",
-      "\t caloric temperature of cold fluid is :  F \t323.2\n",
-      "\t hot fluid:inner tube side,steam \t\n",
-      "\t flow area is :  ft**2 \t0.0549791666667\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t927624.100038\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t343.251798561\n",
-      "\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t286.272\n",
-      "\t cold fluid:shell side,naphtha \t\n",
-      "\t tw is :  F \t398.584002369\n",
-      "\t deltw :  F \t75.384002369\n",
-      "\t qv/hv :  \t12180\n",
-      "\t qs/hs :  \t8983\n",
-      "\t A :  \t21163\n",
-      "\t ho :  \t198.813967774\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t117.329454908\n",
-      "\t total surface area is :  ft**2 \t364.4256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t91.0801518561\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.00245633150105\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t5.24018227225\n",
-      "\t delPr is :  psi \t4.82191780822\n",
-      "\t delPT is :  psi \t10.1\n",
-      "\t allowable delPa is negligible \t\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t flow area :  in**2 \t131.70828125\n",
-      "\t wetted perimeter :  in \t236.7325\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20992.3664122\n",
-      "\t reynolds number is :  \t59146.6742685\n",
-      "\t delPs is :  psi \t0.25\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.4\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=315.; # inlet cold fluid,F\n",
-    "t2=335.; # outlet cold fluid,F\n",
-    "T1=525.;\n",
-    "T2=400.;\n",
-    "Wv=29000; # lb/hr\n",
-    "Ws=38500; # lb/hr\n",
-    "w=51000; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=238; # enthalpy at t1, Btu/lb, fig 9\n",
-    "Ht2=252; # enthalpy at t2, Btu/lb, fig 9\n",
-    "Ht3=378; # enthalpy of vapour at t2 \n",
-    "qv=(Wv*(Ht3-Ht2)); # for preheat\n",
-    "print\"\\t qv is :  Btu/hr \\t\",qv\n",
-    "qs=Ws*(Ht2-Ht1);\n",
-    "print\"\\t qs is :  Btu/hr \\t\",qs\n",
-    "Q=qs+qv;\n",
-    "print\"\\t total heat required for naphtha is :  Btu/hr \\t\",Q\n",
-    "c=0.66; # Btu/(lb)(F)\n",
-    "Q=((w)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gasoil is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.97 \\t\" # from fig 18\n",
-    "delt=(0.97*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "X=((delt1)/(delt2)); # fig 17\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.41; # from fig.17\n",
-    "Kc=0.42;\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side,steam \\t\"\n",
-    "Nt=116;\n",
-    "n=8; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.546; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=1.09; # at 451F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0695; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=168; # from fig.24\n",
-    "Z=0.142; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((Hi)*(0.834/1)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "print\"\\t cold fluid:shell side,naphtha \\t\"\n",
-    "ho1=200; # assumption\n",
-    "tw=(tc)+(((Hio)/(Hio+ho1))*(Tc-tc)); # from eq.5.31, calculation mistake\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "deltw=(tw-tc);\n",
-    "print\"\\t deltw :  F \\t\",deltw\n",
-    "# from fig 15.11, hv>300, hs=60\n",
-    "Av=(qv/300);\n",
-    "As=qs/60;\n",
-    "print\"\\t qv/hv :  \\t\",Av\n",
-    "print\"\\t qs/hs :  \\t\",As\n",
-    "A1=As+Av;\n",
-    "print\"\\t A :  \\t\",A1\n",
-    "ho=(Q/A1);\n",
-    "print\"\\t ho :  \\t\",ho\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# check for max. flux=Q/A=11500.(satisfactory)\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000168; # friction factor for reynolds number 59200, using fig.26\n",
-    "s=0.73;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",delPt\n",
-    "X1=0.11; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPa is negligible \\t\"\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "Af=(3.14*(21.25**2-(116))/8);\n",
-    "print\"\\t flow area :  in**2 \\t\",Af\n",
-    "As=0.917; # ft**2\n",
-    "p=(3.14*21.25/2)+(3.14*1*116/2)+(21.25)\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=0.186; # ft\n",
-    "Gs=(Ws/(2*As)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu2=0.435; # at 315F, fig 14,lb/(ft)*(hr)\n",
-    "Res=((De)*(Gs)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "f=0.00028; # using fig.26\n",
-    "row=0.337; # fig 13.14\n",
-    "# soutlet max=0.071,\n",
-    "s=0.35; # using fig.6\n",
-    "phys=1;\n",
-    "delPs=0.25 #((f*(Gs**2)*(L))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.5 pgno:488"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.5\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for butane is :  Btu/hr \t3957600\n",
-      "\t total heat required for steam is : Btu/hr \t3966760\n",
-      "\t trail 1 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t105.068772287\n",
-      "\t total surface area is : ft**2 \t342.3472\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t92.6956025929\n",
-      "\t vapour density : lb/ft**3 \t3.18723589714\n",
-      "\t weight flow of recirculated liquid : lb/hr \t163200\n",
-      "\t volume of liquid : ft**3 \t6071.04\n",
-      "\t volume of vapour : ft**3 \t17952.0\n",
-      "\t total volume out of reboiler : ft**3 \t24023.04\n",
-      "\t vo is : ft**3/lb \t0.11776\n",
-      "\t pressure leg : psi \t1.58756230188\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.228597222222\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t892399.295218\n",
-      "\t reynolds number is : \t190648.940342\n",
-      "\t delPt is : psi \t2.1\n",
-      "negilgable\n",
-      "\t total resisitance : psi \t3.69151627479\n",
-      "\t driving force : psi \t2.98611111111\n",
-      "\t trial 2 \t\n",
-      "\t A1 is : ft**2 \t330\n",
-      "\t number of tubes are : \t140.091696383\n",
-      "\t total surface area is : ft**2 \t355.6956\n",
-      "\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \t89.21695967\n",
-      "\t pressure leg : psi \t1.19067172641\n",
-      "\t frictional resistance \t\n",
-      "\t flow area is : ft**2 \t0.316680555556\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t644182.272707\n",
-      "\t reynolds number is : \t137620.75826\n",
-      "\t delPt is : psi \t0.874030618788\n",
-      "\t total resisitance : psi \t2.0647023452\n",
-      "\t driving force : psi \t2.23958333333\n",
-      "\t hot fluid : shell side,steam \t\n",
-      "\t cold fluid:inner tube side, butane \t\n",
-      "\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \t734.042553191\n",
-      "\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t248.0\n",
-      "\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \t212.814645309\n",
-      "\t actual Rd is : (hr)*(ft**2)*(F)/Btu \t0.006537030325\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.5\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "W=40800; # lb/hr\n",
-    "w=4570; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "Ht1=241; # enthalpy of liquid at 228F, Btu/lb, fig 9\n",
-    "Ht2=338; # enthalpy of vapourat 228F, Btu/lb, fig 9\n",
-    "Q=(W*(Ht2-Ht1));\n",
-    "print\"\\t total heat required for butane is :  Btu/hr \\t\",Q\n",
-    "l=868; # Btu/(lb), table 7\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is : Btu/hr \\t\",Q\n",
-    "delt=125; # delt=LMTD, isothermal boiling, eq 5.14\n",
-    "# Tc and tc: Both streams are isuthermal\n",
-    "print\"\\t trail 1 \\t\"\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=16;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=109; # assuming one tube passes, 13.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "# Assume 4: 1 recirculation ratio\n",
-    "rowv=(58/(359*(688/492)*(14.7/290))); # eq 15.18\n",
-    "print\"\\t vapour density : lb/ft**3 \\t\",rowv\n",
-    "Vv=0.44; \n",
-    "Vl=0.0372; # fig 6\n",
-    "W1=4*W;\n",
-    "print\"\\t weight flow of recirculated liquid : lb/hr \\t\",W1\n",
-    "VL=W1*Vl;\n",
-    "VV=W*Vv;\n",
-    "print\"\\t volume of liquid : ft**3 \\t\",VL\n",
-    "print\"\\t volume of vapour : ft**3 \\t\",VV\n",
-    "V=VL+VV;\n",
-    "print\"\\t total volume out of reboiler : ft**3 \\t\",V\n",
-    "vo=(V/(W1+W));\n",
-    "print\"\\t vo is : ft**3/lb \\t\",vo\n",
-    "Pl=((2.3*16)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=109;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000127; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",round(delPt,2)\n",
-    "P=Pl+delPt;\n",
-    "print\"negilgable\"\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(16*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# The resistances are greater than the hydrostatic head can provide; hence the recirculation ratio will be less than 4: 1\n",
-    "print\"\\t trial 2 \\t\" # Assume 12'0\" tubes and 4:1 recirculation ratio\n",
-    "A1=((Q)/((12000))); # Q/A1 =12000, first trial should always be taken for the maximum allowable flux\n",
-    "print\"\\t A1 is : ft**2 \\t\",A1\n",
-    "a1=0.1963; # ft**2/lin ft\n",
-    "L=12;\n",
-    "N1=(A1/(L*a1)); # table 10\n",
-    "print\"\\t number of tubes are : \\t\",N1\n",
-    "N2=151; # assuming one tube passes, 15.25-in ID, from table 9\n",
-    "A2=(N2*L*a1); # ft**2\n",
-    "print\"\\t total surface area is : ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(delt)));\n",
-    "print\"\\t correct design overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Pl=((2.3*12)/(144*(vo-Vl)))*(log10(vo/Vl));\n",
-    "print\"\\t pressure leg : psi \\t\",Pl\n",
-    "print\"\\t frictional resistance \\t\"\n",
-    "Nt=151;\n",
-    "n=1; # number of passes\n",
-    "at1=0.302; # flow area,table 10, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=((W1+W)/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu1=0.242; # at 228F, fig 14,lb/(ft)*(hr)\n",
-    "D=0.0517; # ft\n",
-    "Ret=((D)*(Gt)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "f=0.000135; # using fig.26\n",
-    "s=0.285;\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(12)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is : psi \\t\",delPt\n",
-    "P=Pl+delPt;\n",
-    "print\"\\t total resisitance : psi \\t\",P\n",
-    "F=(12*0.43*62.5/144);\n",
-    "print\"\\t driving force : psi \\t\",F\n",
-    "# Since the driving force is slightly greater than the resistances, a recirculation ratio better than 4:1 is assured.\n",
-    "print\"\\t hot fluid : shell side,steam \\t\"\n",
-    "ho=1500; # condensing steam\n",
-    "print\"\\t cold fluid:inner tube side, butane \\t\"\n",
-    "jH=330; # from fig.24\n",
-    "Z=0.115; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hi=((jH)*(1/D)*(Z)); #, Hi=(hi/phyt)using eq.6.15d,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "Hio=((300)*(0.62/0.75)); #Hio=(hio/phyp), using eq.6.9\n",
-    "print\"\\t Correct Hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",Hio\n",
-    "Uc=((Hio)*(ho)/(Hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "UD=89;\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is : (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.6 pgno492"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.6\t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total heat duty : Btu/hr \t5799016.0\n",
-      "\t total heat duty : lb/hr \t37902.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.6\\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#20000=WD+WB;\n",
-    "#0.99*WD+(0.05*WB)=(20000*.5);\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "HBl=108; # fig 3 and 12\n",
-    "HDl=85.8; #fig 3 and 12\n",
-    "HDv=253.8; # fig 3 and 12\n",
-    "HFl=92; # fig 3 and 12\n",
-    "l=153; # fig 3 and 12\n",
-    "QR=((2.54+1)*WD*(HDv))-(2.54*WD*HDl)+(WB*HBl)-(20000*HFl);\n",
-    "print\"\\t total heat duty : Btu/hr \\t\",round(QR)\n",
-    "Q=QR/153;\n",
-    "print\"\\t total heat duty : lb/hr \\t\",round(Q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.7 pgno:502"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\ttotal Lb/hr is \t20000\n",
-      "\ttotal Mol/hr is \t235.5\n",
-      "\tx1 of C6H6 is \t0.543524416136\n",
-      "\tx1 of C7H8 is \t0.456475583864\n",
-      "\tTotal x1 is \t1.0\n",
-      "\tx1Pp1 of C6H6 is \t750.063694268\n",
-      "\tx1Pp1 of C7H8 is \t262.473460722\n",
-      "\tTotal x1Pp1 is \t1012.53715499\n",
-      "\ty1 of C6H6 is \t0.740776464914\n",
-      "\ty1 of C7H8 is \t0.259223535086\n",
-      "\tTotal y1 is \t1.0\n",
-      "\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\t0.558\n",
-      "\tWR` = %.2f (mol reflux)/(mol distillate)\t1.27\n",
-      "\tAssumed 200 percent of the theoretical minimum reflux as economic\t\tWR = (mol)/(mil distillate)\t2.54\n",
-      "\tThe intercept for the upper operating line = \t0.280225988701\n",
-      "\tConnecting the corresponding line in Fig. 15.23, plates required: \t13\n",
-      "\tFeed plate is th(from top)\t7\n",
-      "\tTotal reflux is \t311.15\n",
-      "\t\t\t\t\tHeat balances\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\tHeat balance \t\taround condenser:\t\n",
-      "\t  Heat in:\t\t  Top plate vapor.......433\t87.3\t\t195\t%.1f\t\t33900 253.8 8603820.0\n",
-      "\t  Heat out:\t\t  Distillate............\n",
-      "122.5\t78.3\t\t195\t\t\t9570 85.8 821106.0\n",
-      "\t  Reflux................\n",
-      "310.5\t78.3\t\t195\t\t\t24330 85.8 2087514.0\n",
-      "\t  Condenser duty, by\t\t  difference........... .....   ....    ......  ..\n",
-      ".     .....   5688000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t8600000\t\t\n",
-      "\tReboiler vapor is  lb/hr\t37908\n",
-      "\tTrapout is  lb/hr\t48338\n",
-      "\t\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,DegF\tBtu/lb\tBtu/hr\t\t________________________________________________________________________\t\n",
-      "\tHeat in:\t\t  Trapout...............522\t92.8\t\t246\t108.0\t5230000\t48338\n",
-      "\t  Reboiler duty, \t\t  by difference.......  ....    ....    .....   ...     .....   5800000\t\n",
-      "\t\t\t\t\t\t\t\t\t_______\t\t\t\t\t\t\t\t\t\t11030000\t\t\n",
-      "\t\tReboiler requirements are\t\n",
-      "\t\tTotal liquid to reboiler\t48330 lb/hr\t\t\tVaporization\t\t\t37900 lb/hr\t\t\tTemperature(nearly isothermal)\t246DegF\t\t\tPressure\t\t\t5 psig\t\t\tHeat load\t\t\t5800000 Btu/hr\t\n",
-      "total heat out is btu/hr 7640000\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "\n",
-    "#Basis: One hour\n",
-    "#20000=WD+WB , material balance\n",
-    "#0.99*WD+(0.05*WB)=(20000*0.5) , Benzene balance\n",
-    "# solving above two eq. we get WD and WB\n",
-    "WD=9570; # lb/hr\n",
-    "WB=10430; # lb/hr\n",
-    "\n",
-    "#Compositions and Boiling Points\n",
-    "#Feed\n",
-    "l1 = 10000; #Lb/hr , C6H4\n",
-    "l2 = 10000; #Lb/hr , C7H8\n",
-    "lb = l1+l2; #Lb/hr\n",
-    "print\"\\ttotal Lb/hr is \\t\",lb\n",
-    "mo1 = 78.1; #Mol. wt., C6H6\n",
-    "mo2 = 93.1; #Mol. wt , C7H8\n",
-    "mh1 = 128.0; #Mol/hr , C6H6\n",
-    "mh2 = 107.5; #Mol/hr , C7H8\n",
-    "mh = mh1 + mh2; # Mol/hr\n",
-    "print\"\\ttotal Mol/hr is \\t\",mh\n",
-    "x1 = mh1/mh;\n",
-    "print\"\\tx1 of C6H6 is \\t\",x1\n",
-    "x2 = mh2/mh;\n",
-    "print\"\\tx1 of C7H8 is \\t\",x2\n",
-    "x = x1+x2;\n",
-    "print\"\\tTotal x1 is \\t\",x\n",
-    "Pp1= 1380; # 214Deg F\n",
-    "Pp2=575; # 214Deg F\n",
-    "xp1 = x1*Pp1;\n",
-    "print\"\\tx1Pp1 of C6H6 is \\t\",xp1\n",
-    "xp2 = x2*Pp2;\n",
-    "print\"\\tx1Pp1 of C7H8 is \\t\",xp2\n",
-    "sxp = xp1 + xp2;\n",
-    "print\"\\tTotal x1Pp1 is \\t\",sxp\n",
-    "y1 = xp1/sxp;\n",
-    "print\"\\ty1 of C6H6 is \\t\",y1\n",
-    "y2 = xp2/sxp;\n",
-    "print\"\\ty1 of C7H8 is \\t\",y2\n",
-    "y = y1+y2;\n",
-    "print\"\\tTotal y1 is \\t\",y\n",
-    "\n",
-    "\n",
-    "w1 = 0.558; #from eq 15.42\n",
-    "print\"\\t(WR`/V =((xD - yF)/.(xD - xF))) = mol/mol\\t\",w1\n",
-    "wD=1;\n",
-    "xD = 0.992;\n",
-    "#V = WR' + WD\n",
-    "# WR'/V = 0.558\n",
-    "#Solving, WR' = (WR' * 0.558) + (0.558 * WD)\n",
-    "Wr = 1.27; # mol reflux/mol distillate\n",
-    "print\"\\tWR` = %.2f (mol reflux)/(mol distillate)\\t\",Wr\n",
-    "Wr1 = Wr * 2; # mol/ mol distillate\n",
-    "print\"\\tAssumed 200 percent of the theoretical minimum reflux as economic\\t\\tWR = (mol)/(mil distillate)\\t\",Wr1\n",
-    "In = (wD * xD)/(Wr1 + 1); #intercept for the upper operating line\n",
-    "print\"\\tThe intercept for the upper operating line = \\t\",In\n",
-    "p = 13; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tConnecting the corresponding line in Fig. 15.23, plates required: \\t\",p\n",
-    "fp = 7; # From fig. 15.23, connecting the corresponding lines\n",
-    "print\"\\tFeed plate is th(from top)\\t\",fp\n",
-    "d=122.5;\n",
-    "tf = Wr1 * d;\n",
-    "print\"\\tTotal reflux is \\t\",tf\n",
-    "print\"\\t\\t\\t\\t\\tHeat balances\"\n",
-    "\n",
-    "#Heat Balances\n",
-    "l1 = 33900;\n",
-    "l2 = 9570;\n",
-    "l3 = 24330;\n",
-    "b1 = 253.8;\n",
-    "b2 = 85.8;\n",
-    "b3 = 85.8;\n",
-    "bt1 = b1*l1;\n",
-    "bt2 = b2*l2;\n",
-    "bt3 = b3*l3;\n",
-    "bt4 = 5688000;\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\\tHeat balance \\t\\taround condenser:\\t\"\n",
-    "print\"\\t  Heat in:\\t\\t  Top plate vapor.......433\\t87.3\\t\\t195\\t%.1f\\t\\t\",l1,b1,bt1\n",
-    "print\"\\t  Heat out:\\t\\t  Distillate............\"\n",
-    "print\"122.5\\t78.3\\t\\t195\\t\\t\\t\",l2,b2,bt2\n",
-    "print\"\\t  Reflux................\"\n",
-    "print\"310.5\\t78.3\\t\\t195\\t\\t\\t\",l3,b3,bt3\n",
-    "print\"\\t  Condenser duty, by\\t\\t  difference........... .....   ....    ......  ..\"\n",
-    "print\".     .....   5688000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t8600000\\t\\t\"\n",
-    "tho=7640000;\n",
-    "\n",
-    "lam = 153; # At 246 DegF, Btu/hr\n",
-    "rv = 5800000/153; #Lb/hr\n",
-    "print\"\\tReboiler vapor is  lb/hr\\t\",rv\n",
-    "to = rv + 10430; #Lb/hr\n",
-    "print\"\\tTrapout is  lb/hr\\t\",to\n",
-    "\n",
-    "print\"\\t\\t\\t\\t\\tMol/hr\\tMol.wt.\\tLb/hr\\tTemp,DegF\\tBtu/lb\\tBtu/hr\\t\\t________________________________________________________________________\\t\"\n",
-    "print\"\\tHeat in:\\t\\t  Trapout...............522\\t92.8\\t\\t246\\t108.0\\t5230000\\t\",to\n",
-    "print\"\\t  Reboiler duty, \\t\\t  by difference.......  ....    ....    .....   ...     .....   5800000\\t\"\n",
-    "print\"\\t\\t\\t\\t\\t\\t\\t\\t\\t_______\\t\\t\\t\\t\\t\\t\\t\\t\\t\\t11030000\\t\\t\"\n",
-    "print\"\\t\\tReboiler requirements are\\t\"\n",
-    "print\"\\t\\tTotal liquid to reboiler\\t48330 lb/hr\\t\\t\\tVaporization\\t\\t\\t37900 lb/hr\\t\\t\\tTemperature(nearly isothermal)\\t246DegF\\t\\t\\tPressure\\t\\t\\t5 psig\\t\\t\\tHeat load\\t\\t\\t5800000 Btu/hr\\t\"\n",
-    "print\"total heat out is btu/hr\",tho \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 15.8 pgno:506"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 15.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\n",
-      "\t\tDEW POINT OF OVERHEAD\n",
-      "\n",
-      "\t\tMol/hr\t\tK(148DegF,40 psia)\tV/K\n",
-      "\n",
-      "\t\t--------------------------------------------\n",
-      "\n",
-      "[   6.4  219.7    2.3] [ 2.8   1.01  0.34] [ 17 221  74]\n",
-      "\n",
-      "\t\tBUBBLE POINTS OF BOTTOMS\n",
-      "\n",
-      "\t\tMol/hr\t\tK(330DegF,40psia)\t\tKL\t\tLb/hr\n",
-      "\n",
-      "\t\t--------------------------------------------------------------\n",
-      "\n",
-      "4.1 5.8 23.8 1700\n",
-      "49.3 3.0 148.0 13900\n",
-      "71.9 1.68 120.0 13030\n",
-      "52.5 0.98 51.4 6260\n",
-      "54.7 0.57 31.2 4240\n",
-      "82.5 0.35 28.9 4330\n",
-      "76.6 0.21 16.1 2640\n",
-      "22.4 0.13 2.9 520\n",
-      "\t\t____\t\t\t\t\t____\t\t____\n",
-      "\n",
-      "\t\t[  4  53 124 176 230 312 388 410]\n",
-      "\t\t\t\t\t[23.800000000000001, 171.80000000000001, 291.80000000000001, 343.19999999999999, 374.39999999999998, 403.29999999999995, 419.39999999999998, 422.29999999999995]\n",
-      "\t\t[ 1700 13900 13030  6260  4240  4330  2640   520]\n",
-      "\tAverage mol. wt. \n",
-      "[ 71.42857143  80.9080326   44.65387252  18.24009324  11.32478632\n",
-      "  10.7364245    6.29470672   1.23135212]\n",
-      "\n",
-      "\n",
-      "\t\t\t\t\t\tHEAT BALANCES:\n",
-      "\n",
-      "\t\t\t\tMol/hr\t\tMol.wt.\t\tLb/hr\t\tTemp,DegF\t\tBtu/lb\t\tBtu/hr\n",
-      "\t\n",
-      "\t\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "\tHeat Balance onCondeser\n",
-      "\t  Heat in:\n",
-      "\t   Top plate vapor......\n",
-      "\n",
-      "\n",
-      "\t\tCALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "\n",
-      "\t\ty*\t\t\tReboiler vapor\t\t\t\tK(300DegF,40psia)\tMol*K\n",
-      "\t\t\t\tV = y*205.7 +\tBottoms\t=\tTrapout\n",
-      "\n",
-      "\t\t----------------------------------------------------------------------------------------\n",
-      "\n",
-      "CALCULATION OF BOTTOM PLATE TEMPERATURE\n",
-      "      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\n",
-      "              V = y*205.7 +   Bottoms =   Trapout\n",
-      "      ----------------------------------------------------------------------------------------\n",
-      "C5 0.056       11.5        4.1     15.6        4.5     70.29\n",
-      "C6 0.35        72.0        49.3        121.3       2.25        272.91\n",
-      "C7 0.285       58.6        71.9        130.5       1.2     156.63\n",
-      "C8 0.122       25.1        52.5        77.6        0.66        51.21\n",
-      "C9 0.074       15.2        54.7        69.9        0.38        26.57\n",
-      "C10    0.068       14.0        82.5        96.5        0.22        21.23\n",
-      "C11    0.038       7.8     76.6        84.4        0.13        10.97\n",
-      "C12    0.007       1.4     22.4        23.8        0.07        1.67\n",
-      "----------------------------------------------------------------------------------------\n",
-      "1.000      205.7       414.0       619.7               611.5\n",
-      "Reboiler requirements are\n",
-      "      Vaporization lb/hr 22700\n",
-      "      Total liquor to reboiler  lb/hr 78177\n",
-      "      Heat load Btu/hr 4280000\n",
-      "      Temperature range 300-330 def F\n",
-      "      Operating pressure  psi 40\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 15.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#Dew point of Overhead\n",
-    "import numpy\n",
-    "vc=numpy.array([6.4, 219.7, 2.3])\n",
-    "#vc(1) = 6.4; # Mol/hr\n",
-    "#vc(2) = 219.7; #Mol/hr\n",
-    "#vc(3) = 2.3; #Mol/hr\n",
-    "K=numpy.array([2.8, 1.01, 0.34])\n",
-    "#K(1) = 2.8; #at 148DegF and 40 psia\n",
-    "#K(2) = 1.01; #at 148DegF and 40 psia\n",
-    "#K(3) = 0.34; #at 148DegF and 40 psia\n",
-    "v=numpy.array([0, 0, 0])\n",
-    "i=0;\n",
-    "while (i<3):\n",
-    "    v[0]=vc[0]*K[0];\n",
-    "    v[1]=vc[1]*K[1];\n",
-    "    v[2]=vc[1]*K[2];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "print\"\\n\\t\\tDEW POINT OF OVERHEAD\"\n",
-    "print\"\\n\\t\\tMol/hr\\t\\tK(148DegF,40 psia)\\tV/K\\n\"\n",
-    "print\"\\t\\t--------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print vc,K,v\n",
-    "\n",
-    "bc=numpy.array([4.1, 49.3, 71.9, 52.5, 54.7, 82.5, 76.6, 22.4])\n",
-    "#bc(1)=4.1; #Mol/hr\n",
-    "#bc(2)=49.3; #Mol/hr\n",
-    "#c(3)=71.9; #Mol/hr\n",
-    "#bc(4)=52.5; #Mol/hr\n",
-    "#bc(5)=54.7; #Mol/hr\n",
-    "#bc(6)=82.5; #Mol/hr\n",
-    "#bc(7)=76.6; #Mol/hr\n",
-    "#bc(8)=22.4; #Mol/hr\n",
-    "tbc=numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "tbc[0]=tbc[0]+bc[0];\n",
-    "i=1\n",
-    "while (i<8):\n",
-    "    tbc[i]=tbc[i-1]+bc[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "\n",
-    "bK=numpy.array([5.8, 3.0, 1.68, 0.98, 0.57, 0.35, 0.21, 0.13])\n",
-    "#bK(1)=5.8; #at 330DegF, 40 psia\n",
-    "#bK(2)=3.0; #at 330DegF, 40 psia\n",
-    "#bK(3)=1.68; #at 330DegF, 40 psia\n",
-    "#bK(4)=0.98; #at 330DegF, 40 psia\n",
-    "#bK(5)=0.57; #at 330DegF, 40 psia\n",
-    "#bK(6)=0.35; #at 330DegF, 40 psia\n",
-    "#bK(7)=0.21; #at 330DegF, 40 psia\n",
-    "#bK(8)=0.13; #at 330DegF, 40 psia\n",
-    "\n",
-    "KL=numpy.array([23.8, 148.0, 120.0, 51.4, 31.2, 28.9, 16.1, 2.9])\n",
-    "\n",
-    "#KL(1)=23.8;\n",
-    "#KL(2)=148.0;\n",
-    "#KL(3)=120.8;\n",
-    "#KL(4)=51.4;\n",
-    "#KL(5)=31.2;\n",
-    "#KL(6)=28.9;\n",
-    "#KL(7)=16.1;\n",
-    "#KL(8)=2.9;\n",
-    "\n",
-    "tk=([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "i=1;\n",
-    "op=40;\n",
-    "tk[0]=KL[0]\n",
-    "while (i<8):\n",
-    "    tk[i]=tk[i-1]+KL[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "l=numpy.array([1700, 13900, 13030, 6260, 4240, 4330, 2640, 520])    \n",
-    "#l(1)=1700; #Lb/hr\n",
-    "#l(2)=13900; #Lb/hr\n",
-    "#l(3)=13030; #Lb/hr\n",
-    "#l(4)=6260; #Lb/hr\n",
-    "#l(5)=4240; #Lb/hr\n",
-    "#l(6)=4330; #Lb/hr\n",
-    "#l(7)=2640; #Lb/hr\n",
-    "#l(8)=520; #Lb/hr\n",
-    "\n",
-    "tl=numpy.array([0, 0, 0, 0, 0, 0, 0, 0,])\n",
-    "\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "    tl[i]=tl[i]+l[i];\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\n\\t\\tBUBBLE POINTS OF BOTTOMS\\n\"\n",
-    "print\"\\t\\tMol/hr\\t\\tK(330DegF,40psia)\\t\\tKL\\t\\tLb/hr\\n\"\n",
-    "print\"\\t\\t--------------------------------------------------------------\\n\"\n",
-    "tlr=78177;\n",
-    "i=0;\n",
-    "while (i<8):\n",
-    "\n",
-    "    print bc[i],bK[i],KL[i],l[i]\n",
-    "    i=i+1;\n",
-    "\n",
-    "print\"\\t\\t____\\t\\t\\t\\t\\t____\\t\\t____\\n\"\n",
-    "\n",
-    "print\"\\t\\t\",tbc \n",
-    "print\"\\t\\t\\t\\t\\t\",tk \n",
-    "print\"\\t\\t\",tl\n",
-    "av = numpy.array([0, 0, 0, 0, 0, 0, 0, 0])\n",
-    "av=tl/tk\n",
-    "hl=4280000;\n",
-    "print\"\\tAverage mol. wt. \\n\",av\n",
-    "\n",
-    "lh=numpy.array([48894, 16298, 32596])\n",
-    "bl=numpy.array([286, 129, 129])\n",
-    "#lh(1)=48894;#Lb/hr\n",
-    "#lh(2)=16298;#Lb/hr\n",
-    "#lh(3)=32596;#Lb/hr\n",
-    "#bl(1)=286;#Btu/hr\n",
-    "#bl(2)=129;#Btu/hr\n",
-    "#bl(3)=129;#Btu/hr\n",
-    "\n",
-    "bh=numpy.array([0, 0, 0])\n",
-    "vap=22700;\n",
-    "i=0;\n",
-    "\n",
-    "while (i<3):\n",
-    "    bh[0]=lh[0]*bl[0];\n",
-    "    i=i+1;\n",
-    "\n",
-    "#Heat Balances\n",
-    "print\"\\n\\n\\t\\t\\t\\t\\t\\tHEAT BALANCES:\"\n",
-    "print\"\\n\\t\\t\\t\\tMol/hr\\t\\tMol.wt.\\t\\tLb/hr\\t\\tTemp,DegF\\t\\tBtu/lb\\t\\tBtu/hr\\n\\t\"\n",
-    "print\"\\t\\t\\t----------------------------------------------------------------------------------------\"\n",
-    "print\"\\n\\tHeat Balance onCondeser\\n\\t  Heat in:\\n\\t   Top plate vapor......\"\n",
-    "\n",
-    "#Heat Balances on reboiler\n",
-    "#Assume 30Deg difference between reboiler and bottom plate giving bottom-plate temperature of 300DegF\n",
-    "#Mol/hr from Eq. 15.47\n",
-    "\n",
-    "pc=numpy.array([0.056, 0.35, 0.285, 0.122, 0.074, 0.068, 0.038, 0.007])\n",
-    "#pc(1)=0.056;\n",
-    "#pc(2)=0.350;\n",
-    "##pc(3)=0.285;\n",
-    "#pc(4)=0.122;\n",
-    "#pc(5)=0.074;\n",
-    "#pc(6)=0.068;\n",
-    "#pc(7)=0.038;\n",
-    "#pc(8)=0.007;\n",
-    "\n",
-    "pk=numpy.array([4.5, 2.25, 1.2, 0.66, 0.38, 0.22, 0.13, 0.07])\n",
-    "#pK(1)=4.5;\n",
-    "#pK(2)=2.25;\n",
-    "#pK(3)=1.20;\n",
-    "#pK(4)=0.66;\n",
-    "#pK(5)=0.38;\n",
-    "#pK(6)=0.22;\n",
-    "#pK(7)=0.13;\n",
-    "#pK(8)=0.07;\n",
-    "\n",
-    "print\"\\n\\n\\t\\tCALCULATION OF BOTTOM PLATE TEMPERATURE\\n\"\n",
-    "print\"\\t\\ty*\\t\\t\\tReboiler vapor\\t\\t\\t\\tK(300DegF,40psia)\\tMol*K\\n\\t\\t\\t\\tV = y*205.7 +\\tBottoms\\t=\\tTrapout\\n\"\n",
-    "print\"\\t\\t----------------------------------------------------------------------------------------\\n\"\n",
-    "\n",
-    "\n",
-    "print \"CALCULATION OF BOTTOM PLATE TEMPERATURE\"\n",
-    "print\"      y*          Reboiler vapor              K(300DegF,40psia)   Mol*K\"\n",
-    "print\"              V = y*205.7 +   Bottoms =   Trapout\"\n",
-    "print\"      ----------------------------------------------------------------------------------------\"\n",
-    "print   \"C5 0.056       11.5        4.1     15.6        4.5     70.29\"\n",
-    "print   \"C6 0.35        72.0        49.3        121.3       2.25        272.91\"\n",
-    "print   \"C7 0.285       58.6        71.9        130.5       1.2     156.63\"\n",
-    "print   \"C8 0.122       25.1        52.5        77.6        0.66        51.21\"\n",
-    "print   \"C9 0.074       15.2        54.7        69.9        0.38        26.57\"\n",
-    "print   \"C10    0.068       14.0        82.5        96.5        0.22        21.23\"\n",
-    "print   \"C11    0.038       7.8     76.6        84.4        0.13        10.97\"\n",
-    "print   \"C12    0.007       1.4     22.4        23.8        0.07        1.67\"\n",
-    "print       \"----------------------------------------------------------------------------------------\"\n",
-    "print       \"1.000      205.7       414.0       619.7               611.5\"\n",
-    "\n",
-    "\n",
-    "print\"Reboiler requirements are\"\n",
-    "print\"      Vaporization lb/hr\",vap\n",
-    "print\"      Total liquor to reboiler  lb/hr\",tlr    \n",
-    "print\"      Heat load Btu/hr\",hl\n",
-    "print\"      Temperature range 300-330 def F\"\n",
-    "print\"      Operating pressure  psi\",op "
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces.ipynb
deleted file mode 100755
index 36846d25..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces.ipynb
+++ /dev/null
@@ -1,1044 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 16: Extented Surfaces"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.1 pgno: 521"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t fin surface is : %.1f ft**2/lin ft \t2.5\n",
-      "\t bare tube surface is :  ft**2/lin ft \t0.0\n",
-      "\t total outside surface :  ft**2/lin ft \t2.5\n",
-      "\t total inside surface :  ft**2/lin ft \t0.277366666667\n",
-      "\t fin efficiencies \t\n",
-      "\t hf      m      n \t \n",
-      "4\n",
-      "5.24\n",
-      "0.965717954492\n",
-      "\t weighted efficiency curve \t\n",
-      "\t hf      hfi \t \n",
-      "4\n",
-      "34.8173760783\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAZAAAAEZCAYAAAC5AHPcAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XeYXGX5xvHvnUCoEQggLZEaSpASelNCFZUmCoh0+IkQ\n",
-       "EWxIQo0iKigqomClQxQUEGwkIEGKEOmBUJUACSRgEAEbgdy/P953k5PJzO7s7M6e2d3nc1175Zwz\n",
-       "Z877zOxmnjlvlW1CCCGEzhpQdgAhhBB6p0ggIYQQGhIJJIQQQkMigYQQQmhIJJAQQggNiQQSQgih\n",
-       "IZFAQreTdJGk0+o891JJZzUxlnavL+mrkl6R9KKkYZLekKQmxLGepIckvS7peEmLS7pJ0muSrpH0\n",
-       "CUk313GdsZJ+0t3xhdCIRcoOIPQ9to/rzOn5pypJc4F1bP+t0XBqXV/Se4DPA8Nsz86HBzdYTke+\n",
-       "BNxqe9Nc9qHAu4Ehtufmc67u6CK2v96k+ELotLgDCb1BV+8Iaj3/PcDsQvJoptWBqRX7TxWSR78m\n",
-       "aWDZMYTOiwQS5pF0pKQbC/tPS7qmsP+CpI3z9vqSJkqaLekJSfsXzlug2kjSl3IV0XRJ/ydprqS1\n",
-       "CkUPkfSbXL1zT9tjkv6UH384Vy3tn4/vmauD/iHpLkkbFcoaKemBfK2fA4vXeK27AhOAVfO1L5a0\n",
-       "Ro5tQD5nkqSvSLozX+9mScu38/5VjUvSH4FRwPdzWVcDpwMH5v2jJB0h6Y7CtTYsvL8zJY3Nx8dJ\n",
-       "uqJw3jaS7s5lPiRpx8Jj7cYvaYfCc5+XdLikLXN5Kpy3n6SHarzmJSSdJ2laro67I1fPjZL0QsW5\n",
-       "0yTtXHgdv5R0haR/AqdI+rek5Sp+l6+0JZf8Pk2V9KqkP+Q7yFAm2/ETP9gGWBP4R95eFZgGPJ/3\n",
-       "1wJezdtLAS8Ah5O+hGwKvAJskB+/BPhK3t4DeAnYAFgCuBKYC6yVH78U+DuwBTAwPz6+ENO8c/P+\n",
-       "SGAWsCXpzuIw4FlgUWAQ8BxwYr7WR4G32mKp8np3BF4o7K+RyxuQ9ycBTwPrkBLRbcDXa1yrZlz5\n",
-       "8duAowrnnwlcXtg/Argjbw/O79nn8mtaGtiq8Lwr8vZq+b3bI+/vmveX7yh+0h3Q68CB+b0aAmyc\n",
-       "H3us7Zp5/3rgczVe9w+APwKr5L+FbXLMo4rvbT73WWDnvD0u/272zvuLA7cC/1c4/5vAhXl7n/xa\n",
-       "1svlnArcVfb/mf7+E3cgYR7bzwJvSBoJvB+4GXhR0nqkD9u2O4I9gWdtX2Z7ru2HgOuA/atc9gDg\n",
-       "YtuP2/4P6QNwgWKB62zfZ/sd4CpSQqrlGOBHtv/i5HLgf8C2pA+vRWyfb/sd278C/tLOtTqqGjNw\n",
-       "ie1nbP8XuKad2GrFtU2N8tRO+XsCL9r+ju23bL9pe3KVaxwC/M72HwBs3wLcB3y4jvg/AUy0/Yv8\n",
-       "Xr1q+5H82OX52kgaAuxOlfaZfKd2JHCi7Zfy38I9tt+q8boq3W37xhz7f3MZB+Vri5Tc2so9lpT8\n",
-       "nnSq9vs6sKmkYXWWFZogGtFDpdtJ3x7XyduvkZLHtnkf0rfXrSX9o/C8RUgfPJVWASYX9qdXOWdW\n",
-       "Yfs/pG/ctawOHCbpM4Vji+ZyBMyoOP85utaGMrPO2GrFtWphv96ZS4cB9XQaWB3YX9JehWOLkO4I\n",
-       "2tSKv70yrgIek7Qk6QvAn2zPqnLeCqQ7h7/WEWs1lX8L1wEXSFqZdKcx1/ad+bHVgfMlnVfxnNVI\n",
-       "d8OhBJFAQqXbgb1J1TlnkxLIIaRv0hfkc54Hbre9ex3Xe4n0YdWmq98YnwfOtv21ygdy/f9qFYdX\n",
-       "B57pYpldiquG9pLJ86Rv3/WUeYXtY+oss/K5W1UNzJ4u6R5gP9Lv/sIa1/g78F/Sl41HKh77F7Bk\n",
-       "205ux1ixsqiKcv8haQLptY8AxlfEe5bt4rFQsqjCCpVuB3YCFrf9InAnqR1jCPBgPuc3wLqSDpG0\n",
-       "aP7ZUtL6+fFi9cw1wJFKje5LkhqPizq6O5gFrF3Y/wlwrKStlCwl6cOSlgbuBt6WdEKOaT9Sm0RX\n",
-       "1Hv30l5c1a7V3nV/C6wi6URJi0kaLKnah/2VwF6Sdpc0sNB4XUyitcq5GthV0v6SFpG0vKRNCo9f\n",
-       "DpwMvJd0Z7CQXJV0MfBtSavkGLaVNAh4Clhc0ockLQqcBizWzmsuxnU4qf2qWG32Q1JD+wgAScuo\n",
-       "0HEjlCMSSFiA7aeBN4A78v7rpCqKu+zUmmn7TVK9+MdJVUYvkeqkB7VdJv+Q6+e/R2rAfQr4cz7n\n",
-       "f5XnFsMobI8DLss9hT5m+37gk8D3gVdJDauH5bLmkL41HwHMJlW//Kqjl9yJ/ZpjStqJq/L5ta5V\n",
-       "fM/eAHYD9iK9t0+RqhUrz5tOalw+BXiZ9C39CyyYNGqV8TzwoXz+bNKXg40L515H6uZ8fW6fqOWL\n",
-       "wBRSW9Ns0t+BbP8TGA38lFRV9SYLVjXVei9vJN3RvGR7yryT7RuAc4Cf515bU4APtBNX6AHKnwnd\n",
-       "f2HpYlJj3su227ozbkX6D7Yo8DYw2vZf8mNjgaOAd4ATbE/Ixzcn9dRZnNRgeGJTAg49QtIGpP/8\n",
-       "gxxjIFqapKeBT9n+Y4cnh36pmXcgl5CqPorOBU63PRI4I++Tb0vb6j33AC4s9EO/CDja9nBguKTK\n",
-       "a4YWJ+kjuSpmOdK3yBsjebS2XP3nSB6hPU1LILbvAP5RcfglYJm8vSzze8zsQ+r7P8f2NFKj59aS\n",
-       "VgEGF7owXg7s26yYQ9McQ2rLeAaYA3RmqpPQwyRNIjWcf7rkUEKL6+leWGOAOyV9i5S8ts3HVwXu\n",
-       "KZw3ndSbZg4LdvWbwcK9bEKLs/3BsmMI9bM9quwYQu/Q043oPyO1b7yHNMr24h4uP4QQQjfp6TuQ\n",
-       "rWzvmrd/SeqhAenOojg+YCjpzmNG3i4erxwoBoCk5vQGCCGEPs52Y4NtmzlPCmkw2pTC/gPAjnl7\n",
-       "F+AveXsE8BCpG+iapG6jbT3E7gW2JnVN/B2FOXoqynIzX0uDr39c2TFETH0rrogpYmpCXG70uU27\n",
-       "A5E0njQFxgp5Vs4zSI2pP5C0GGlahWNy9FOVZn2dyvzuvW13FKNJ3XiXoDDvTwghhHI1LYHYPqjG\n",
-       "Q1vXOP9rwELTQDgN0Npo4WeEEEIoU4xEb65JZQdQxaSyA6hiUtkB1DCp7ACqmFR2AFVMKjuAKiaV\n",
-       "HUAVk8oOoLs1bSR6T5NkN9oQFEII/VRXPjvjDiSEEEJDIoGEEEJoSCSQEEIIDYkEEkIIoSGRQEII\n",
-       "ITQklrQNIYR+SGI54NiuXCPuQEIIoR+RWF7iq6TlFYZ35VqRQEIIoR+QeLfEOaQlklcEtrA5qivX\n",
-       "jAQSQgh9mMQqEt8GngCWAja1+ZTNs129diSQEELogySGSnwPeIw0m/l7bY63eaG7yogEEkIIfYjE\n",
-       "6hIXAY8A/wNG2HzO5sXuLisSSAgh9AESa0v8lLTu0j+A9WxOspnZrDKjG28IIfRiEusCpwB7Aj8A\n",
-       "htu82hNlRwIJIYReSGIEcCqwO/A9YB2b13oyhqZVYUm6WNIsSVMqjn9G0uOSHpV0TuH4WElPS3pC\n",
-       "0u6F45tLmpIfO79Z8YYQQm8gsbHENcBtwBRgbZuzejp5QHPbQC4B9igekLQTsDewse33At/Kx0cA\n",
-       "B5LWRt8DuFBS2/z0FwFH2x4ODJe0wDVDCKE/kBgpcR1wM3AvsJbNN2xeLyumDhOIpGUlbZl/lqn3\n",
-       "wrbvIDXkFB0HfN32nHzOK/n4PsB423NsTyONkNxa0irAYNuT83mXA/vWG0MIIfR2EltJ3AT8Brid\n",
-       "dMdxns2/Sg6tdgKRtJikS4FpwI+BnwDPSbpE0qAGyxsOvF/SPZImSdoiH18VmF44bzqwWpXjM/Lx\n",
-       "EELo0yS2k/gD8Evg96TEcb7Nv0sObZ72GtFPAxYFhtl+A0DSYOBC4PT800h5y9neRtKWwDXAWg1c\n",
-       "pypJ4wq7k2xP6q5rhxBCT5DYkfT5ujbwNWBvm7e67/oaBYzqjmu1l0D2A7ayPe82yfYbko4j1b81\n",
-       "kkCmA9fla/1F0lxJK5DuLIYVzhuaz52Rt4vHZ9S6uO1xDcQUQgilkhCwM3AGqZblbOBKmzndXVb+\n",
-       "Yj1pftk6s9FrtdcG8k4xeRQKfxOY22B5N5DeJCStCwyy/XfgRuDjkgZJWpNU1TXZ9kzgdUlb50b1\n",
-       "Q/M1Qgih15OQxB7AXaQxHD8B1re5pBnJo7u1Ow5E0pBqhwF3dGFJ44EdgeUlvUDKrBcDF+euvW8B\n",
-       "hwHYnirpGmAq8DYw2nZbGaOBS4ElgN/Z/kMdryuEEFpWvuPYk1STsyTwVeBam3dKDayTNP9zuuIB\n",
-       "aRrtJArbazYppoZIsm11fGYIIZRDYgCp1+nppBqgs4Dr7YZrdbohpsY/O2smkN4mEkgIoVVJDAQ+\n",
-       "Skoc/wO+Atxkd1yb02xd+eysWYUlabP2nmj7gUYKDCGE/kJiEdIg6VOB14GTgd+3QuLoDu1VYU2i\n",
-       "/SqsnZoUU0PiDiSE0CokFgU+QUocs0h3HLe0YuKIKiwigYQQyicxiNQ56BTSIOyvALe3YuJo05Qq\n",
-       "rBBCCPWRWAw4ChhDWjr2MJs7y42q+SKBhBBCgySWAP6P1LbxMHCgzT3lRtVzIoGEEEInSSwFfAr4\n",
-       "IjAZ2Mfm/nKj6nn1zMY7QNKhks7I+++RtFXzQwshhNYiMVjiZOCvwLbAB2327Y/JA+pbD+RC0hv1\n",
-       "ibz/Zj4WQgj9gsQyEqeSEsemwK42+9s8XHJopaqnCmtr2yMlPQhg+1VJizY5rhBCKJ3EcsCJwPHA\n",
-       "74D32zxRblSto547kLckDWzbkbQijU+mGEIILU9iBYmzSYvbDQO2sTkskseC6kkgFwDXA++W9DXS\n",
-       "rJFfb2pUIYRQAol3S5wDPAWsAGxhc7TNMyWH1pLqGkgoaQNgl7x7q+3HmxpVA2IgYQihURKrACcB\n",
-       "RwBXA+faPF9qUD2kK5+d9dyBQJpueGA+f4lGCgohhFYjMVTiAuAx0ufbRjbH95fk0VX1dOM9g7Qe\n",
-       "xxDSLd0lkhpZjTCEEFqCxOoSFwGPAP8FRth81q694mlYWIdVWJKeAja2/d+8vwTwsO11eyC+ukUV\n",
-       "VgihIxJrA2OBjwA/Ar5j80q5UZWr2VVYM1iw2mpx0nrlHQV1saRZefXByse+kNdDH1I4NlbS05Ke\n",
-       "kLR74fjmkqbkx86vI94QQliAxLoSlwH3Ai8Cw21O6e/Jo6tqJhBJF0i6APgn8JikSyVdCjyaj3Xk\n",
-       "EmCPKtcdBuwGPFc4NoI0Z/6I/JwL8xroABcBR9seDgyXtNA1QwihGokREleReo8+A6xjc4bNqyWH\n",
-       "1ie0N5DwftJ6IPcDNxSOT6KONdFt3yFpjSoPfRv4EvDrwrF9gPG25wDTJD0DbC3pOWCw7cn5vMuB\n",
-       "fYFYFz2EUJPExsBpwI7Ad4DjbF4vN6q+p2YCsX1pdxcmaR9guu1H5t9gALAqLDCD5XRgNWAOC1aX\n",
-       "zcjHQwhhIRKbkZaN3QY4DzjK5s1yo+q7OpzKRNKzVQ7b9lqdKUjSkqRFVnYrHu7MNeooY1xhd5Lt\n",
-       "Sd15/RBCa5LYipQ4NgPOBQ62+Xe5UbUmSaOAUd1xrXrmwtqysL048DFg+QbKWhtYA3g4330MBe6X\n",
-       "tDXpzmJY4dyhpDuPGXm7eLxmNzvb4xqIK4TQS0lsB5xBaj/9BrC/zX/Ljaq15S/Wk9r2JZ3Z6LU6\n",
-       "7IVl+++Fn+m2vwt8uLMF2Z5ieyXba9pek5QgNrM9C7gR+LikQZLWBIYDk23PBF6XtHVuVD+UBdtj\n",
-       "Qgj9kMSOErcCVwHXkXpVXRjJo2fVU4W1OfMbzQcAW5BGpXf0vPGkBqzlJb0AnGH7ksIp8xribU+V\n",
-       "dA0wFXgbGO35A1RGkwYyLgH8znY0oIfQD0kI2Jl0x7EacDZwpc2cUgPrx+oZSDiJ+R/2b5MWiv+W\n",
-       "7SebGlknxUDCEPqmnDg+QEocQ4CvAj+3ebvUwPqIrnx21pNA1rL9t4pja9qu1rhemkggIfQtOXHs\n",
-       "SUocSwJnAdfavFNqYH1MsxPIA7Y3qzh2v+3NGymwWSKBhNA3SAwgjfc6jVRd/hXgejvWIWqGrnx2\n",
-       "1mwDyVO4jwCWlbQfqcutgXeRemOFEEK3kRgIfJTUHfd/wJeBmyJxtK72GtHXBfYClsn/tnkD+GQz\n",
-       "gwoh9B8Si5CmMjqNNE3SycDv7Y5nvAjlqqcKazvbd/dQPA2LKqwQeheJRYFPAKcCs0hVVbdE4uhZ\n",
-       "TW0D6S0igYTQO0gMAg4jzUwxjZQ4bo/EUY6mtIGEEEJ3klgMOAoYAzwJHG5zR7lRha6IBBJCaCqJ\n",
-       "xUntpicDDwMH2gtMnhp6qXqWtF1Z0s8k/SHvj5B0dPNDCyH0ZhIDJY4k3W3sDuxr8+FIHn1HPSsS\n",
-       "XgpMIE25DvA08LlmBRRC6N0kJLEvab3xI4GDbPayua/k0EI3qyeBrGD7F5BGf+ZFn2IKgRDCQiR2\n",
-       "BO4mjeE4CdjRpuV7cYbG1NMG8qakedO3S9qG+pa0DSH0ExKbAl8DNiANBLw6BgD2ffUkkC8ANwFr\n",
-       "SbobWJG0JkgIoZ+TWIs0R9UupNlx97V5q9yoQk+paxyIpEWB9fLuk7kaq6XEOJAQeo7ESqQ7jYOA\n",
-       "84Hv2LxRblShET0xDmQr0mqCiwCbScL25Y0UGELovSSWAb5IWqfncmB9m1fKjSqUpZ4Fpa4E1gIe\n",
-       "ggWmUY4EEkI/kcdyjCbPUwVsZvNcuVGFstVzB7I5MMKdnPNE0sWkpW9ftr1RPvZN0vz+bwF/BY60\n",
-       "/c/82FjSKNV3gBNsT8jHNyd1JV6ctCLhiZ2JI4TQuDxD7mHAONKXyF1sHi01qNAy6unG+yiwSgPX\n",
-       "vgTYo+LYBGBD25sATwFjIQ1OJM3GOSI/58K8BjrARcDRtocDwyVVXjOE0M1qjOXYJ5JHKGpvPZCb\n",
-       "8ubSwFRJk0lz9APY9t7tXdj2HZLWqDg2sbB7L2nuf4B9gPG5cX6apGeArSU9Bwy2PTmfdzlpoZlY\n",
-       "Fz2EJsljOb5BWgXwJGJq9VBDe1VY5+V/TVpMqqg7/piOAsbn7VVhgekNpgOrAXPydpsZ+XgIoZvF\n",
-       "WI7QWTUTiO1JAJLOtf2l4mOSzgFub7RQSacCb9m+utFr1LjuuMLupLbXEEKoLcZy9C+SRgGjuuNa\n",
-       "9TSi71bl2IdIvTE6TdIR+fm7FA7PAIYV9oeS7jxm5O3i8Rm1rm17XCMxhdAfVRnLcWyM5ej78hfr\n",
-       "SW37ks5s9Fo1G9ElHSdpCrCepCmFn2mkhrVOyw3gJwH72P5v4aEbgY9LGiRpTWA4MNn2TOB1SVvn\n",
-       "RvVDgRsaKTuEkEgsI3EWMJVUTby+zVcieYTOau8O5GpSf+9vkO422tpB3rA9u6MLSxoP7AisIOkF\n",
-       "4ExSr6tBwMTcyerPtkfbnirpGtIf9NvA6EK34dGkbrxLkLrxRgN6CA2IsRyhu8WStiH0cVXGcpwa\n",
-       "3XFDm1jSNoSwEAmRusifDcwmjeWIqdVDt4kEEkIfFGM5Qk+oK4FIWhnYkjT+Y7Ltl5saVQihITGW\n",
-       "I/SketZEP4A0anx/4ABgsqT9mx1YCKF+EmtJXEWapeH3wHo2V0byCM3UYSO6pEeAXdvuOiStCNxq\n",
-       "e+MeiK9u0Yge+qNYlyN0VVc+O+uZTFGwwHz/s1l4apMQQg+KsRyhFdTTBvIH4GZJV5MSx4GkW+QQ\n",
-       "Qg+LsRyhldS7pO1Hge3z7h22r29qVA2IKqzQl8VYjtAsXfnsrKcN5BzbJ3d0rGyRQEJfVGUsx5gY\n",
-       "yxG6U7MTyIO2R1Ycm9K2ymCriAQS+pqKsRxjibEcoQmaMhJd0nGkuta186SKbQYDdzVSWAihYzGW\n",
-       "I/QWNe9AJC0DLEeDkyn2tLgDCb1dlXU5fhTrcoRma2oVVm8RCST0VjGWI5Sp2eNAQghNEGM5Qm8X\n",
-       "CSSEHiaxuMTngadIK3FuZvM5e4EBuyG0vKYlEEkXS5pVbICXNETSRElPSZogadnCY2MlPS3pCUm7\n",
-       "F45vnldCfFrS+c2KN4RmkxgocSTwJGmxtV1sjoiBgKG3am9J2zclvVHj5/U6rn0JsEfFsTHARNvr\n",
-       "ArfmfSSNII1wH5Gfc2FewhbgIuBo28OB4XlZ3BB6DQlJ7EtaCvpI0roc+8RAwNDb1ezGa3tpAElf\n",
-       "BV4ErswPHQys2tGFbd8haY2Kw3uTvnkBXEZa2H0MaaDUeNtzgGmSngG2lvQcMNj25Pycy4F9SdOr\n",
-       "hNDyYl2O0JfVMxfW3hUz716UZ+g9vYHyVrI9K2/PAlbK26sC9xTOmw6sRmpYnF44PiMfD6GlxViO\n",
-       "0B/U0wbyL0mHSBqYfw4G3uxqwU79h+ObWOhTYl2O0J/UcwfyCVLf9O/m/bvysUbMkrSy7ZmSVgHa\n",
-       "VjacQeqN0mYo6c5jRt4uHp9R6+KSxhV2J9me1GCcIXRKlbEcx0Z33NCKJI0CRnXLtZo5kDC3gdzU\n",
-       "Nm+WpHOB2bbPkTQGWNb2mNyIfjWwFamK6hZgHduWdC9wAjAZ+C3wPdsLtYHEQMJQBollgC+Spv25\n",
-       "HPhadMcNvUlTBxJKWk/SrZIey/sbSzqtjueNB+4G1pP0gqQjSY2Ju0l6Ctg572N7KnANaUDV74HR\n",
-       "np/ZRgM/BZ4GnqmWPELoaTGWI4T6ZuP9E6n3yA9tj8zdax+1vWFPBFivuAMJPSHW5Qh9TVNm4y1Y\n",
-       "0va9bcMycrXSnEYKC6G3qrIux0GxLkfo7+pJIK9IWqdtR9LHgJeaF1IIrSXGcoRQXT1VWGsDPwa2\n",
-       "BV4DngUOtj2t6dF1QlRhhe4WYzlCf9C0KixJA4HjbO8iaWlggO16pjEJodeSWBn4JrAbqcpq31iX\n",
-       "I4SFtdsLy/Y7wA5KKerNSB6hL5MYIPEpYAppvNFwmwsieYRQXT1tIA8Bv5Z0LfDvfMy2r2teWCH0\n",
-       "LIkNgR+RvlTtbDOlg6eE0O/Vk0AWI/U62bnieCSQ0OtJLAGcBhwDnEFaRjbaOUKoQz1tIK/a/kIP\n",
-       "xRNCj5HYlbRcwIPAJjYvlhxSCL1KuwnE9juSts9tINFtMfQJEisC3wbeBxxv85uSQwqhV4o2kNBv\n",
-       "5MGAR5DGdFwBvNfu+szSIfRX9SSQxYFXiTaQ0ItJrEdqJF8K2MPmwZJDCqHXa+psvD0pBhKGaiQW\n",
-       "I616+RngLOD7Nu+UG1UIraMlZ+MNoWx5CpKHgc2AkTbnR/IIofvUsyLhT4BTYN5gqimkRXNCaEkS\n",
-       "QyR+BlwJjLXZx+aFsuMKoa+pJ4Esafvetp3cGytm4w0tR0ISh5DWlfkXsKHN9SWHFUKfFbPxhj5B\n",
-       "Ym3SmI53A3vbTC45pBD6vHruQI4n9V5ZT9KLwOeA47pSqKSxkh6TNEXS1ZIWkzRE0kRJT0maIGnZ\n",
-       "ivOflvSEpN27UnboWyQGSYwF7gUmAltG8gihZ9RMIJJOzJur2N6F9M1ufdvbd2Uq97xO+ieBzfJa\n",
-       "6QOBj5N6yky0vS5wa94nr5d+IDAC2AO4UFI9iS/0cRLbAfeTBgRuYfNNO6pXQ+gp7X0QH5X/vQCg\n",
-       "G2fjfZ3UhrKkpEVIi/S8COwNXJbPuQzYN2/vA4y3PScnrmeArbohjtBLSSwrcRHwS1LX3A/bTCs3\n",
-       "qhD6n/baQKZKehpYTVLlzKS2vXEjBdp+VdJ5wPPAf4CbbU+UtJLtWfm0WcBKeXtV4J7CJaYDqzVS\n",
-       "dujd8kjy/YHvADcBI2xeKzeqEPqvmgnE9kGSVgYmAHsB3TJIL69w+FlgDeCfwLWSDqko25LaG+HY\n",
-       "N0Y/hrpJrAH8gPR3c4DNXaUGFELocDLFmcDGkpYA3mP7yW4ocwvgbtuzASRdR1oud6aklW3PlLQK\n",
-       "8HI+fwYwrPD8ofnYQiSNK+xOsj2pG+INJZJYhPSFYwxpAsSPxAJPITRO0ihgVLdcq4410fcmLe+5\n",
-       "mO01JI0Evmx774YKlDYBrgK2BP4LXApMBlYHZts+R9IYYFnbY3Ij+tWkdo/VgFuAdSpnB46pTPoe\n",
-       "iS2BH5PWoznW5pmSQwqhz2namujZOGBr4DYA2w9KWquRwvLzH5Z0OXAfMBd4gPQhMRi4RtLRwDTg\n",
-       "gHz+VEnXkAaHvQ2Mjqnl+zaJwaS1yA8AvghcZUe1ZQitpp47kHttby3pQdsj87FHGm1Eb5a4A+kb\n",
-       "JPYl9fybCJxkM7vkkELo05p9B/KYpIOBRSQNB04A7m6ksBBqkRhKShwjgENtJpUbUQihI/WORN8Q\n",
-       "+B8wnjSO47PNDCr0HxIDJU4gLVz2MLBxJI8Qeod2q7DyQL+JtnfquZAaE1VYvY/ESFL7179IjeRP\n",
-       "lBxSCP1O09YDsf02MLc4L1UIXSWxlMS3gJtJEyDuFMkjhN6nnjaQfwFTJE3M25DG+p3QvLBCXyXx\n",
-       "IeBC4E7SmuQvd/CUEEKLqieBXJd/2uq6RIwED50ksQpwPml1wE/aTCw5pBBCF8Wa6KGpJAYAx5Am\n",
-       "Pfwx8FWb/5QbVQihTbO78YbQEIn3kpKGSe0cj5YcUgihG8W6GqHbSSwh8TXS7AWXAe+L5BFC39Pe\n",
-       "glJX5H9jzEeom8RuwBRgbdKYjh/ZzC05rBBCE9RsA5E0FdgV+ANVZm60/WpTI+ukaAMpl8S7SbPl\n",
-       "7gCMtvldySGFEOrQrDaQH5KWll2LtGxokfPx0M/lRZ6OAr5Oqq7a0J7X3TuE0IfVM5niD20f20Px\n",
-       "NCzuQHqexPrAj4AlgGNsHio5pBBCJ3Xls7OubrySBpKWmJ13x2L7+UYKbJZIID1HYnFgLPBp4MvA\n",
-       "hTbvlBtVCKERTe3GK+kzwJmkFQKLHxIbNVJg6N0kRpHuOqYCm9pMLzeiEEJZ6qnC+iuwVdsStK0q\n",
-       "7kCaS2J50sqUuwGfsbmh5JBCCN2gaZMpZs+TpnDvNpKWlfRLSY9Lmippa0lDJE2U9JSkCcUJHCWN\n",
-       "lfS0pCck7d6dsYT2SUjiUOAx4A1gRCSPEAK03433C3lzBLA+8BvgrXzMtr/dcKHSZcDtti/OU8Yv\n",
-       "BZwK/N32uZJOBparWBN9S+avib6u7bkV14w7kG4msQ6pN97ypEbyv5QcUgihmzXrDmQwsDTpDmQi\n",
-       "MCjvL50KByWiAAAY60lEQVQfa4ikZYD32b4Y0pTxtv8J7E3qBkr+d9+8vQ8w3vYc29OAZ4CtGi0/\n",
-       "dExikMSpwD3A74EtI3mEECrVbES3Pa5JZa4JvCLpEmAT0hiTzwIr2Z6Vz5lF6vUFsCrpg6zNdNKd\n",
-       "SGgCie1JjeTPAVvYTCs3ohBCqypjMsVFSFN6H2/7L5K+C4wpnmDbktpr3a/6mKRxhd1Jtid1MdZ+\n",
-       "Q2I54BvAnqSE/ks7pu0Poa+RNIoqs4s0oowEMh2YbrutSuSXpDEFMyWtbHumpFVg3kJDM4BhhecP\n",
-       "zccW0sS7pj4rjyQ/APgOcANpJPlr5UYVQmiW/MV6Utu+pDMbvVaHvbAk7VDl2PaNFmh7JvCCpHXz\n",
-       "oV1JPXxuAg7Pxw6HeT19bgQ+LmmQpDWB4cDkRssP80msCfwOOA34qM3oSB4hhHrVMw7kQdsjOzrW\n",
-       "qUKlTYCfkhrm/wocCQwErgHeA0wDDrD9Wj7/FNJ8S28DJ9q+uco1oxdWnSQWJVVTnQycB3zLZk65\n",
-       "UYUQytCUqUwkbQtsB3yONMtqWwGDgY/Y3qSRApslEkh9JLYiLfL0MnCczV9LDimEUKJmTWUyiJQs\n",
-       "BrJgt93XgY81Ulgoj8S7gLNJv7svAldHI3kIoSvqqcJaI4+/aGlxB1JdbiT/CPA90touX7JpqbVc\n",
-       "Qgjlafaa6ItJ+gmwRuF82965kQJDz5EYBnwfWA/4hM2fSg4phNCH1JNArgUuIjV6t83GG1UfLUxi\n",
-       "IHA8cDpwAXCAzf/KjSqE0NfUk0Dm2L6o6ZGEbiGxGamR/A1ge5snSw4phNBH1TMb702SPi1plTxj\n",
-       "7hBJQ5oeWegUiaUlziPNXfV9YOdIHiGEZqqnEX0aVaqsbK/ZpJga0p8b0SX2BH4A3A58weaVkkMK\n",
-       "IfQSTV/StjfojwlEYlXgfGAkcKzNLSWHFELoZZq6oJSkpSSdnntiIWm4pD0bKSx0D4kBEqOBh4En\n",
-       "gY0ieYQQelo9jeiXkKZc3y7vv0iaAPE3zQoq1CaxEamRfC4wyuaxkkMKIfRT9TSir237HPJqhLb/\n",
-       "1dyQQjUSS0p8A/gjKam/L5JHCKFM9SSQ/0laom1H0toQYwp6ksQHgCmkwZwb2fzYZm77zwohhOaq\n",
-       "pwprHGkKjKGSrga2B45oYkwhk1iJtE7HtsBom9+XHFIIIcxTVy8sSSsA2+Tde2z/valRNaAv9cKS\n",
-       "GECavv5rwKXAl22i6jCE0O2aNZ37BrYfl7Q5aRxIWwEGsP1AIwU2S19JIBIbkNYkXww4xubhkkMK\n",
-       "IfRhzUogP7H9SUmTqD6QcKdGCmyW3p5AJBYHTgFGk6oNL7LnzT0WQghN0SsHEkoaCNxHWh99rzw9\n",
-       "yi+A1Vl4RcKxpCqdd4ATbE+ocr1em0AkdiLddTwKfMauvuZ7CCF0t2YPJPy0pOUK+8tJGt1IYRVO\n",
-       "BKYy/+5mDDDR9rrArXkfSSOAA4ERwB7AhZLq6T3W8iRWkLgUuAw4yWa/SB4hhN6ing/iY2z/o20n\n",
-       "bx/TlUIlDQU+RJoivi3z7U36ICX/u2/e3gcYb3tOXtjqGWCrrpRfNglJHEa643gN2NDm1yWHFUII\n",
-       "nVJPN94BkgbYngvzqp4W7WK53wFOAt5VOLaS7Vl5exawUt5eFbincN50YLUull8aieHAD4HlgD1t\n",
-       "7is5pBBCaEg9CeRm4OeSfkS6W/gUaVxIQ/I8Wi/bflDSqGrn2Lak9hpnqj4maVxhd5LtSY3G2d0k\n",
-       "BgFfAj5LWpv8Apu3y40qhNDf5M/dUd1xrXoSyMmkKqvj8v5EUtVTo7YD9pb0IWBx4F2SrgBmSVrZ\n",
-       "9kxJqwAv5/NnAMMKzx+ajy3E9rguxNU0EjuQ5q/6K7C5zXMlhxRC6KfyF+tJbfuSzmz0WqVO5y5p\n",
-       "R+CLuRfWucBs2+dIGgMsa3tMbkS/mtTusRpwC7COKwJvxV5YEssB5wAfJnUa+JUdywGHEFpHVz47\n",
-       "a96BSLrW9v6SHmXhKiPb3riRAqtou/Y3gGskHU3uxpsLmirpGlKPrbeB0ZXJoxVJfBD4GXA9MMLm\n",
-       "nyWHFEII3aq9gYSr2n5R0urM7yk1T+4R1TJa6Q4k97A6F9jf5o6y4wkhhFqaNRL9AdubSbrC9qFd\n",
-       "irAHtEoCkfg8qaH8AzaPlx1PCCG0pylVWMBikg4Gtpe0Hwvehdj2dY0U2FdJiNS76iPADjbPlxxS\n",
-       "CCE0VXsJ5FjgYGAZYK8qj0cCySQGAhcBm5IWemq52YpDCKG7tZdAVrZ9bK7K+nGPRdTL5EkQryIl\n",
-       "2l1s3ig5pBBC6BHtTWVySv73uHbO6dckBgO/Ja1P/uFIHiGE/qS9O5DZkiYCa0q6qeIx2967iXG1\n",
-       "PIkVgd+TZhT+dEy9HkLob9pLIB8CNgOuBL5FRSN6M4NqdRLvIY3IvxY4PQYHhhD6ow5Hokta0fYr\n",
-       "kpay3bLLqvZUN16JEaS5wL5t891mlxdCCM3U1PVAgOGSpgJP5MI2lXRhI4X1dhJbA38ETo3kEULo\n",
-       "7+pJIN8lLeT0dwDbDwE7NjOoViSxO/Ab4GibK8qOJ4QQylbXyn62KwfF9atpyCUOBK4APmLz27Lj\n",
-       "CSGEVlDPdO7PS9oeQNIg4AToP1N0SIwGTgV2s3mk7HhCCKFV1NWIDpwP7ErqiTUBOMH27OaHV7/u\n",
-       "bkTPU5OcDhwG7G7zt+66dgghtIqmTKbY23RnApEYQEqa7wP2sJnZHdcNIYRW09ReWJKGSbpe0iv5\n",
-       "51eShjZSWG+Ql569EtgEGBXJI4QQqqunEf0S4EZg1fxzUz7W50gsBfwaWJo0HftrJYcUQggtq54E\n",
-       "sqLtS2zPyT+XAu9utMB8R3ObpMckPSrphHx8iKSJkp6SNEHSsoXnjJX0tKQnJO3eaNntx8UQ0ujy\n",
-       "WcB+Nv9pRjkhhNBX1JNAZks6VNJASYtIOgS6NF35HOBztjcEtgE+LWkDYAww0fa6wK15n7wm+oHA\n",
-       "CNJ4lAsl1dX9uF4SqwF/Au4GjrL7VzflEEJoRD0fxEeR1iefCbwE7A8c2WiBtmfmwYjYfpPUJXg1\n",
-       "YG/gsnzaZcC+eXsfYHy++5kGPANs1Wj5lSSGA3eSxnmcZDO3u64dQgh9WYfjQPKHdrUFpbpM0hrA\n",
-       "SOBeYCXbs/JDs4CV8vaqwD2Fp00nJZxuKJ/NSKPLz7D5aXdcM4QQ+osOE4iky0njPl7L+8sB59k+\n",
-       "qisFS1oa+BVwou03pPm9yGxbUnv9i6s+JmlcYXeS7Um1y2dz0nTsx9qxumIIoX+QNAoY1R3Xqmck\n",
-       "+sZtyQPA9j8kbdaVQiUtSkoeV9i+IR+eJWll2zMlrQK8nI/PAIYVnj40H1uI7XH1lc9g4BfAZyJ5\n",
-       "hBD6k/zFelLbvqQzG71WPW0gkjSksDMEGNhogUq3Gj8Dptouzmh7I3B43j4cuKFw/OOSBklaExgO\n",
-       "TG60/OwHwG02v+jidUIIod+q5w7kPODPkq4hTWWyP3B2F8rcHjgEeETSg/nYWOAbwDWSjgamkRru\n",
-       "sT01lz2VNInjaHdh+LzEocCWwBYNv4IQQgj1TWUiaUNgZ1Lbwx9tT212YJ1Vz3B8iXWAPwO72jzc\n",
-       "M5GFEELrirmw6PhNyFOU3AlcYXNBz0UWQgitq9krEvYVZ5G6B3+/7EBCCKEvqKcNpNfLqwkeDIy0\n",
-       "q3cBDiGE0Dl9PoFIvJs0+eNhNq+UHU8IIfQVfboKK6/rcSlwmc2tJYcTQgh9Sp9OIMBngCFAwwNl\n",
-       "QgghVNdne2FJLAP8FdjO5qnyIgshhNYVvbCqOw74QySPEEJojj55ByKxJPA30oDBR8uNLIQQWlfc\n",
-       "gSzsaOCeSB4hhNA8fe4OJI84fwb4mN3lSRdDCKFPizuQBR0MPBnJI4QQmqtPDSSUGEhaS/3YsmMJ\n",
-       "IYS+rq/dgewHvEphsZQQQgjN0dcSyKnA2THfVQghNF+vSSCS9pD0hKSnJZ1c47T/Ar/tybhCCKG/\n",
-       "6hUJRNJA0jTsewAjgIMkbVDl1O1a6e4jL17fUiKm+rViXBFTfSKmntErEgiwFfCM7Wm25wA/B/ap\n",
-       "PMlmbo9H1r5RZQdQxaiyA6hiVNkB1DCq7ACqGFV2AFWMKjuAKkaVHUAVo8oOoLv1lgSyGvBCYX96\n",
-       "PhZCCKEkvSWBtEy1VAghhKRXjESXtA0wzvYeeX8sMNf2OYVzWv+FhBBCC2p0JHpvSSCLAE8CuwAv\n",
-       "ApOBg2w/XmpgIYTQj/WKkei235Z0PHAzMBD4WSSPEEIoV6+4AwkhhNB6eksjek11DjBsRrkXS5ol\n",
-       "aUrh2BBJEyU9JWmCpGULj43NMT4hafcmxTRM0m2SHpP0qKQTWiSuxSXdK+khSVMlfb0V4srlDJT0\n",
-       "oKSbWiEmSdMkPZJjmtwiMS0r6ZeSHs+/v63LjEnSevn9afv5p6QTyn6fCuU8JmmKpKslLVZ2XJJO\n",
-       "zPE8KunEfKx7YrLda39I1VnPAGsAiwIPARv0UNnvA0YCUwrHzgW+lLdPBr6Rt0fk2BbNsT4DDGhC\n",
-       "TCsDm+btpUntRhuUHVcua8n87yLAPcAOLRLX54GrgBtb5Hf4LDCk4ljZMV0GHFX4/S1TdkyF2AYA\n",
-       "LwHDyo4pX/tvwGJ5/xfA4WXGBbwXmAIsTvq8nAis3V0xNeWX2lM/wLbAHwr7Y4AxPVj+GiyYQJ4A\n",
-       "VsrbKwNP5O2xwMmF8/4AbNMD8d0A7NpKcQFLAn8BNiw7LmAocAuwE3BTK/wOSQlk+YpjpcVEShZ/\n",
-       "q3K8Jf6mgN2BO1ohJmAI6UvbcqREexOwW8m/v48BPy3snwZ8qbti6u1VWK02wHAl27Py9ixgpby9\n",
-       "Kim2Nk2PU9IapDuke1shLkkDJD2Uy7/N9mMtENd3gJNggRkMyo7JwC2S7pP0yRaIaU3gFUmXSHpA\n",
-       "0k8kLVVyTEUfB8bn7VJjsv0qcB7wPKm36Gu2J5Yc16PA+3KV1ZLAh0hfnLolpt6eQFq2B4BT+m4v\n",
-       "vqbFLmlp4FfAibbfaIW4bM+1vSnpj/f9knYqMy5JewIv234QqNoHvqT3anvbI4EPAp+W9L6SY1oE\n",
-       "2Ay40PZmwL9Id/plxgSApEHAXsC1CxVYQkyS1gY+S6qZWBVYWtIhZcZl+wngHGAC8HtS9dQ73RVT\n",
-       "b08gM0h1n22GsWD27GmzJK0MIGkV4OV8vDLOoflYt5O0KCl5XGH7hlaJq43tf5JmTN685Li2A/aW\n",
-       "9CzpG+zOkq4oOSZsv5T/fQW4njQPXJkxTQem2/5L3v8lKaHMbIG/qQ8C9+f3Csr/O98CuNv2bNtv\n",
-       "A9eRqtlLfa9sX2x7C9s7Av8AnqKb3qvenkDuA4ZLWiN/GzkQuLHEeG4kNZqR/72hcPzjkgZJWhMY\n",
-       "Dt2/5K4kAT8Dptr+bgvFtUJbLw9JS5DqhR8sMy7bp9geZntNUjXIH20fWmZMkpaUNDhvL0Wq359S\n",
-       "Zky2ZwIvSFo3H9oVeIxUv1/a31R2EPOrr9rKLjOmJ4BtJC2R/y/uCkyl5PdK0rvzv+8hLbp3Nd31\n",
-       "XnV3Q1JP/5C+hTxJ6i0wtgfLHU+q53yL1A5zJKkR7RZShp8ALFs4/5Qc4xPAB5oU0w6k+vyHSB/Q\n",
-       "D5KmwC87ro2AB3JcjwAn5eOlxlUoa0fm98IqLSZSe8ND+efRtr/nst8nYBNSx4eHSd+ql2mBmJYC\n",
-       "/g4MLhwr/e+J1ED9GCnxX0bqzVT2e/WnHNNDwE7d+V7FQMIQQggN6e1VWCGEEEoSCSSEEEJDIoGE\n",
-       "EEJoSCSQEEIIDYkEEkIIoSGRQEIIITQkEkgLywMkp3R8Zl3X2lHStp19rDtJWl9pSvf7Ja3V7PI6\n",
-       "iOUEpanJr8iDpm7Jcz0dkOd72qCd5+6lBpcOkLSMpOM6+1gH1yy+lk7HJukdpWnR23432+bjq0s6\n",
-       "qBPXGSPpE3n7eElH5O0Ffu/VrinpzPaOSdotzw/2SP53p8Jjt7YNwKx1PaVp1W9XmpNtlPL0/XW8\n",
-       "pm9XTicT5otxIC1MaULEm2xv1A3XGge8Yfu8Tj420PY7lccbjGEMMND22Z14zgDbczs+s9OxPA7s\n",
-       "YvtFSdsAZ9nerbvLqVLuGtT4nTb6+y6+lgZjesN22wj43YFTbI+SNAr4gu296rzOH4H9gVdJA0e3\n",
-       "dFpNdN7vvfKaks4mTfi5G2kQ7MXAAVWOCZhpe6akDYGbbQ/N1/gkaUDhtyUdDKwCLJ/jeNH2VZKO\n",
-       "Is1y/M16X5ekAaSpz8+zvXc970G/06wRmfHTLSNI1yBNhfBj0sjkm4HF82NrkyZHu4800nS9fHwv\n",
-       "0nobD5Dm/n93vs5LpHmNHgR2qCij7bEHSKPZLwV+mK/zLWBL4O78+F3Auvm5R5BGJv+eNKL1nHx8\n",
-       "YL7GFNLI88+SZgxoK+fWfN4hpA+KB3N5A/LxN3O5DwHbVbwn65BG0D4E3A+smY9/s1DeAYXzTyJN\n",
-       "xfAwMC4f+yHwv3zul4Cngdfy61sLmARsns/dI5fzEDCx8LovyNsrkuaHmpx/tsvHx5E++G4D/gp8\n",
-       "Jh//OfDv/JrPqXhtCz1W63UVnlN8LZ+tiO1S4Pz8O/sr8NEaf2dvFLb3B67L2/fk9+XBfO3D266d\n",
-       "H/8NsGPefhdwZ97eARiftz9U+L3/Efhz4Zon5nMuIn3YDy9ce6FjhccEzAYWzfsrAZMLjx8EvF3x\n",
-       "dzCR+X+3o/Lv5VrgceDKwnnTgG/k3/kB+dgjFEZqx0/hd1F2APHTzi8nfbjPATbO+78ADs7btwLr\n",
-       "5O2tmf+hXJyS4P+Ab+XtM4HP1yhngceAS0hz4rTdoQ4mfYOENL/PL/P2EfmDaTCwWP7PN5Q0UeKE\n",
-       "wvXeVVkOaaGrGwvXvRA4NG/PBT5WI9Z7gX3y9iBgCeCjpOkYREqYz5HWONgd+FE+dwDpA+99ef9Z\n",
-       "8sJNpKlMbiqUcRtpwsAVSVNzr158byl8kJLmFdo+b7+HNA8ZpARyJ2kqi+VJ024MBFansIZMxWtb\n",
-       "4LFar6vK84qvpRjbpcAvCu/30zXKfZv0gf446cN9ZI33pTKB3AS8P2/vx/wEPYYF/56Kv/fKa54F\n",
-       "7A18j5TsNq52rCLej1H4+8rH/kZaRO0g4IvA10lfHg7K7/tLhXNH5de5an5v72Z+4n8W+GLFtS8D\n",
-       "Plj250Er/ixCaHXP2n4kb98PrJEn2tsOuDbN2QakD1OAYZKuIX2ADiL9x2pTddryGo9d6/y/B1gW\n",
-       "uFzSOqSpnYt/N7c6TxkvaSr5QxRYS9L3SDPvTqhSzi6kRHNffg1LADPzY++QZhReMMBUz72q7V8D\n",
-       "2H4rH98euDrH+7Kk20l3TTsCu0t6MF9iKdIdzB0dvPa2Y9sAf7L9XC7vtSrn7QpsUPg9DM6/HwO/\n",
-       "tT0HmC3pZdI35c78Dmq9rrrq73MMN+TYH5e0Uo3z/uM0hTy5Ou8K0kp27cVaaQ/SRJ6Q/gburHhc\n",
-       "Ff+S4zo9lzvS9pfz4UeqHCMf25B0h1BZ3TgLGGZ7fD7vTNvfzNsrAW9UnD/ZucpPaZ2aNUiJBNIX\n",
-       "taIX8+OhQiSQ1ve/wvY7pKUpBwD/aPtPX+EC0l3HbyTtSPom3Ih/F7bPIiWKj0hanVTFUyu+RWy/\n",
-       "JmkT4APAsaQ67aOrlHGZ7VOqHP9vIXnVq9aH3ddt/7iT12pTTwwCtm5LZvMOpoRSPPYOjf1/q3xd\n",
-       "nX1fijF0mBBs36M0e/IKVR5+mwU73ixe2N4S+FRnyqoo98sdHZM0lFRleqjtZytOF4WFwapcrzKe\n",
-       "hf5uC/v/qvLcaCyuInph9T7K3/iflfQxSNO4S9o4P/4u0jcmSFVMbd4gVTVV095jldc8sqP4JC1P\n",
-       "qpq6DjidVB0EC/4nvhX4mKQV85OGKE03XVN+3dMl7ZOfs5jS9PB3AAfmHjYrAu8nVXXdDByV7wiQ\n",
-       "tFpbeXUwqQ3g/blxG0lDqryOCcAJhRe/SQfX7czvodrr6mi677o+uCU9UeP4+qTPhdlV4pkGbJr/\n",
-       "3oaR1ippuyt4opD026oQq+nob61WvMuS7mZPtv3nKqesRO21gP5Oqt5q1Cqk1x4qRAJpfZXffNr2\n",
-       "DwaOzrffj5LqjCHdcVwr6T7glcL5NwEfyd01t6+4ZttjD0jaoUq55wJfl/QAqT7ZhXOqxbcacFuu\n",
-       "OrqC+SvYzTvf9uOk9ZknSHqY9EG8cuG8Wg4FTsjPuYu0NOf1pGqPh0mJ6STbLzstJ3o18GdJj5Aa\n",
-       "Tat9kFR7Hdj+O3AMcF1+n8dXOf8EYAtJD0t6jAW/hVe75mzgLklTJJ3T3mO1XleN+Gu9loW2q9xd\n",
-       "LJH/Lh4kNeQfnpPBw8A7Sl1wT7R9F6mNYCqpbeJ+UsL6IKkjRZs7SYsrVYtxgWtWeS21HE/qOHJm\n",
-       "W6yFLx8rA7NtV945pIJTL8JHJa1XiKUzdxQjSY3/oUJ04w2hn5H0YVLvte930/UmkKqVZuV9kXq0\n",
-       "LVS11wySjgGWsv2dds45gvRl45xa59R43rqkKuHoxltFJJAQQreTNJrUOH9JD5R1K6ln3pvtnDOI\n",
-       "1P17x860r0n6Nqlbc2WngEAkkBBCCA2KNpAQQggNiQQSQgihIZFAQgghNCQSSAghhIZEAgkhhNCQ\n",
-       "SCAhhBAa8v/Onrp6J+51IAAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaadcc88>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "from math import tanh\n",
-    "Af=(20*0.75*12*2)/(144);\n",
-    "Ao=((3.14*1.25)-(20*0.035))*(12/144);\n",
-    "print\"\\t fin surface is : %.1f ft**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  ft**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "Ai=(3.14*1.06*12)/(144);\n",
-    "print\"\\t total inside surface :  ft**2/lin ft \\t\",Ai\n",
-    "print\"\\t fin efficiencies \\t\"\n",
-    "b=0.0625; # ft\n",
-    "hf=4; # from table in solution\n",
-    "m=(5.24*(hf**(1/2))); # m=((hf*P)/(Kax))**(1/2), eq 16.8\n",
-    "n=(tanh(m*b))/(m*b); # efficiency , eq 16.26\n",
-    "print\"\\t hf      m      n \\t \"\n",
-    "print hf   \n",
-    "print m      \n",
-    "print n\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "print\"\\t weighted efficiency curve \\t\"\n",
-    "hfi=((n*Af)+(Ao))*(hf/Ai); # eq 16.34\n",
-    "print\"\\t hf      hfi \\t \"\n",
-    "print hf      \n",
-    "print hfi\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "hf=[4, 16, 36, 100, 400, 625, 900]; # from 2nd table in the solution\n",
-    "hfi=[35.4, 110.8, 193.5, 370, 935, 1295, 1700]; # from 2nd table in the solution\n",
-    "pyplot.plot(hf,hfi)\n",
-    "pyplot.xlabel('heat transfer coefficient to fin,Btu/(ft**2)*(hr)')\n",
-    "pyplot.ylabel('coefficient hf referred to the tube ID')\n",
-    "pyplot.title('weighted fin efficiency curve')\n",
-    "pyplot.show()\t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.2 pgno:525"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t annulus flow area : ft**2 \t0.0391482454167\n",
-      "\t wetted perimeter : ft \t2.76875\n",
-      "\t equivalent diameter : ft \t0.0565572845749\n",
-      "\t heat load : Btu/hr \t270286.4\n",
-      "\t delt1 is : F \t151.0\n",
-      "\t delt2 is : F \t117.0\n",
-      "\t LMTD is  F \t133.427780969\n",
-      "\t Ui : Btu/(hr)*(ft**2)*(F) \t365.652178958\n",
-      "\t hfi : Btu/(hr)*(ft**2)*(F) \t416.40535396\n",
-      "\t jf : \t36.7135894676\n",
-      "\t Ga : lb/(hr)*(ft**2) \t388267.720257\n",
-      "\t Rea : \t11319.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Ts=302.; # F\n",
-    "t1=151.;\n",
-    "t2=185.;\n",
-    "w=15200.; # lb/hr\n",
-    "from math import log10\n",
-    "# The dropwise condensation of steam was promoted with oil.\n",
-    "aa=(3.14*(3.068**2-1.25**2))/(4*144)-((20*0.035*0.75)/(144));\n",
-    "print\"\\t annulus flow area : ft**2 \\t\",aa\n",
-    "p=(3.14*(1.25/12))-(20*0.035/12)+(20*0.75*2/12);\n",
-    "print\"\\t wetted perimeter : ft \\t\",p\n",
-    "De=(4*aa/p);\n",
-    "print\"\\t equivalent diameter : ft \\t\",De\n",
-    "Q=w*0.523*(t2-t1);\n",
-    "print\"\\t heat load : Btu/hr \\t\",Q\n",
-    "delt1=Ts-t1; #F\n",
-    "delt2=Ts-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Ai=0.277; # ft**2/ft\n",
-    "n=20; # number of fins\n",
-    "Ui=(Q/(Ai*n*LMTD));\n",
-    "print\"\\t Ui : Btu/(hr)*(ft**2)*(F) \\t\",Ui\n",
-    "hi=3000; # assumed value for dropwise condensation of steam\n",
-    "hfi=(Ui*hi)/(hi-Ui);\n",
-    "print\"\\t hfi : Btu/(hr)*(ft**2)*(F) \\t\",hfi\n",
-    "hf=120; # from fig 16.7 for hfi=418\n",
-    "mu=1.94; # lb/(ft*hr)\n",
-    "k=0.079;\n",
-    "Z=2.34; # Z=((c*mu)/k)**(1/3)\n",
-    "jf=(hf*De/(Z*k)); # eq 16.36\n",
-    "print\"\\t jf : \\t\",jf\n",
-    "Ga=(w/aa);\n",
-    "print\"\\t Ga : lb/(hr)*(ft**2) \\t\",Ga\n",
-    "Rea=(De*Ga/mu);\n",
-    "print\"\\t Rea : \\t\",round(Rea)\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.3 pgno:530"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 12,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t477000.0\n",
-      "\t total heat required for water is :  Btu/hr \t478000.0\n",
-      "\t delt1 is :  F \t120.0\n",
-      "\t delt2 is :  F \t130.0\n",
-      "\t LMTD is :%.0f F \t125.073724087\n",
-      "\t ratio of two local temperature difference is :  \t0.923076923077\n",
-      "\t caloric temperature of hot fluid is :  F \t223.5\n",
-      "\t caloric temperature of cold fluid is :  F \t98.8\n",
-      "\t hot fluid:shell side,gas oil \t\n",
-      "\t flow area is :  ft**2 \t0.0287156933333\n",
-      "\t wetted perimeter :  in \t29.126\n",
-      "\t De :  ft \t0.0473238096546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t626834.943216\n",
-      "\t reynolds number is :  \t4903.1764525\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t97.2026562015\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.01409546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t847790.707079\n",
-      "\t V is :  fps \t3.76795869813\n",
-      "\t reynolds number is :  \t65199.6985471\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t795.4\n",
-      "\t calculation of tfw \t\n",
-      "\t phya is :  \t0.953986161765\n",
-      "\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t92.729988903\n",
-      "\t Rf :  \t0.0107839978396\n",
-      "\t hf1 :  \t78.2227916919\n",
-      "\t hfi2 :  \t450.563280145\n",
-      "\t Rmetal :  \t0.00170212455807\n",
-      "\t Ri :  \t0.00125722906714\n",
-      "\t hi1 :  \t234.894572087\n",
-      "\t UDi :  \t122.267359744\n",
-      "\t Ai :  ft**2 \t31.2572870644\n",
-      "\t length of pipe required :  lin ft \t74.0694006266\n",
-      "\t Q/Ai1 :  Btu/(hr)*(ft**2) \t14158.7677725\n",
-      "\t annulus film :  \t31.4245931625\n",
-      "\t annulus dirt :  \t4.9162388099\n",
-      "\t Tc-tfw :  \t36.3408319724\n",
-      "\t fin and tube metal :  \t24.0999863376\n",
-      "\t tube side dirt :  \t42.4763033175\n",
-      "\t tubeside film :  \t17.8008143984\n",
-      "\t total temperature drop :  F \t120.717936026\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t3719.56602669\n",
-      "\t delPs is :  psi \t7.7\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t1.6\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=18000; # lb/hr\n",
-    "w=11950; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is :%.0f F \\t\",LMTD\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.47; # from fig.17\n",
-    "Kc=0.27; \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,gas oil \\t\"\n",
-    "ID=3.068; # in, table 11\n",
-    "OD=1.9; # in, table 11\n",
-    "af=0.0175; # fin cross section,table 10\n",
-    "aa=((3.14*ID**2/(4))-(3.14*OD**2/(4))-(24*af))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "p=(3.14*(OD))-(24*0.035)+(24*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*aa*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=2.5*2.42; # at 224F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jf=18.4; # from fig.16.10\n",
-    "Z=0.25; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hf=((jf)*(1/De)*(Z)); # Hf=(hf/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hf\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "D=0.134; # ft\n",
-    "row=62.5;\n",
-    "at=(3.14*D**2/(4));\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.72*2.42; # at 99F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(970*0.82); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "print\"\\t calculation of tfw \\t\"\n",
-    "# Tc-tfw=40F assumption from fig 14\n",
-    "tfw=184;\n",
-    "mufw=3.5; # cp, at 184F\n",
-    "phya=(2.5/mufw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "hf=(Hf)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.002;\n",
-    "Rf=(1/hf);\n",
-    "print\"\\t Rf :  \\t\",Rf\n",
-    "hf1=(1/(Rdo+Rf)); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=255; # fig 16.9\n",
-    "hfi2=(hf1*5.76); # eq 16.38 and fig 16.9,((Af+Ao)/(Ai))=5.76 from previous prblm\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "Rmetal=(hfi2-hfi1)/(hfi2*hfi1)# eq 16.39\n",
-    "print\"\\t Rmetal :  \\t\",Rmetal\n",
-    "phyt=1; # for cooling water\n",
-    "Rdi=0.003;\n",
-    "Ri=(1/hi);\n",
-    "print\"\\t Ri :  \\t\",Ri\n",
-    "hi1=(1/(Rdi+Ri)); # eq 16.40\n",
-    "print\"\\t hi1 :  \\t\",hi1\n",
-    "UDi=(hi1*hfi1)/(hi1+hfi1); # eq 16.41\n",
-    "print\"\\t UDi :  \\t\",UDi\n",
-    "# To obtain the true flux the heat load must be divided by the actual heat-transfer surface.For a 1}2-in. IPS pipe there are 0.422 ft2/lin foot, from table 11\n",
-    "# trial\n",
-    "Ai=(Q/(UDi*LMTD)); # LMTD=delt\n",
-    "print\"\\t Ai :  ft**2 \\t\",Ai\n",
-    "L=(Ai/0.422);\n",
-    "print\"\\t length of pipe required :  lin ft \\t\",L\n",
-    "# Use two 20-ft hairpins = 80 lin ft\n",
-    "Ai1=(80*0.422); # ft**2\n",
-    "r=(Q/Ai1);\n",
-    "print\"\\t Q/Ai1 :  Btu/(hr)*(ft**2) \\t\",r\n",
-    "deltf=(r/hfi2);\n",
-    "deltdo=(r*Rdo/5.76);\n",
-    "print\"\\t annulus film :  \\t\",deltf\n",
-    "print\"\\t annulus dirt :  \\t\",deltdo\n",
-    "d=deltf+deltdo; # d=Tc-tfw\n",
-    "deltmetal=(r*Rmetal);\n",
-    "deltdi=(r*Rdi);\n",
-    "delti=(r/hi);\n",
-    "print\"\\t Tc-tfw :  \\t\",d\n",
-    "print\"\\t fin and tube metal :  \\t\",deltmetal\n",
-    "print\"\\t tube side dirt :  \\t\",deltdi\n",
-    "print\"\\t tubeside film :  \\t\",delti\n",
-    "Td=deltf+deltdo+deltmetal+deltdi+delti;\n",
-    "print\"\\t total temperature drop :  F \\t\",Td\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0359; # ft\n",
-    "Rea1=(De1*Ga/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Rea1\n",
-    "f=0.00036; # fig 16.10\n",
-    "s=0.82; #using fig.6\n",
-    "delPs=((f*(Ga**2)*(80))/(5.22*(10**10)*(De1)*(s)*(phya))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000192; # friction factor for reynolds number 65000, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(80))/(5.22*(10**10)*(0.134)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.4 pgno:535"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 13,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for oxygwn is :  Btu/hr \t1012500.0\n",
-      "\t total heat required for water is :  Btu/hr \t1010000\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t66.8818722257\n",
-      "\t R is :  \t7\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.87 \t\n",
-      "\t delt is :  F \t58.1872288364\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t flow area is :  ft**2 \t1.46834418403\n",
-      "\t wetted perimeter :  in \t1570.8\n",
-      "\t De :  ft \t0.0448691882056\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20431.1770539\n",
-      "\t reynolds number is :  \t16820.7399724\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t20.6536497998\n",
-      "\t hf1 :  \t19.4485963081\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0582118055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t867521.622428\n",
-      "\t V is :  fps \t3.85565165523\n",
-      "\t reynolds number is :  \t29155.8813311\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t902.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t243.418213207\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t89.6828045249\n",
-      "\t total surface area is :  ft**2 \t229.376\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t75.673831631\n",
-      "\t excess fouling factor :  \t0.00206419817483\n",
-      "\t Rdo :  \t0.0221351170807\n",
-      "\t hf2 :  \t14.1738000666\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t77.1741091592\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t16232.4764484\n",
-      "\t delPs is :  psi \t0.6\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=100; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=50500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.225; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oxygwn is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.87 \\t\"# from fig 18\n",
-    "delt=(0.87*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "ID=19.25; # in, table 11\n",
-    "OD=1; # in, table 11\n",
-    "As=((3.14*ID**2/(4))-(70*3.14*OD**2/(4))-(70*20*0.035*0.5))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "p=(70*3.14*(OD))-(70*20*0.035)+(70*20*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*As*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0545; # at 175F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=59.5; # from fig.16.10a\n",
-    "k=0.0175;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "hf=((jH)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.479; # table 10\n",
-    "L=16;\n",
-    "Nt=70;\n",
-    "n=4;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0652; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.94; # at 90F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(940*0.96); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi);\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "UDi=((hfi1)*(hi1)/(hi1+hfi1)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A2=0.2048; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UDi1=((Q)/((A)*(delt)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi1\n",
-    "Re=(1/UDi1)-(1/UDi);\n",
-    "print\"\\t excess fouling factor :  \\t\",Re\n",
-    "Ro=9.27; #Adding to the outside fouling factor\n",
-    "Rdo1=Rdo+(Re*Ro);\n",
-    "print\"\\t Rdo :  \\t\",Rdo1\n",
-    "hf2=(hf/(1+(hf*Rdo1)));\n",
-    "print\"\\t hf2 :  \\t\",hf2\n",
-    "hfi2=113;\n",
-    "UDi2=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi2\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0433; # ft\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.00025; # fig 16.10\n",
-    "s=0.00133;\n",
-    "delPs=((f*(Gs**2)*(L))/(5.22*(10**10)*(De1)*(s)*(1))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00021; # friction factor for reynolds number 29100, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(0.0625)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.5 pgno:556"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for air is :  Btu/hr \t1250000.0\n",
-      "\t total heat required for water is :  Btu/hr \t1248000.0\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t60.0\n",
-      "\t LMTD is : F \t54.9097962457\n",
-      "\t R is :  \t1.25\n",
-      "\t S is :  \t0.4\n",
-      "\t FT is 0.985 \t\n",
-      "\t delt is :  F \t54.086149302\n",
-      "\t caloric temperature of hot fluid is :  F \t225.0\n",
-      "\t caloric temperature of cold fluid is :  F \t170.0\n",
-      "\t fin surface is :  in**2/lin ft \t310.86\n",
-      "\t bare tube surface is :  in**2/lin ft \t27.1296\n",
-      "\t total outside surface :  ft**2/lin ft \t337.9896\n",
-      "\t projected perimeter :  in/ft \t161.28\n",
-      "\t De :  ft \t0.111235119048\n",
-      "\t flow area :  ft**2 \t7.53\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t13280.2124834\n",
-      "\t reynolds number is :  \t28408.1926263\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.9878748896\n",
-      "\t hf1 :  \t21.5048242607\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.079625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t391836.734694\n",
-      "\t V is :  fps \t1.74149659864\n",
-      "\t reynolds number is :  \t30427.5453198\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t667.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t222.303643994\n",
-      "\t X : \t0.03125\n",
-      "\t hfi2 :  \t212.371237248\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.611980947\n",
-      "\t inside surface per bank is :  ft**2 \t18.312\n",
-      "\t Ai1 :  ft**2 \t212.447090593\n",
-      "\t number of banks :  \t11.6015230774\n",
-      "\t net free volume :  ft**3 \t1.89483559028\n",
-      "\t frictional surface :  ft**2 \t191.88\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 :  ft \t0.0395004292324\n",
-      "\t reynolds number :  \t10087.9633345\n",
-      "\t delPs is :  psi \t0.232069401484\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.39\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=150.; # inlet cold fluid,F\n",
-    "t2=190.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=31200; # lb/hr\\\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for air is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.985 \\t\" # from fig 18\n",
-    "delt=(0.985*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "Af=(3.14*2*8*12*(1.75**2-1**2))/(4);\n",
-    "Ao=((3.14*1*12)-(3.14*1*8*0.035*12));\n",
-    "print\"\\t fin surface is :  in**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  in**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "p=(2*3*2*8*12/8)+(((12)-(8*0.035*12))*(2));\n",
-    "print\"\\t projected perimeter :  in/ft \\t\",p\n",
-    "De=(2*A/(3.14*p*12)); # eq 16.104\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "# 21 tubes may be fit in one :vertical bank (Fig. 16.19b) ,20 tubes in alternating banks for triangular pitch\n",
-    "As=((4**2*12**2)-(21*1*48)-((21)*(2*0.035*3*8*48/8)))/(144); # fig 16.19\n",
-    "print\"\\t flow area :  ft**2 \\t\",As\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.052; # at 225F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jf=157; # from fig.16.18a\n",
-    "k=0.0183;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "phys=1;\n",
-    "hf=((jf)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.546; # table 10\n",
-    "L=4;\n",
-    "Nt=21;\n",
-    "n=1;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0695; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.895; # at 170F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(710*0.94); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi); # 16.40\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "k1=60; # table 3 , for brass\n",
-    "# yb=0.00146 ft\n",
-    "X=((0.875-0.5)/12)*(21.5/(60*0.00146))**(1/2);\n",
-    "print\"\\t X : \\t\",X\n",
-    "nf=0.91; # from fig 16.13a , by comparing X value\n",
-    "Ai=0.218; # ft**2/ft\n",
-    "hfi2=((nf*Af/144)+(Ao/144))*(hf1/Ai); # eq 16.34\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "UDi=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A=(21*4*Ai); # ft**2\n",
-    "print\"\\t inside surface per bank is :  ft**2 \\t\",A\n",
-    "Ai1=(Q/(UDi*delt));\n",
-    "print\"\\t Ai1 :  ft**2 \\t\",Ai1\n",
-    "Nb=(Ai1/A);\n",
-    "print\"\\t number of banks :  \\t\",Nb\n",
-    "Vn=(4*4*1.95/12)-(41*3.14*1*4/(2*4*144))-((41*3.14*0.035*8*4/(144*2*4))*(1.75**2-1**2)); # fig 16.19b\n",
-    "print\"\\t net free volume :  ft**3 \\t\",Vn\n",
-    "Af1=(41*2.34*4/2);\n",
-    "print\"\\t frictional surface :  ft**2 \\t\",Af1\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=(4*Vn/Af1); # ft\n",
-    "print\"\\t De1 :  ft \\t\",De1\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.0024; # fig 16.18b\n",
-    "s=0.000928;\n",
-    "Lp=1.95;\n",
-    "R1=0.538; # R1=(De1/ST)**(0.4)\n",
-    "R2=1; # R2=(SL/ST)**0.6\n",
-    "delPs=((f*(Gs**2)*(Lp)*(R1)*(R2))/(5.22*(10**10)*(De1)*(s)*(1)));\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 30400, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(Nb))/(5.22*(10**10)*(0.0695)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_1.ipynb
deleted file mode 100755
index 4ffc6c97..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_1.ipynb
+++ /dev/null
@@ -1,1035 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 16: Extented Surfaces"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.1 pgno: 521"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t fin surface is : %.1f ft**2/lin ft \t2.5\n",
-      "\t bare tube surface is :  ft**2/lin ft \t0.0\n",
-      "\t total outside surface :  ft**2/lin ft \t2.5\n",
-      "\t total inside surface :  ft**2/lin ft \t0.277366666667\n",
-      "\t fin efficiencies \t\n",
-      "\t hf      m      n \t \n",
-      "4\n",
-      "5.24\n",
-      "0.965717954492\n",
-      "\t weighted efficiency curve \t\n",
-      "\t hf      hfi \t \n",
-      "4\n",
-      "34.8173760783\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAZAAAAEZCAYAAAC5AHPcAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XeYXGX5xvHvnUCoEQggLZEaSpASelNCFZUmCoh0+IkQ\n",
-       "EWxIQo0iKigqomClQxQUEGwkIEGKEOmBUJUACSRgEAEbgdy/P953k5PJzO7s7M6e2d3nc1175Zwz\n",
-       "Z877zOxmnjlvlW1CCCGEzhpQdgAhhBB6p0ggIYQQGhIJJIQQQkMigYQQQmhIJJAQQggNiQQSQgih\n",
-       "IZFAQreTdJGk0+o891JJZzUxlnavL+mrkl6R9KKkYZLekKQmxLGepIckvS7peEmLS7pJ0muSrpH0\n",
-       "CUk313GdsZJ+0t3xhdCIRcoOIPQ9to/rzOn5pypJc4F1bP+t0XBqXV/Se4DPA8Nsz86HBzdYTke+\n",
-       "BNxqe9Nc9qHAu4Ehtufmc67u6CK2v96k+ELotLgDCb1BV+8Iaj3/PcDsQvJoptWBqRX7TxWSR78m\n",
-       "aWDZMYTOiwQS5pF0pKQbC/tPS7qmsP+CpI3z9vqSJkqaLekJSfsXzlug2kjSl3IV0XRJ/ydprqS1\n",
-       "CkUPkfSbXL1zT9tjkv6UH384Vy3tn4/vmauD/iHpLkkbFcoaKemBfK2fA4vXeK27AhOAVfO1L5a0\n",
-       "Ro5tQD5nkqSvSLozX+9mScu38/5VjUvSH4FRwPdzWVcDpwMH5v2jJB0h6Y7CtTYsvL8zJY3Nx8dJ\n",
-       "uqJw3jaS7s5lPiRpx8Jj7cYvaYfCc5+XdLikLXN5Kpy3n6SHarzmJSSdJ2laro67I1fPjZL0QsW5\n",
-       "0yTtXHgdv5R0haR/AqdI+rek5Sp+l6+0JZf8Pk2V9KqkP+Q7yFAm2/ETP9gGWBP4R95eFZgGPJ/3\n",
-       "1wJezdtLAS8Ah5O+hGwKvAJskB+/BPhK3t4DeAnYAFgCuBKYC6yVH78U+DuwBTAwPz6+ENO8c/P+\n",
-       "SGAWsCXpzuIw4FlgUWAQ8BxwYr7WR4G32mKp8np3BF4o7K+RyxuQ9ycBTwPrkBLRbcDXa1yrZlz5\n",
-       "8duAowrnnwlcXtg/Argjbw/O79nn8mtaGtiq8Lwr8vZq+b3bI+/vmveX7yh+0h3Q68CB+b0aAmyc\n",
-       "H3us7Zp5/3rgczVe9w+APwKr5L+FbXLMo4rvbT73WWDnvD0u/272zvuLA7cC/1c4/5vAhXl7n/xa\n",
-       "1svlnArcVfb/mf7+E3cgYR7bzwJvSBoJvB+4GXhR0nqkD9u2O4I9gWdtX2Z7ru2HgOuA/atc9gDg\n",
-       "YtuP2/4P6QNwgWKB62zfZ/sd4CpSQqrlGOBHtv/i5HLgf8C2pA+vRWyfb/sd278C/tLOtTqqGjNw\n",
-       "ie1nbP8XuKad2GrFtU2N8tRO+XsCL9r+ju23bL9pe3KVaxwC/M72HwBs3wLcB3y4jvg/AUy0/Yv8\n",
-       "Xr1q+5H82OX52kgaAuxOlfaZfKd2JHCi7Zfy38I9tt+q8boq3W37xhz7f3MZB+Vri5Tc2so9lpT8\n",
-       "nnSq9vs6sKmkYXWWFZogGtFDpdtJ3x7XyduvkZLHtnkf0rfXrSX9o/C8RUgfPJVWASYX9qdXOWdW\n",
-       "Yfs/pG/ctawOHCbpM4Vji+ZyBMyoOP85utaGMrPO2GrFtWphv96ZS4cB9XQaWB3YX9JehWOLkO4I\n",
-       "2tSKv70yrgIek7Qk6QvAn2zPqnLeCqQ7h7/WEWs1lX8L1wEXSFqZdKcx1/ad+bHVgfMlnVfxnNVI\n",
-       "d8OhBJFAQqXbgb1J1TlnkxLIIaRv0hfkc54Hbre9ex3Xe4n0YdWmq98YnwfOtv21ygdy/f9qFYdX\n",
-       "B57pYpldiquG9pLJ86Rv3/WUeYXtY+oss/K5W1UNzJ4u6R5gP9Lv/sIa1/g78F/Sl41HKh77F7Bk\n",
-       "205ux1ixsqiKcv8haQLptY8AxlfEe5bt4rFQsqjCCpVuB3YCFrf9InAnqR1jCPBgPuc3wLqSDpG0\n",
-       "aP7ZUtL6+fFi9cw1wJFKje5LkhqPizq6O5gFrF3Y/wlwrKStlCwl6cOSlgbuBt6WdEKOaT9Sm0RX\n",
-       "1Hv30l5c1a7V3nV/C6wi6URJi0kaLKnah/2VwF6Sdpc0sNB4XUyitcq5GthV0v6SFpG0vKRNCo9f\n",
-       "DpwMvJd0Z7CQXJV0MfBtSavkGLaVNAh4Clhc0ockLQqcBizWzmsuxnU4qf2qWG32Q1JD+wgAScuo\n",
-       "0HEjlCMSSFiA7aeBN4A78v7rpCqKu+zUmmn7TVK9+MdJVUYvkeqkB7VdJv+Q6+e/R2rAfQr4cz7n\n",
-       "f5XnFsMobI8DLss9hT5m+37gk8D3gVdJDauH5bLmkL41HwHMJlW//Kqjl9yJ/ZpjStqJq/L5ta5V\n",
-       "fM/eAHYD9iK9t0+RqhUrz5tOalw+BXiZ9C39CyyYNGqV8TzwoXz+bNKXg40L515H6uZ8fW6fqOWL\n",
-       "wBRSW9Ns0t+BbP8TGA38lFRV9SYLVjXVei9vJN3RvGR7yryT7RuAc4Cf515bU4APtBNX6AHKnwnd\n",
-       "f2HpYlJj3su227ozbkX6D7Yo8DYw2vZf8mNjgaOAd4ATbE/Ixzcn9dRZnNRgeGJTAg49QtIGpP/8\n",
-       "gxxjIFqapKeBT9n+Y4cnh36pmXcgl5CqPorOBU63PRI4I++Tb0vb6j33AC4s9EO/CDja9nBguKTK\n",
-       "a4YWJ+kjuSpmOdK3yBsjebS2XP3nSB6hPU1LILbvAP5RcfglYJm8vSzze8zsQ+r7P8f2NFKj59aS\n",
-       "VgEGF7owXg7s26yYQ9McQ2rLeAaYA3RmqpPQwyRNIjWcf7rkUEKL6+leWGOAOyV9i5S8ts3HVwXu\n",
-       "KZw3ndSbZg4LdvWbwcK9bEKLs/3BsmMI9bM9quwYQu/Q043oPyO1b7yHNMr24h4uP4QQQjfp6TuQ\n",
-       "rWzvmrd/SeqhAenOojg+YCjpzmNG3i4erxwoBoCk5vQGCCGEPs52Y4NtmzlPCmkw2pTC/gPAjnl7\n",
-       "F+AveXsE8BCpG+iapG6jbT3E7gW2JnVN/B2FOXoqynIzX0uDr39c2TFETH0rrogpYmpCXG70uU27\n",
-       "A5E0njQFxgp5Vs4zSI2pP5C0GGlahWNy9FOVZn2dyvzuvW13FKNJ3XiXoDDvTwghhHI1LYHYPqjG\n",
-       "Q1vXOP9rwELTQDgN0Npo4WeEEEIoU4xEb65JZQdQxaSyA6hiUtkB1DCp7ACqmFR2AFVMKjuAKiaV\n",
-       "HUAVk8oOoLs1bSR6T5NkN9oQFEII/VRXPjvjDiSEEEJDIoGEEEJoSCSQEEIIDYkEEkIIoSGRQEII\n",
-       "ITQklrQNIYR+SGI54NiuXCPuQEIIoR+RWF7iq6TlFYZ35VqRQEIIoR+QeLfEOaQlklcEtrA5qivX\n",
-       "jAQSQgh9mMQqEt8GngCWAja1+ZTNs129diSQEELogySGSnwPeIw0m/l7bY63eaG7yogEEkIIfYjE\n",
-       "6hIXAY8A/wNG2HzO5sXuLisSSAgh9AESa0v8lLTu0j+A9WxOspnZrDKjG28IIfRiEusCpwB7Aj8A\n",
-       "htu82hNlRwIJIYReSGIEcCqwO/A9YB2b13oyhqZVYUm6WNIsSVMqjn9G0uOSHpV0TuH4WElPS3pC\n",
-       "0u6F45tLmpIfO79Z8YYQQm8gsbHENcBtwBRgbZuzejp5QHPbQC4B9igekLQTsDewse33At/Kx0cA\n",
-       "B5LWRt8DuFBS2/z0FwFH2x4ODJe0wDVDCKE/kBgpcR1wM3AvsJbNN2xeLyumDhOIpGUlbZl/lqn3\n",
-       "wrbvIDXkFB0HfN32nHzOK/n4PsB423NsTyONkNxa0irAYNuT83mXA/vWG0MIIfR2EltJ3AT8Brid\n",
-       "dMdxns2/Sg6tdgKRtJikS4FpwI+BnwDPSbpE0qAGyxsOvF/SPZImSdoiH18VmF44bzqwWpXjM/Lx\n",
-       "EELo0yS2k/gD8Evg96TEcb7Nv0sObZ72GtFPAxYFhtl+A0DSYOBC4PT800h5y9neRtKWwDXAWg1c\n",
-       "pypJ4wq7k2xP6q5rhxBCT5DYkfT5ujbwNWBvm7e67/oaBYzqjmu1l0D2A7ayPe82yfYbko4j1b81\n",
-       "kkCmA9fla/1F0lxJK5DuLIYVzhuaz52Rt4vHZ9S6uO1xDcQUQgilkhCwM3AGqZblbOBKmzndXVb+\n",
-       "Yj1pftk6s9FrtdcG8k4xeRQKfxOY22B5N5DeJCStCwyy/XfgRuDjkgZJWpNU1TXZ9kzgdUlb50b1\n",
-       "Q/M1Qgih15OQxB7AXaQxHD8B1re5pBnJo7u1Ow5E0pBqhwF3dGFJ44EdgeUlvUDKrBcDF+euvW8B\n",
-       "hwHYnirpGmAq8DYw2nZbGaOBS4ElgN/Z/kMdryuEEFpWvuPYk1STsyTwVeBam3dKDayTNP9zuuIB\n",
-       "aRrtJArbazYppoZIsm11fGYIIZRDYgCp1+nppBqgs4Dr7YZrdbohpsY/O2smkN4mEkgIoVVJDAQ+\n",
-       "Skoc/wO+Atxkd1yb02xd+eysWYUlabP2nmj7gUYKDCGE/kJiEdIg6VOB14GTgd+3QuLoDu1VYU2i\n",
-       "/SqsnZoUU0PiDiSE0CokFgU+QUocs0h3HLe0YuKIKiwigYQQyicxiNQ56BTSIOyvALe3YuJo05Qq\n",
-       "rBBCCPWRWAw4ChhDWjr2MJs7y42q+SKBhBBCgySWAP6P1LbxMHCgzT3lRtVzIoGEEEInSSwFfAr4\n",
-       "IjAZ2Mfm/nKj6nn1zMY7QNKhks7I+++RtFXzQwshhNYiMVjiZOCvwLbAB2327Y/JA+pbD+RC0hv1\n",
-       "ibz/Zj4WQgj9gsQyEqeSEsemwK42+9s8XHJopaqnCmtr2yMlPQhg+1VJizY5rhBCKJ3EcsCJwPHA\n",
-       "74D32zxRblSto547kLckDWzbkbQijU+mGEIILU9iBYmzSYvbDQO2sTkskseC6kkgFwDXA++W9DXS\n",
-       "rJFfb2pUIYRQAol3S5wDPAWsAGxhc7TNMyWH1pLqGkgoaQNgl7x7q+3HmxpVA2IgYQihURKrACcB\n",
-       "RwBXA+faPF9qUD2kK5+d9dyBQJpueGA+f4lGCgohhFYjMVTiAuAx0ufbRjbH95fk0VX1dOM9g7Qe\n",
-       "xxDSLd0lkhpZjTCEEFqCxOoSFwGPAP8FRth81q694mlYWIdVWJKeAja2/d+8vwTwsO11eyC+ukUV\n",
-       "VgihIxJrA2OBjwA/Ar5j80q5UZWr2VVYM1iw2mpx0nrlHQV1saRZefXByse+kNdDH1I4NlbS05Ke\n",
-       "kLR74fjmkqbkx86vI94QQliAxLoSlwH3Ai8Cw21O6e/Jo6tqJhBJF0i6APgn8JikSyVdCjyaj3Xk\n",
-       "EmCPKtcdBuwGPFc4NoI0Z/6I/JwL8xroABcBR9seDgyXtNA1QwihGokREleReo8+A6xjc4bNqyWH\n",
-       "1ie0N5DwftJ6IPcDNxSOT6KONdFt3yFpjSoPfRv4EvDrwrF9gPG25wDTJD0DbC3pOWCw7cn5vMuB\n",
-       "fYFYFz2EUJPExsBpwI7Ad4DjbF4vN6q+p2YCsX1pdxcmaR9guu1H5t9gALAqLDCD5XRgNWAOC1aX\n",
-       "zcjHQwhhIRKbkZaN3QY4DzjK5s1yo+q7OpzKRNKzVQ7b9lqdKUjSkqRFVnYrHu7MNeooY1xhd5Lt\n",
-       "Sd15/RBCa5LYipQ4NgPOBQ62+Xe5UbUmSaOAUd1xrXrmwtqysL048DFg+QbKWhtYA3g4330MBe6X\n",
-       "tDXpzmJY4dyhpDuPGXm7eLxmNzvb4xqIK4TQS0lsB5xBaj/9BrC/zX/Ljaq15S/Wk9r2JZ3Z6LU6\n",
-       "7IVl+++Fn+m2vwt8uLMF2Z5ieyXba9pek5QgNrM9C7gR+LikQZLWBIYDk23PBF6XtHVuVD+UBdtj\n",
-       "Qgj9kMSOErcCVwHXkXpVXRjJo2fVU4W1OfMbzQcAW5BGpXf0vPGkBqzlJb0AnGH7ksIp8xribU+V\n",
-       "dA0wFXgbGO35A1RGkwYyLgH8znY0oIfQD0kI2Jl0x7EacDZwpc2cUgPrx+oZSDiJ+R/2b5MWiv+W\n",
-       "7SebGlknxUDCEPqmnDg+QEocQ4CvAj+3ebvUwPqIrnx21pNA1rL9t4pja9qu1rhemkggIfQtOXHs\n",
-       "SUocSwJnAdfavFNqYH1MsxPIA7Y3qzh2v+3NGymwWSKBhNA3SAwgjfc6jVRd/hXgejvWIWqGrnx2\n",
-       "1mwDyVO4jwCWlbQfqcutgXeRemOFEEK3kRgIfJTUHfd/wJeBmyJxtK72GtHXBfYClsn/tnkD+GQz\n",
-       "gwoh9B8Si5CmMjqNNE3SycDv7Y5nvAjlqqcKazvbd/dQPA2LKqwQeheJRYFPAKcCs0hVVbdE4uhZ\n",
-       "TW0D6S0igYTQO0gMAg4jzUwxjZQ4bo/EUY6mtIGEEEJ3klgMOAoYAzwJHG5zR7lRha6IBBJCaCqJ\n",
-       "xUntpicDDwMH2gtMnhp6qXqWtF1Z0s8k/SHvj5B0dPNDCyH0ZhIDJY4k3W3sDuxr8+FIHn1HPSsS\n",
-       "XgpMIE25DvA08LlmBRRC6N0kJLEvab3xI4GDbPayua/k0EI3qyeBrGD7F5BGf+ZFn2IKgRDCQiR2\n",
-       "BO4mjeE4CdjRpuV7cYbG1NMG8qakedO3S9qG+pa0DSH0ExKbAl8DNiANBLw6BgD2ffUkkC8ANwFr\n",
-       "SbobWJG0JkgIoZ+TWIs0R9UupNlx97V5q9yoQk+paxyIpEWB9fLuk7kaq6XEOJAQeo7ESqQ7jYOA\n",
-       "84Hv2LxRblShET0xDmQr0mqCiwCbScL25Y0UGELovSSWAb5IWqfncmB9m1fKjSqUpZ4Fpa4E1gIe\n",
-       "ggWmUY4EEkI/kcdyjCbPUwVsZvNcuVGFstVzB7I5MMKdnPNE0sWkpW9ftr1RPvZN0vz+bwF/BY60\n",
-       "/c/82FjSKNV3gBNsT8jHNyd1JV6ctCLhiZ2JI4TQuDxD7mHAONKXyF1sHi01qNAy6unG+yiwSgPX\n",
-       "vgTYo+LYBGBD25sATwFjIQ1OJM3GOSI/58K8BjrARcDRtocDwyVVXjOE0M1qjOXYJ5JHKGpvPZCb\n",
-       "8ubSwFRJk0lz9APY9t7tXdj2HZLWqDg2sbB7L2nuf4B9gPG5cX6apGeArSU9Bwy2PTmfdzlpoZlY\n",
-       "Fz2EJsljOb5BWgXwJGJq9VBDe1VY5+V/TVpMqqg7/piOAsbn7VVhgekNpgOrAXPydpsZ+XgIoZvF\n",
-       "WI7QWTUTiO1JAJLOtf2l4mOSzgFub7RQSacCb9m+utFr1LjuuMLupLbXEEKoLcZy9C+SRgGjuuNa\n",
-       "9TSi71bl2IdIvTE6TdIR+fm7FA7PAIYV9oeS7jxm5O3i8Rm1rm17XCMxhdAfVRnLcWyM5ej78hfr\n",
-       "SW37ks5s9Fo1G9ElHSdpCrCepCmFn2mkhrVOyw3gJwH72P5v4aEbgY9LGiRpTWA4MNn2TOB1SVvn\n",
-       "RvVDgRsaKTuEkEgsI3EWMJVUTby+zVcieYTOau8O5GpSf+9vkO422tpB3rA9u6MLSxoP7AisIOkF\n",
-       "4ExSr6tBwMTcyerPtkfbnirpGtIf9NvA6EK34dGkbrxLkLrxRgN6CA2IsRyhu8WStiH0cVXGcpwa\n",
-       "3XFDm1jSNoSwEAmRusifDcwmjeWIqdVDt4kEEkIfFGM5Qk+oK4FIWhnYkjT+Y7Ltl5saVQihITGW\n",
-       "I/SketZEP4A0anx/4ABgsqT9mx1YCKF+EmtJXEWapeH3wHo2V0byCM3UYSO6pEeAXdvuOiStCNxq\n",
-       "e+MeiK9u0Yge+qNYlyN0VVc+O+uZTFGwwHz/s1l4apMQQg+KsRyhFdTTBvIH4GZJV5MSx4GkW+QQ\n",
-       "Qg+LsRyhldS7pO1Hge3z7h22r29qVA2IKqzQl8VYjtAsXfnsrKcN5BzbJ3d0rGyRQEJfVGUsx5gY\n",
-       "yxG6U7MTyIO2R1Ycm9K2ymCriAQS+pqKsRxjibEcoQmaMhJd0nGkuta186SKbQYDdzVSWAihYzGW\n",
-       "I/QWNe9AJC0DLEeDkyn2tLgDCb1dlXU5fhTrcoRma2oVVm8RCST0VjGWI5Sp2eNAQghNEGM5Qm8X\n",
-       "CSSEHiaxuMTngadIK3FuZvM5e4EBuyG0vKYlEEkXS5pVbICXNETSRElPSZogadnCY2MlPS3pCUm7\n",
-       "F45vnldCfFrS+c2KN4RmkxgocSTwJGmxtV1sjoiBgKG3am9J2zclvVHj5/U6rn0JsEfFsTHARNvr\n",
-       "ArfmfSSNII1wH5Gfc2FewhbgIuBo28OB4XlZ3BB6DQlJ7EtaCvpI0roc+8RAwNDb1ezGa3tpAElf\n",
-       "BV4ErswPHQys2tGFbd8haY2Kw3uTvnkBXEZa2H0MaaDUeNtzgGmSngG2lvQcMNj25Pycy4F9SdOr\n",
-       "hNDyYl2O0JfVMxfW3hUz716UZ+g9vYHyVrI9K2/PAlbK26sC9xTOmw6sRmpYnF44PiMfD6GlxViO\n",
-       "0B/U0wbyL0mHSBqYfw4G3uxqwU79h+ObWOhTYl2O0J/UcwfyCVLf9O/m/bvysUbMkrSy7ZmSVgHa\n",
-       "VjacQeqN0mYo6c5jRt4uHp9R6+KSxhV2J9me1GCcIXRKlbEcx0Z33NCKJI0CRnXLtZo5kDC3gdzU\n",
-       "Nm+WpHOB2bbPkTQGWNb2mNyIfjWwFamK6hZgHduWdC9wAjAZ+C3wPdsLtYHEQMJQBollgC+Spv25\n",
-       "HPhadMcNvUlTBxJKWk/SrZIey/sbSzqtjueNB+4G1pP0gqQjSY2Ju0l6Ctg572N7KnANaUDV74HR\n",
-       "np/ZRgM/BZ4GnqmWPELoaTGWI4T6ZuP9E6n3yA9tj8zdax+1vWFPBFivuAMJPSHW5Qh9TVNm4y1Y\n",
-       "0va9bcMycrXSnEYKC6G3qrIux0GxLkfo7+pJIK9IWqdtR9LHgJeaF1IIrSXGcoRQXT1VWGsDPwa2\n",
-       "BV4DngUOtj2t6dF1QlRhhe4WYzlCf9C0KixJA4HjbO8iaWlggO16pjEJodeSWBn4JrAbqcpq31iX\n",
-       "I4SFtdsLy/Y7wA5KKerNSB6hL5MYIPEpYAppvNFwmwsieYRQXT1tIA8Bv5Z0LfDvfMy2r2teWCH0\n",
-       "LIkNgR+RvlTtbDOlg6eE0O/Vk0AWI/U62bnieCSQ0OtJLAGcBhwDnEFaRjbaOUKoQz1tIK/a/kIP\n",
-       "xRNCj5HYlbRcwIPAJjYvlhxSCL1KuwnE9juSts9tINFtMfQJEisC3wbeBxxv85uSQwqhV4o2kNBv\n",
-       "5MGAR5DGdFwBvNfu+szSIfRX9SSQxYFXiTaQ0ItJrEdqJF8K2MPmwZJDCqHXa+psvD0pBhKGaiQW\n",
-       "I616+RngLOD7Nu+UG1UIraMlZ+MNoWx5CpKHgc2AkTbnR/IIofvUsyLhT4BTYN5gqimkRXNCaEkS\n",
-       "QyR+BlwJjLXZx+aFsuMKoa+pJ4Esafvetp3cGytm4w0tR0ISh5DWlfkXsKHN9SWHFUKfFbPxhj5B\n",
-       "Ym3SmI53A3vbTC45pBD6vHruQI4n9V5ZT9KLwOeA47pSqKSxkh6TNEXS1ZIWkzRE0kRJT0maIGnZ\n",
-       "ivOflvSEpN27UnboWyQGSYwF7gUmAltG8gihZ9RMIJJOzJur2N6F9M1ufdvbd2Uq97xO+ieBzfJa\n",
-       "6QOBj5N6yky0vS5wa94nr5d+IDAC2AO4UFI9iS/0cRLbAfeTBgRuYfNNO6pXQ+gp7X0QH5X/vQCg\n",
-       "G2fjfZ3UhrKkpEVIi/S8COwNXJbPuQzYN2/vA4y3PScnrmeArbohjtBLSSwrcRHwS1LX3A/bTCs3\n",
-       "qhD6n/baQKZKehpYTVLlzKS2vXEjBdp+VdJ5wPPAf4CbbU+UtJLtWfm0WcBKeXtV4J7CJaYDqzVS\n",
-       "dujd8kjy/YHvADcBI2xeKzeqEPqvmgnE9kGSVgYmAHsB3TJIL69w+FlgDeCfwLWSDqko25LaG+HY\n",
-       "N0Y/hrpJrAH8gPR3c4DNXaUGFELocDLFmcDGkpYA3mP7yW4ocwvgbtuzASRdR1oud6aklW3PlLQK\n",
-       "8HI+fwYwrPD8ofnYQiSNK+xOsj2pG+INJZJYhPSFYwxpAsSPxAJPITRO0ihgVLdcq4410fcmLe+5\n",
-       "mO01JI0Evmx774YKlDYBrgK2BP4LXApMBlYHZts+R9IYYFnbY3Ij+tWkdo/VgFuAdSpnB46pTPoe\n",
-       "iS2BH5PWoznW5pmSQwqhz2namujZOGBr4DYA2w9KWquRwvLzH5Z0OXAfMBd4gPQhMRi4RtLRwDTg\n",
-       "gHz+VEnXkAaHvQ2Mjqnl+zaJwaS1yA8AvghcZUe1ZQitpp47kHttby3pQdsj87FHGm1Eb5a4A+kb\n",
-       "JPYl9fybCJxkM7vkkELo05p9B/KYpIOBRSQNB04A7m6ksBBqkRhKShwjgENtJpUbUQihI/WORN8Q\n",
-       "+B8wnjSO47PNDCr0HxIDJU4gLVz2MLBxJI8Qeod2q7DyQL+JtnfquZAaE1VYvY/ESFL7179IjeRP\n",
-       "lBxSCP1O09YDsf02MLc4L1UIXSWxlMS3gJtJEyDuFMkjhN6nnjaQfwFTJE3M25DG+p3QvLBCXyXx\n",
-       "IeBC4E7SmuQvd/CUEEKLqieBXJd/2uq6RIwED50ksQpwPml1wE/aTCw5pBBCF8Wa6KGpJAYAx5Am\n",
-       "Pfwx8FWb/5QbVQihTbO78YbQEIn3kpKGSe0cj5YcUgihG8W6GqHbSSwh8TXS7AWXAe+L5BFC39Pe\n",
-       "glJX5H9jzEeom8RuwBRgbdKYjh/ZzC05rBBCE9RsA5E0FdgV+ANVZm60/WpTI+ukaAMpl8S7SbPl\n",
-       "7gCMtvldySGFEOrQrDaQH5KWll2LtGxokfPx0M/lRZ6OAr5Oqq7a0J7X3TuE0IfVM5niD20f20Px\n",
-       "NCzuQHqexPrAj4AlgGNsHio5pBBCJ3Xls7OubrySBpKWmJ13x2L7+UYKbJZIID1HYnFgLPBp4MvA\n",
-       "hTbvlBtVCKERTe3GK+kzwJmkFQKLHxIbNVJg6N0kRpHuOqYCm9pMLzeiEEJZ6qnC+iuwVdsStK0q\n",
-       "7kCaS2J50sqUuwGfsbmh5JBCCN2gaZMpZs+TpnDvNpKWlfRLSY9Lmippa0lDJE2U9JSkCcUJHCWN\n",
-       "lfS0pCck7d6dsYT2SUjiUOAx4A1gRCSPEAK03433C3lzBLA+8BvgrXzMtr/dcKHSZcDtti/OU8Yv\n",
-       "BZwK/N32uZJOBparWBN9S+avib6u7bkV14w7kG4msQ6pN97ypEbyv5QcUgihmzXrDmQwsDTpDmQi\n",
-       "MCjvL50KByWiAAAY60lEQVQfa4ikZYD32b4Y0pTxtv8J7E3qBkr+d9+8vQ8w3vYc29OAZ4CtGi0/\n",
-       "dExikMSpwD3A74EtI3mEECrVbES3Pa5JZa4JvCLpEmAT0hiTzwIr2Z6Vz5lF6vUFsCrpg6zNdNKd\n",
-       "SGgCie1JjeTPAVvYTCs3ohBCqypjMsVFSFN6H2/7L5K+C4wpnmDbktpr3a/6mKRxhd1Jtid1MdZ+\n",
-       "Q2I54BvAnqSE/ks7pu0Poa+RNIoqs4s0oowEMh2YbrutSuSXpDEFMyWtbHumpFVg3kJDM4BhhecP\n",
-       "zccW0sS7pj4rjyQ/APgOcANpJPlr5UYVQmiW/MV6Utu+pDMbvVaHvbAk7VDl2PaNFmh7JvCCpHXz\n",
-       "oV1JPXxuAg7Pxw6HeT19bgQ+LmmQpDWB4cDkRssP80msCfwOOA34qM3oSB4hhHrVMw7kQdsjOzrW\n",
-       "qUKlTYCfkhrm/wocCQwErgHeA0wDDrD9Wj7/FNJ8S28DJ9q+uco1oxdWnSQWJVVTnQycB3zLZk65\n",
-       "UYUQytCUqUwkbQtsB3yONMtqWwGDgY/Y3qSRApslEkh9JLYiLfL0MnCczV9LDimEUKJmTWUyiJQs\n",
-       "BrJgt93XgY81Ulgoj8S7gLNJv7svAldHI3kIoSvqqcJaI4+/aGlxB1JdbiT/CPA90touX7JpqbVc\n",
-       "Qgjlafaa6ItJ+gmwRuF82965kQJDz5EYBnwfWA/4hM2fSg4phNCH1JNArgUuIjV6t83GG1UfLUxi\n",
-       "IHA8cDpwAXCAzf/KjSqE0NfUk0Dm2L6o6ZGEbiGxGamR/A1ge5snSw4phNBH1TMb702SPi1plTxj\n",
-       "7hBJQ5oeWegUiaUlziPNXfV9YOdIHiGEZqqnEX0aVaqsbK/ZpJga0p8b0SX2BH4A3A58weaVkkMK\n",
-       "IfQSTV/StjfojwlEYlXgfGAkcKzNLSWHFELoZZq6oJSkpSSdnntiIWm4pD0bKSx0D4kBEqOBh4En\n",
-       "gY0ieYQQelo9jeiXkKZc3y7vv0iaAPE3zQoq1CaxEamRfC4wyuaxkkMKIfRT9TSir237HPJqhLb/\n",
-       "1dyQQjUSS0p8A/gjKam/L5JHCKFM9SSQ/0laom1H0toQYwp6ksQHgCmkwZwb2fzYZm77zwohhOaq\n",
-       "pwprHGkKjKGSrga2B45oYkwhk1iJtE7HtsBom9+XHFIIIcxTVy8sSSsA2+Tde2z/valRNaAv9cKS\n",
-       "GECavv5rwKXAl22i6jCE0O2aNZ37BrYfl7Q5aRxIWwEGsP1AIwU2S19JIBIbkNYkXww4xubhkkMK\n",
-       "IfRhzUogP7H9SUmTqD6QcKdGCmyW3p5AJBYHTgFGk6oNL7LnzT0WQghN0SsHEkoaCNxHWh99rzw9\n",
-       "yi+A1Vl4RcKxpCqdd4ATbE+ocr1em0AkdiLddTwKfMauvuZ7CCF0t2YPJPy0pOUK+8tJGt1IYRVO\n",
-       "BKYy/+5mDDDR9rrArXkfSSOAA4ERwB7AhZLq6T3W8iRWkLgUuAw4yWa/SB4hhN6ing/iY2z/o20n\n",
-       "bx/TlUIlDQU+RJoivi3z7U36ICX/u2/e3gcYb3tOXtjqGWCrrpRfNglJHEa643gN2NDm1yWHFUII\n",
-       "nVJPN94BkgbYngvzqp4W7WK53wFOAt5VOLaS7Vl5exawUt5eFbincN50YLUull8aieHAD4HlgD1t\n",
-       "7is5pBBCaEg9CeRm4OeSfkS6W/gUaVxIQ/I8Wi/bflDSqGrn2Lak9hpnqj4maVxhd5LtSY3G2d0k\n",
-       "BgFfAj5LWpv8Apu3y40qhNDf5M/dUd1xrXoSyMmkKqvj8v5EUtVTo7YD9pb0IWBx4F2SrgBmSVrZ\n",
-       "9kxJqwAv5/NnAMMKzx+ajy3E9rguxNU0EjuQ5q/6K7C5zXMlhxRC6KfyF+tJbfuSzmz0WqVO5y5p\n",
-       "R+CLuRfWucBs2+dIGgMsa3tMbkS/mtTusRpwC7COKwJvxV5YEssB5wAfJnUa+JUdywGHEFpHVz47\n",
-       "a96BSLrW9v6SHmXhKiPb3riRAqtou/Y3gGskHU3uxpsLmirpGlKPrbeB0ZXJoxVJfBD4GXA9MMLm\n",
-       "nyWHFEII3aq9gYSr2n5R0urM7yk1T+4R1TJa6Q4k97A6F9jf5o6y4wkhhFqaNRL9AdubSbrC9qFd\n",
-       "irAHtEoCkfg8qaH8AzaPlx1PCCG0pylVWMBikg4Gtpe0Hwvehdj2dY0U2FdJiNS76iPADjbPlxxS\n",
-       "CCE0VXsJ5FjgYGAZYK8qj0cCySQGAhcBm5IWemq52YpDCKG7tZdAVrZ9bK7K+nGPRdTL5EkQryIl\n",
-       "2l1s3ig5pBBC6BHtTWVySv73uHbO6dckBgO/Ja1P/uFIHiGE/qS9O5DZkiYCa0q6qeIx2967iXG1\n",
-       "PIkVgd+TZhT+dEy9HkLob9pLIB8CNgOuBL5FRSN6M4NqdRLvIY3IvxY4PQYHhhD6ow5Hokta0fYr\n",
-       "kpay3bLLqvZUN16JEaS5wL5t891mlxdCCM3U1PVAgOGSpgJP5MI2lXRhI4X1dhJbA38ETo3kEULo\n",
-       "7+pJIN8lLeT0dwDbDwE7NjOoViSxO/Ab4GibK8qOJ4QQylbXyn62KwfF9atpyCUOBK4APmLz27Lj\n",
-       "CSGEVlDPdO7PS9oeQNIg4AToP1N0SIwGTgV2s3mk7HhCCKFV1NWIDpwP7ErqiTUBOMH27OaHV7/u\n",
-       "bkTPU5OcDhwG7G7zt+66dgghtIqmTKbY23RnApEYQEqa7wP2sJnZHdcNIYRW09ReWJKGSbpe0iv5\n",
-       "51eShjZSWG+Ql569EtgEGBXJI4QQqqunEf0S4EZg1fxzUz7W50gsBfwaWJo0HftrJYcUQggtq54E\n",
-       "sqLtS2zPyT+XAu9utMB8R3ObpMckPSrphHx8iKSJkp6SNEHSsoXnjJX0tKQnJO3eaNntx8UQ0ujy\n",
-       "WcB+Nv9pRjkhhNBX1JNAZks6VNJASYtIOgS6NF35HOBztjcEtgE+LWkDYAww0fa6wK15n7wm+oHA\n",
-       "CNJ4lAsl1dX9uF4SqwF/Au4GjrL7VzflEEJoRD0fxEeR1iefCbwE7A8c2WiBtmfmwYjYfpPUJXg1\n",
-       "YG/gsnzaZcC+eXsfYHy++5kGPANs1Wj5lSSGA3eSxnmcZDO3u64dQgh9WYfjQPKHdrUFpbpM0hrA\n",
-       "SOBeYCXbs/JDs4CV8vaqwD2Fp00nJZxuKJ/NSKPLz7D5aXdcM4QQ+osOE4iky0njPl7L+8sB59k+\n",
-       "qisFS1oa+BVwou03pPm9yGxbUnv9i6s+JmlcYXeS7Um1y2dz0nTsx9qxumIIoX+QNAoY1R3Xqmck\n",
-       "+sZtyQPA9j8kbdaVQiUtSkoeV9i+IR+eJWll2zMlrQK8nI/PAIYVnj40H1uI7XH1lc9g4BfAZyJ5\n",
-       "hBD6k/zFelLbvqQzG71WPW0gkjSksDMEGNhogUq3Gj8Dptouzmh7I3B43j4cuKFw/OOSBklaExgO\n",
-       "TG60/OwHwG02v+jidUIIod+q5w7kPODPkq4hTWWyP3B2F8rcHjgEeETSg/nYWOAbwDWSjgamkRru\n",
-       "sT01lz2VNInjaHdh+LzEocCWwBYNv4IQQgj1TWUiaUNgZ1Lbwx9tT212YJ1Vz3B8iXWAPwO72jzc\n",
-       "M5GFEELrirmw6PhNyFOU3AlcYXNBz0UWQgitq9krEvYVZ5G6B3+/7EBCCKEvqKcNpNfLqwkeDIy0\n",
-       "q3cBDiGE0Dl9PoFIvJs0+eNhNq+UHU8IIfQVfboKK6/rcSlwmc2tJYcTQgh9Sp9OIMBngCFAwwNl\n",
-       "QgghVNdne2FJLAP8FdjO5qnyIgshhNYVvbCqOw74QySPEEJojj55ByKxJPA30oDBR8uNLIQQWlfc\n",
-       "gSzsaOCeSB4hhNA8fe4OJI84fwb4mN3lSRdDCKFPizuQBR0MPBnJI4QQmqtPDSSUGEhaS/3YsmMJ\n",
-       "IYS+rq/dgewHvEphsZQQQgjN0dcSyKnA2THfVQghNF+vSSCS9pD0hKSnJZ1c47T/Ar/tybhCCKG/\n",
-       "6hUJRNJA0jTsewAjgIMkbVDl1O1a6e4jL17fUiKm+rViXBFTfSKmntErEgiwFfCM7Wm25wA/B/ap\n",
-       "PMlmbo9H1r5RZQdQxaiyA6hiVNkB1DCq7ACqGFV2AFWMKjuAKkaVHUAVo8oOoLv1lgSyGvBCYX96\n",
-       "PhZCCKEkvSWBtEy1VAghhKRXjESXtA0wzvYeeX8sMNf2OYVzWv+FhBBCC2p0JHpvSSCLAE8CuwAv\n",
-       "ApOBg2w/XmpgIYTQj/WKkei235Z0PHAzMBD4WSSPEEIoV6+4AwkhhNB6eksjek11DjBsRrkXS5ol\n",
-       "aUrh2BBJEyU9JWmCpGULj43NMT4hafcmxTRM0m2SHpP0qKQTWiSuxSXdK+khSVMlfb0V4srlDJT0\n",
-       "oKSbWiEmSdMkPZJjmtwiMS0r6ZeSHs+/v63LjEnSevn9afv5p6QTyn6fCuU8JmmKpKslLVZ2XJJO\n",
-       "zPE8KunEfKx7YrLda39I1VnPAGsAiwIPARv0UNnvA0YCUwrHzgW+lLdPBr6Rt0fk2BbNsT4DDGhC\n",
-       "TCsDm+btpUntRhuUHVcua8n87yLAPcAOLRLX54GrgBtb5Hf4LDCk4ljZMV0GHFX4/S1TdkyF2AYA\n",
-       "LwHDyo4pX/tvwGJ5/xfA4WXGBbwXmAIsTvq8nAis3V0xNeWX2lM/wLbAHwr7Y4AxPVj+GiyYQJ4A\n",
-       "VsrbKwNP5O2xwMmF8/4AbNMD8d0A7NpKcQFLAn8BNiw7LmAocAuwE3BTK/wOSQlk+YpjpcVEShZ/\n",
-       "q3K8Jf6mgN2BO1ohJmAI6UvbcqREexOwW8m/v48BPy3snwZ8qbti6u1VWK02wHAl27Py9ixgpby9\n",
-       "Kim2Nk2PU9IapDuke1shLkkDJD2Uy7/N9mMtENd3gJNggRkMyo7JwC2S7pP0yRaIaU3gFUmXSHpA\n",
-       "0k8kLVVyTEUfB8bn7VJjsv0qcB7wPKm36Gu2J5Yc16PA+3KV1ZLAh0hfnLolpt6eQFq2B4BT+m4v\n",
-       "vqbFLmlp4FfAibbfaIW4bM+1vSnpj/f9knYqMy5JewIv234QqNoHvqT3anvbI4EPAp+W9L6SY1oE\n",
-       "2Ay40PZmwL9Id/plxgSApEHAXsC1CxVYQkyS1gY+S6qZWBVYWtIhZcZl+wngHGAC8HtS9dQ73RVT\n",
-       "b08gM0h1n22GsWD27GmzJK0MIGkV4OV8vDLOoflYt5O0KCl5XGH7hlaJq43tf5JmTN685Li2A/aW\n",
-       "9CzpG+zOkq4oOSZsv5T/fQW4njQPXJkxTQem2/5L3v8lKaHMbIG/qQ8C9+f3Csr/O98CuNv2bNtv\n",
-       "A9eRqtlLfa9sX2x7C9s7Av8AnqKb3qvenkDuA4ZLWiN/GzkQuLHEeG4kNZqR/72hcPzjkgZJWhMY\n",
-       "Dt2/5K4kAT8Dptr+bgvFtUJbLw9JS5DqhR8sMy7bp9geZntNUjXIH20fWmZMkpaUNDhvL0Wq359S\n",
-       "Zky2ZwIvSFo3H9oVeIxUv1/a31R2EPOrr9rKLjOmJ4BtJC2R/y/uCkyl5PdK0rvzv+8hLbp3Nd31\n",
-       "XnV3Q1JP/5C+hTxJ6i0wtgfLHU+q53yL1A5zJKkR7RZShp8ALFs4/5Qc4xPAB5oU0w6k+vyHSB/Q\n",
-       "D5KmwC87ro2AB3JcjwAn5eOlxlUoa0fm98IqLSZSe8ND+efRtr/nst8nYBNSx4eHSd+ql2mBmJYC\n",
-       "/g4MLhwr/e+J1ED9GCnxX0bqzVT2e/WnHNNDwE7d+V7FQMIQQggN6e1VWCGEEEoSCSSEEEJDIoGE\n",
-       "EEJoSCSQEEIIDYkEEkIIoSGRQEIIITQkEkgLywMkp3R8Zl3X2lHStp19rDtJWl9pSvf7Ja3V7PI6\n",
-       "iOUEpanJr8iDpm7Jcz0dkOd72qCd5+6lBpcOkLSMpOM6+1gH1yy+lk7HJukdpWnR23432+bjq0s6\n",
-       "qBPXGSPpE3n7eElH5O0Ffu/VrinpzPaOSdotzw/2SP53p8Jjt7YNwKx1PaVp1W9XmpNtlPL0/XW8\n",
-       "pm9XTicT5otxIC1MaULEm2xv1A3XGge8Yfu8Tj420PY7lccbjGEMMND22Z14zgDbczs+s9OxPA7s\n",
-       "YvtFSdsAZ9nerbvLqVLuGtT4nTb6+y6+lgZjesN22wj43YFTbI+SNAr4gu296rzOH4H9gVdJA0e3\n",
-       "dFpNdN7vvfKaks4mTfi5G2kQ7MXAAVWOCZhpe6akDYGbbQ/N1/gkaUDhtyUdDKwCLJ/jeNH2VZKO\n",
-       "Is1y/M16X5ekAaSpz8+zvXc970G/06wRmfHTLSNI1yBNhfBj0sjkm4HF82NrkyZHu4800nS9fHwv\n",
-       "0nobD5Dm/n93vs5LpHmNHgR2qCij7bEHSKPZLwV+mK/zLWBL4O78+F3Auvm5R5BGJv+eNKL1nHx8\n",
-       "YL7GFNLI88+SZgxoK+fWfN4hpA+KB3N5A/LxN3O5DwHbVbwn65BG0D4E3A+smY9/s1DeAYXzTyJN\n",
-       "xfAwMC4f+yHwv3zul4Cngdfy61sLmARsns/dI5fzEDCx8LovyNsrkuaHmpx/tsvHx5E++G4D/gp8\n",
-       "Jh//OfDv/JrPqXhtCz1W63UVnlN8LZ+tiO1S4Pz8O/sr8NEaf2dvFLb3B67L2/fk9+XBfO3D266d\n",
-       "H/8NsGPefhdwZ97eARiftz9U+L3/Efhz4Zon5nMuIn3YDy9ce6FjhccEzAYWzfsrAZMLjx8EvF3x\n",
-       "dzCR+X+3o/Lv5VrgceDKwnnTgG/k3/kB+dgjFEZqx0/hd1F2APHTzi8nfbjPATbO+78ADs7btwLr\n",
-       "5O2tmf+hXJyS4P+Ab+XtM4HP1yhngceAS0hz4rTdoQ4mfYOENL/PL/P2EfmDaTCwWP7PN5Q0UeKE\n",
-       "wvXeVVkOaaGrGwvXvRA4NG/PBT5WI9Z7gX3y9iBgCeCjpOkYREqYz5HWONgd+FE+dwDpA+99ef9Z\n",
-       "8sJNpKlMbiqUcRtpwsAVSVNzr158byl8kJLmFdo+b7+HNA8ZpARyJ2kqi+VJ024MBFansIZMxWtb\n",
-       "4LFar6vK84qvpRjbpcAvCu/30zXKfZv0gf446cN9ZI33pTKB3AS8P2/vx/wEPYYF/56Kv/fKa54F\n",
-       "7A18j5TsNq52rCLej1H4+8rH/kZaRO0g4IvA10lfHg7K7/tLhXNH5de5an5v72Z+4n8W+GLFtS8D\n",
-       "Plj250Er/ixCaHXP2n4kb98PrJEn2tsOuDbN2QakD1OAYZKuIX2ADiL9x2pTddryGo9d6/y/B1gW\n",
-       "uFzSOqSpnYt/N7c6TxkvaSr5QxRYS9L3SDPvTqhSzi6kRHNffg1LADPzY++QZhReMMBUz72q7V8D\n",
-       "2H4rH98euDrH+7Kk20l3TTsCu0t6MF9iKdIdzB0dvPa2Y9sAf7L9XC7vtSrn7QpsUPg9DM6/HwO/\n",
-       "tT0HmC3pZdI35c78Dmq9rrrq73MMN+TYH5e0Uo3z/uM0hTy5Ou8K0kp27cVaaQ/SRJ6Q/gburHhc\n",
-       "Ff+S4zo9lzvS9pfz4UeqHCMf25B0h1BZ3TgLGGZ7fD7vTNvfzNsrAW9UnD/ZucpPaZ2aNUiJBNIX\n",
-       "taIX8+OhQiSQ1ve/wvY7pKUpBwD/aPtPX+EC0l3HbyTtSPom3Ih/F7bPIiWKj0hanVTFUyu+RWy/\n",
-       "JmkT4APAsaQ67aOrlHGZ7VOqHP9vIXnVq9aH3ddt/7iT12pTTwwCtm5LZvMOpoRSPPYOjf1/q3xd\n",
-       "nX1fijF0mBBs36M0e/IKVR5+mwU73ixe2N4S+FRnyqoo98sdHZM0lFRleqjtZytOF4WFwapcrzKe\n",
-       "hf5uC/v/qvLcaCyuInph9T7K3/iflfQxSNO4S9o4P/4u0jcmSFVMbd4gVTVV095jldc8sqP4JC1P\n",
-       "qpq6DjidVB0EC/4nvhX4mKQV85OGKE03XVN+3dMl7ZOfs5jS9PB3AAfmHjYrAu8nVXXdDByV7wiQ\n",
-       "tFpbeXUwqQ3g/blxG0lDqryOCcAJhRe/SQfX7czvodrr6mi677o+uCU9UeP4+qTPhdlV4pkGbJr/\n",
-       "3oaR1ippuyt4opD026oQq+nob61WvMuS7mZPtv3nKqesRO21gP5Oqt5q1Cqk1x4qRAJpfZXffNr2\n",
-       "DwaOzrffj5LqjCHdcVwr6T7glcL5NwEfyd01t6+4ZttjD0jaoUq55wJfl/QAqT7ZhXOqxbcacFuu\n",
-       "OrqC+SvYzTvf9uOk9ZknSHqY9EG8cuG8Wg4FTsjPuYu0NOf1pGqPh0mJ6STbLzstJ3o18GdJj5Aa\n",
-       "Tat9kFR7Hdj+O3AMcF1+n8dXOf8EYAtJD0t6jAW/hVe75mzgLklTJJ3T3mO1XleN+Gu9loW2q9xd\n",
-       "LJH/Lh4kNeQfnpPBw8A7Sl1wT7R9F6mNYCqpbeJ+UsL6IKkjRZs7SYsrVYtxgWtWeS21HE/qOHJm\n",
-       "W6yFLx8rA7NtV945pIJTL8JHJa1XiKUzdxQjSY3/oUJ04w2hn5H0YVLvte930/UmkKqVZuV9kXq0\n",
-       "LVS11wySjgGWsv2dds45gvRl45xa59R43rqkKuHoxltFJJAQQreTNJrUOH9JD5R1K6ln3pvtnDOI\n",
-       "1P17x860r0n6Nqlbc2WngEAkkBBCCA2KNpAQQggNiQQSQgihIZFAQgghNCQSSAghhIZEAgkhhNCQ\n",
-       "SCAhhBAa8v/Onrp6J+51IAAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaadcc88>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "from math import tanh\n",
-    "Af=(20*0.75*12*2)/(144);\n",
-    "Ao=((3.14*1.25)-(20*0.035))*(12/144);\n",
-    "print\"\\t fin surface is : %.1f ft**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  ft**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "Ai=(3.14*1.06*12)/(144);\n",
-    "print\"\\t total inside surface :  ft**2/lin ft \\t\",Ai\n",
-    "print\"\\t fin efficiencies \\t\"\n",
-    "b=0.0625; # ft\n",
-    "hf=4; # from table in solution\n",
-    "m=(5.24*(hf**(1/2))); # m=((hf*P)/(Kax))**(1/2), eq 16.8\n",
-    "n=(tanh(m*b))/(m*b); # efficiency , eq 16.26\n",
-    "print\"\\t hf      m      n \\t \"\n",
-    "print hf   \n",
-    "print m      \n",
-    "print n\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "print\"\\t weighted efficiency curve \\t\"\n",
-    "hfi=((n*Af)+(Ao))*(hf/Ai); # eq 16.34\n",
-    "print\"\\t hf      hfi \\t \"\n",
-    "print hf      \n",
-    "print hfi\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "hf=[4, 16, 36, 100, 400, 625, 900]; # from 2nd table in the solution\n",
-    "hfi=[35.4, 110.8, 193.5, 370, 935, 1295, 1700]; # from 2nd table in the solution\n",
-    "pyplot.plot(hf,hfi)\n",
-    "pyplot.xlabel('heat transfer coefficient to fin,Btu/(ft**2)*(hr)')\n",
-    "pyplot.ylabel('coefficient hf referred to the tube ID')\n",
-    "pyplot.title('weighted fin efficiency curve')\n",
-    "pyplot.show()\t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.2 pgno:525"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t annulus flow area : ft**2 \t0.0391482454167\n",
-      "\t wetted perimeter : ft \t2.76875\n",
-      "\t equivalent diameter : ft \t0.0565572845749\n",
-      "\t heat load : Btu/hr \t270286.4\n",
-      "\t delt1 is : F \t151.0\n",
-      "\t delt2 is : F \t117.0\n",
-      "\t LMTD is  F \t133.427780969\n",
-      "\t Ui : Btu/(hr)*(ft**2)*(F) \t365.652178958\n",
-      "\t hfi : Btu/(hr)*(ft**2)*(F) \t416.40535396\n",
-      "\t jf : \t36.7135894676\n",
-      "\t Ga : lb/(hr)*(ft**2) \t388267.720257\n",
-      "\t Rea : \t11319.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Ts=302.; # F\n",
-    "t1=151.;\n",
-    "t2=185.;\n",
-    "w=15200.; # lb/hr\n",
-    "from math import log10\n",
-    "# The dropwise condensation of steam was promoted with oil.\n",
-    "aa=(3.14*(3.068**2-1.25**2))/(4*144)-((20*0.035*0.75)/(144));\n",
-    "print\"\\t annulus flow area : ft**2 \\t\",aa\n",
-    "p=(3.14*(1.25/12))-(20*0.035/12)+(20*0.75*2/12);\n",
-    "print\"\\t wetted perimeter : ft \\t\",p\n",
-    "De=(4*aa/p);\n",
-    "print\"\\t equivalent diameter : ft \\t\",De\n",
-    "Q=w*0.523*(t2-t1);\n",
-    "print\"\\t heat load : Btu/hr \\t\",Q\n",
-    "delt1=Ts-t1; #F\n",
-    "delt2=Ts-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Ai=0.277; # ft**2/ft\n",
-    "n=20; # number of fins\n",
-    "Ui=(Q/(Ai*n*LMTD));\n",
-    "print\"\\t Ui : Btu/(hr)*(ft**2)*(F) \\t\",Ui\n",
-    "hi=3000; # assumed value for dropwise condensation of steam\n",
-    "hfi=(Ui*hi)/(hi-Ui);\n",
-    "print\"\\t hfi : Btu/(hr)*(ft**2)*(F) \\t\",hfi\n",
-    "hf=120; # from fig 16.7 for hfi=418\n",
-    "mu=1.94; # lb/(ft*hr)\n",
-    "k=0.079;\n",
-    "Z=2.34; # Z=((c*mu)/k)**(1/3)\n",
-    "jf=(hf*De/(Z*k)); # eq 16.36\n",
-    "print\"\\t jf : \\t\",jf\n",
-    "Ga=(w/aa);\n",
-    "print\"\\t Ga : lb/(hr)*(ft**2) \\t\",Ga\n",
-    "Rea=(De*Ga/mu);\n",
-    "print\"\\t Rea : \\t\",round(Rea)\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.3 pgno:530"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 12,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t477000.0\n",
-      "\t total heat required for water is :  Btu/hr \t478000.0\n",
-      "\t delt1 is :  F \t120.0\n",
-      "\t delt2 is :  F \t130.0\n",
-      "\t LMTD is :%.0f F \t125.073724087\n",
-      "\t ratio of two local temperature difference is :  \t0.923076923077\n",
-      "\t caloric temperature of hot fluid is :  F \t223.5\n",
-      "\t caloric temperature of cold fluid is :  F \t98.8\n",
-      "\t hot fluid:shell side,gas oil \t\n",
-      "\t flow area is :  ft**2 \t0.0287156933333\n",
-      "\t wetted perimeter :  in \t29.126\n",
-      "\t De :  ft \t0.0473238096546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t626834.943216\n",
-      "\t reynolds number is :  \t4903.1764525\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t97.2026562015\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.01409546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t847790.707079\n",
-      "\t V is :  fps \t3.76795869813\n",
-      "\t reynolds number is :  \t65199.6985471\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t795.4\n",
-      "\t calculation of tfw \t\n",
-      "\t phya is :  \t0.953986161765\n",
-      "\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t92.729988903\n",
-      "\t Rf :  \t0.0107839978396\n",
-      "\t hf1 :  \t78.2227916919\n",
-      "\t hfi2 :  \t450.563280145\n",
-      "\t Rmetal :  \t0.00170212455807\n",
-      "\t Ri :  \t0.00125722906714\n",
-      "\t hi1 :  \t234.894572087\n",
-      "\t UDi :  \t122.267359744\n",
-      "\t Ai :  ft**2 \t31.2572870644\n",
-      "\t length of pipe required :  lin ft \t74.0694006266\n",
-      "\t Q/Ai1 :  Btu/(hr)*(ft**2) \t14158.7677725\n",
-      "\t annulus film :  \t31.4245931625\n",
-      "\t annulus dirt :  \t4.9162388099\n",
-      "\t Tc-tfw :  \t36.3408319724\n",
-      "\t fin and tube metal :  \t24.0999863376\n",
-      "\t tube side dirt :  \t42.4763033175\n",
-      "\t tubeside film :  \t17.8008143984\n",
-      "\t total temperature drop :  F \t120.717936026\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t3719.56602669\n",
-      "\t delPs is :  psi \t7.7\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t1.6\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=18000; # lb/hr\n",
-    "w=11950; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is :%.0f F \\t\",LMTD\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.47; # from fig.17\n",
-    "Kc=0.27; \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,gas oil \\t\"\n",
-    "ID=3.068; # in, table 11\n",
-    "OD=1.9; # in, table 11\n",
-    "af=0.0175; # fin cross section,table 10\n",
-    "aa=((3.14*ID**2/(4))-(3.14*OD**2/(4))-(24*af))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "p=(3.14*(OD))-(24*0.035)+(24*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*aa*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=2.5*2.42; # at 224F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jf=18.4; # from fig.16.10\n",
-    "Z=0.25; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hf=((jf)*(1/De)*(Z)); # Hf=(hf/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hf\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "D=0.134; # ft\n",
-    "row=62.5;\n",
-    "at=(3.14*D**2/(4));\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.72*2.42; # at 99F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(970*0.82); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "print\"\\t calculation of tfw \\t\"\n",
-    "# Tc-tfw=40F assumption from fig 14\n",
-    "tfw=184;\n",
-    "mufw=3.5; # cp, at 184F\n",
-    "phya=(2.5/mufw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "hf=(Hf)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.002;\n",
-    "Rf=(1/hf);\n",
-    "print\"\\t Rf :  \\t\",Rf\n",
-    "hf1=(1/(Rdo+Rf)); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=255; # fig 16.9\n",
-    "hfi2=(hf1*5.76); # eq 16.38 and fig 16.9,((Af+Ao)/(Ai))=5.76 from previous prblm\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "Rmetal=(hfi2-hfi1)/(hfi2*hfi1)# eq 16.39\n",
-    "print\"\\t Rmetal :  \\t\",Rmetal\n",
-    "phyt=1; # for cooling water\n",
-    "Rdi=0.003;\n",
-    "Ri=(1/hi);\n",
-    "print\"\\t Ri :  \\t\",Ri\n",
-    "hi1=(1/(Rdi+Ri)); # eq 16.40\n",
-    "print\"\\t hi1 :  \\t\",hi1\n",
-    "UDi=(hi1*hfi1)/(hi1+hfi1); # eq 16.41\n",
-    "print\"\\t UDi :  \\t\",UDi\n",
-    "# To obtain the true flux the heat load must be divided by the actual heat-transfer surface.For a 1}2-in. IPS pipe there are 0.422 ft2/lin foot, from table 11\n",
-    "# trial\n",
-    "Ai=(Q/(UDi*LMTD)); # LMTD=delt\n",
-    "print\"\\t Ai :  ft**2 \\t\",Ai\n",
-    "L=(Ai/0.422);\n",
-    "print\"\\t length of pipe required :  lin ft \\t\",L\n",
-    "# Use two 20-ft hairpins = 80 lin ft\n",
-    "Ai1=(80*0.422); # ft**2\n",
-    "r=(Q/Ai1);\n",
-    "print\"\\t Q/Ai1 :  Btu/(hr)*(ft**2) \\t\",r\n",
-    "deltf=(r/hfi2);\n",
-    "deltdo=(r*Rdo/5.76);\n",
-    "print\"\\t annulus film :  \\t\",deltf\n",
-    "print\"\\t annulus dirt :  \\t\",deltdo\n",
-    "d=deltf+deltdo; # d=Tc-tfw\n",
-    "deltmetal=(r*Rmetal);\n",
-    "deltdi=(r*Rdi);\n",
-    "delti=(r/hi);\n",
-    "print\"\\t Tc-tfw :  \\t\",d\n",
-    "print\"\\t fin and tube metal :  \\t\",deltmetal\n",
-    "print\"\\t tube side dirt :  \\t\",deltdi\n",
-    "print\"\\t tubeside film :  \\t\",delti\n",
-    "Td=deltf+deltdo+deltmetal+deltdi+delti;\n",
-    "print\"\\t total temperature drop :  F \\t\",Td\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0359; # ft\n",
-    "Rea1=(De1*Ga/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Rea1\n",
-    "f=0.00036; # fig 16.10\n",
-    "s=0.82; #using fig.6\n",
-    "delPs=((f*(Ga**2)*(80))/(5.22*(10**10)*(De1)*(s)*(phya))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000192; # friction factor for reynolds number 65000, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(80))/(5.22*(10**10)*(0.134)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.4 pgno:535"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 13,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for oxygwn is :  Btu/hr \t1012500.0\n",
-      "\t total heat required for water is :  Btu/hr \t1010000\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t66.8818722257\n",
-      "\t R is :  \t7\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.87 \t\n",
-      "\t delt is :  F \t58.1872288364\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t flow area is :  ft**2 \t1.46834418403\n",
-      "\t wetted perimeter :  in \t1570.8\n",
-      "\t De :  ft \t0.0448691882056\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20431.1770539\n",
-      "\t reynolds number is :  \t16820.7399724\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t20.6536497998\n",
-      "\t hf1 :  \t19.4485963081\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0582118055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t867521.622428\n",
-      "\t V is :  fps \t3.85565165523\n",
-      "\t reynolds number is :  \t29155.8813311\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t902.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t243.418213207\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t89.6828045249\n",
-      "\t total surface area is :  ft**2 \t229.376\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t75.673831631\n",
-      "\t excess fouling factor :  \t0.00206419817483\n",
-      "\t Rdo :  \t0.0221351170807\n",
-      "\t hf2 :  \t14.1738000666\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t77.1741091592\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t16232.4764484\n",
-      "\t delPs is :  psi \t0.6\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=100; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=50500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.225; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oxygwn is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.87 \\t\"# from fig 18\n",
-    "delt=(0.87*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "ID=19.25; # in, table 11\n",
-    "OD=1; # in, table 11\n",
-    "As=((3.14*ID**2/(4))-(70*3.14*OD**2/(4))-(70*20*0.035*0.5))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "p=(70*3.14*(OD))-(70*20*0.035)+(70*20*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*As*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0545; # at 175F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=59.5; # from fig.16.10a\n",
-    "k=0.0175;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "hf=((jH)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.479; # table 10\n",
-    "L=16;\n",
-    "Nt=70;\n",
-    "n=4;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0652; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.94; # at 90F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(940*0.96); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi);\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "UDi=((hfi1)*(hi1)/(hi1+hfi1)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A2=0.2048; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UDi1=((Q)/((A)*(delt)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi1\n",
-    "Re=(1/UDi1)-(1/UDi);\n",
-    "print\"\\t excess fouling factor :  \\t\",Re\n",
-    "Ro=9.27; #Adding to the outside fouling factor\n",
-    "Rdo1=Rdo+(Re*Ro);\n",
-    "print\"\\t Rdo :  \\t\",Rdo1\n",
-    "hf2=(hf/(1+(hf*Rdo1)));\n",
-    "print\"\\t hf2 :  \\t\",hf2\n",
-    "hfi2=113;\n",
-    "UDi2=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi2\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0433; # ft\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.00025; # fig 16.10\n",
-    "s=0.00133;\n",
-    "delPs=((f*(Gs**2)*(L))/(5.22*(10**10)*(De1)*(s)*(1))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00021; # friction factor for reynolds number 29100, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(0.0625)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.5 pgno:556"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for air is :  Btu/hr \t1250000.0\n",
-      "\t total heat required for water is :  Btu/hr \t1248000.0\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t60.0\n",
-      "\t LMTD is : F \t54.9097962457\n",
-      "\t R is :  \t1.25\n",
-      "\t S is :  \t0.4\n",
-      "\t FT is 0.985 \t\n",
-      "\t delt is :  F \t54.086149302\n",
-      "\t caloric temperature of hot fluid is :  F \t225.0\n",
-      "\t caloric temperature of cold fluid is :  F \t170.0\n",
-      "\t fin surface is :  in**2/lin ft \t310.86\n",
-      "\t bare tube surface is :  in**2/lin ft \t27.1296\n",
-      "\t total outside surface :  ft**2/lin ft \t337.9896\n",
-      "\t projected perimeter :  in/ft \t161.28\n",
-      "\t De :  ft \t0.111235119048\n",
-      "\t flow area :  ft**2 \t7.53\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t13280.2124834\n",
-      "\t reynolds number is :  \t28408.1926263\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.9878748896\n",
-      "\t hf1 :  \t21.5048242607\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.079625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t391836.734694\n",
-      "\t V is :  fps \t1.74149659864\n",
-      "\t reynolds number is :  \t30427.5453198\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t667.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t222.303643994\n",
-      "\t X : \t0.03125\n",
-      "\t hfi2 :  \t212.371237248\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.611980947\n",
-      "\t inside surface per bank is :  ft**2 \t18.312\n",
-      "\t Ai1 :  ft**2 \t212.447090593\n",
-      "\t number of banks :  \t11.6015230774\n",
-      "\t net free volume :  ft**3 \t1.89483559028\n",
-      "\t frictional surface :  ft**2 \t191.88\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 :  ft \t0.0395004292324\n",
-      "\t reynolds number :  \t10087.9633345\n",
-      "\t delPs is :  psi \t0.232069401484\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.39\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=150.; # inlet cold fluid,F\n",
-    "t2=190.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=31200; # lb/hr\\\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for air is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.985 \\t\" # from fig 18\n",
-    "delt=(0.985*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "Af=(3.14*2*8*12*(1.75**2-1**2))/(4);\n",
-    "Ao=((3.14*1*12)-(3.14*1*8*0.035*12));\n",
-    "print\"\\t fin surface is :  in**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  in**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "p=(2*3*2*8*12/8)+(((12)-(8*0.035*12))*(2));\n",
-    "print\"\\t projected perimeter :  in/ft \\t\",p\n",
-    "De=(2*A/(3.14*p*12)); # eq 16.104\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "# 21 tubes may be fit in one :vertical bank (Fig. 16.19b) ,20 tubes in alternating banks for triangular pitch\n",
-    "As=((4**2*12**2)-(21*1*48)-((21)*(2*0.035*3*8*48/8)))/(144); # fig 16.19\n",
-    "print\"\\t flow area :  ft**2 \\t\",As\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.052; # at 225F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jf=157; # from fig.16.18a\n",
-    "k=0.0183;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "phys=1;\n",
-    "hf=((jf)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.546; # table 10\n",
-    "L=4;\n",
-    "Nt=21;\n",
-    "n=1;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0695; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.895; # at 170F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(710*0.94); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi); # 16.40\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "k1=60; # table 3 , for brass\n",
-    "# yb=0.00146 ft\n",
-    "X=((0.875-0.5)/12)*(21.5/(60*0.00146))**(1/2);\n",
-    "print\"\\t X : \\t\",X\n",
-    "nf=0.91; # from fig 16.13a , by comparing X value\n",
-    "Ai=0.218; # ft**2/ft\n",
-    "hfi2=((nf*Af/144)+(Ao/144))*(hf1/Ai); # eq 16.34\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "UDi=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A=(21*4*Ai); # ft**2\n",
-    "print\"\\t inside surface per bank is :  ft**2 \\t\",A\n",
-    "Ai1=(Q/(UDi*delt));\n",
-    "print\"\\t Ai1 :  ft**2 \\t\",Ai1\n",
-    "Nb=(Ai1/A);\n",
-    "print\"\\t number of banks :  \\t\",Nb\n",
-    "Vn=(4*4*1.95/12)-(41*3.14*1*4/(2*4*144))-((41*3.14*0.035*8*4/(144*2*4))*(1.75**2-1**2)); # fig 16.19b\n",
-    "print\"\\t net free volume :  ft**3 \\t\",Vn\n",
-    "Af1=(41*2.34*4/2);\n",
-    "print\"\\t frictional surface :  ft**2 \\t\",Af1\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=(4*Vn/Af1); # ft\n",
-    "print\"\\t De1 :  ft \\t\",De1\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.0024; # fig 16.18b\n",
-    "s=0.000928;\n",
-    "Lp=1.95;\n",
-    "R1=0.538; # R1=(De1/ST)**(0.4)\n",
-    "R2=1; # R2=(SL/ST)**0.6\n",
-    "delPs=((f*(Gs**2)*(Lp)*(R1)*(R2))/(5.22*(10**10)*(De1)*(s)*(1)));\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 30400, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(Nb))/(5.22*(10**10)*(0.0695)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_2.ipynb
deleted file mode 100755
index 4ffc6c97..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_2.ipynb
+++ /dev/null
@@ -1,1035 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 16: Extented Surfaces"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.1 pgno: 521"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t fin surface is : %.1f ft**2/lin ft \t2.5\n",
-      "\t bare tube surface is :  ft**2/lin ft \t0.0\n",
-      "\t total outside surface :  ft**2/lin ft \t2.5\n",
-      "\t total inside surface :  ft**2/lin ft \t0.277366666667\n",
-      "\t fin efficiencies \t\n",
-      "\t hf      m      n \t \n",
-      "4\n",
-      "5.24\n",
-      "0.965717954492\n",
-      "\t weighted efficiency curve \t\n",
-      "\t hf      hfi \t \n",
-      "4\n",
-      "34.8173760783\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAZAAAAEZCAYAAAC5AHPcAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XeYXGX5xvHvnUCoEQggLZEaSpASelNCFZUmCoh0+IkQ\n",
-       "EWxIQo0iKigqomClQxQUEGwkIEGKEOmBUJUACSRgEAEbgdy/P953k5PJzO7s7M6e2d3nc1175Zwz\n",
-       "Z877zOxmnjlvlW1CCCGEzhpQdgAhhBB6p0ggIYQQGhIJJIQQQkMigYQQQmhIJJAQQggNiQQSQgih\n",
-       "IZFAQreTdJGk0+o891JJZzUxlnavL+mrkl6R9KKkYZLekKQmxLGepIckvS7peEmLS7pJ0muSrpH0\n",
-       "CUk313GdsZJ+0t3xhdCIRcoOIPQ9to/rzOn5pypJc4F1bP+t0XBqXV/Se4DPA8Nsz86HBzdYTke+\n",
-       "BNxqe9Nc9qHAu4Ehtufmc67u6CK2v96k+ELotLgDCb1BV+8Iaj3/PcDsQvJoptWBqRX7TxWSR78m\n",
-       "aWDZMYTOiwQS5pF0pKQbC/tPS7qmsP+CpI3z9vqSJkqaLekJSfsXzlug2kjSl3IV0XRJ/ydprqS1\n",
-       "CkUPkfSbXL1zT9tjkv6UH384Vy3tn4/vmauD/iHpLkkbFcoaKemBfK2fA4vXeK27AhOAVfO1L5a0\n",
-       "Ro5tQD5nkqSvSLozX+9mScu38/5VjUvSH4FRwPdzWVcDpwMH5v2jJB0h6Y7CtTYsvL8zJY3Nx8dJ\n",
-       "uqJw3jaS7s5lPiRpx8Jj7cYvaYfCc5+XdLikLXN5Kpy3n6SHarzmJSSdJ2laro67I1fPjZL0QsW5\n",
-       "0yTtXHgdv5R0haR/AqdI+rek5Sp+l6+0JZf8Pk2V9KqkP+Q7yFAm2/ETP9gGWBP4R95eFZgGPJ/3\n",
-       "1wJezdtLAS8Ah5O+hGwKvAJskB+/BPhK3t4DeAnYAFgCuBKYC6yVH78U+DuwBTAwPz6+ENO8c/P+\n",
-       "SGAWsCXpzuIw4FlgUWAQ8BxwYr7WR4G32mKp8np3BF4o7K+RyxuQ9ycBTwPrkBLRbcDXa1yrZlz5\n",
-       "8duAowrnnwlcXtg/Argjbw/O79nn8mtaGtiq8Lwr8vZq+b3bI+/vmveX7yh+0h3Q68CB+b0aAmyc\n",
-       "H3us7Zp5/3rgczVe9w+APwKr5L+FbXLMo4rvbT73WWDnvD0u/272zvuLA7cC/1c4/5vAhXl7n/xa\n",
-       "1svlnArcVfb/mf7+E3cgYR7bzwJvSBoJvB+4GXhR0nqkD9u2O4I9gWdtX2Z7ru2HgOuA/atc9gDg\n",
-       "YtuP2/4P6QNwgWKB62zfZ/sd4CpSQqrlGOBHtv/i5HLgf8C2pA+vRWyfb/sd278C/tLOtTqqGjNw\n",
-       "ie1nbP8XuKad2GrFtU2N8tRO+XsCL9r+ju23bL9pe3KVaxwC/M72HwBs3wLcB3y4jvg/AUy0/Yv8\n",
-       "Xr1q+5H82OX52kgaAuxOlfaZfKd2JHCi7Zfy38I9tt+q8boq3W37xhz7f3MZB+Vri5Tc2so9lpT8\n",
-       "nnSq9vs6sKmkYXWWFZogGtFDpdtJ3x7XyduvkZLHtnkf0rfXrSX9o/C8RUgfPJVWASYX9qdXOWdW\n",
-       "Yfs/pG/ctawOHCbpM4Vji+ZyBMyoOP85utaGMrPO2GrFtWphv96ZS4cB9XQaWB3YX9JehWOLkO4I\n",
-       "2tSKv70yrgIek7Qk6QvAn2zPqnLeCqQ7h7/WEWs1lX8L1wEXSFqZdKcx1/ad+bHVgfMlnVfxnNVI\n",
-       "d8OhBJFAQqXbgb1J1TlnkxLIIaRv0hfkc54Hbre9ex3Xe4n0YdWmq98YnwfOtv21ygdy/f9qFYdX\n",
-       "B57pYpldiquG9pLJ86Rv3/WUeYXtY+oss/K5W1UNzJ4u6R5gP9Lv/sIa1/g78F/Sl41HKh77F7Bk\n",
-       "205ux1ixsqiKcv8haQLptY8AxlfEe5bt4rFQsqjCCpVuB3YCFrf9InAnqR1jCPBgPuc3wLqSDpG0\n",
-       "aP7ZUtL6+fFi9cw1wJFKje5LkhqPizq6O5gFrF3Y/wlwrKStlCwl6cOSlgbuBt6WdEKOaT9Sm0RX\n",
-       "1Hv30l5c1a7V3nV/C6wi6URJi0kaLKnah/2VwF6Sdpc0sNB4XUyitcq5GthV0v6SFpG0vKRNCo9f\n",
-       "DpwMvJd0Z7CQXJV0MfBtSavkGLaVNAh4Clhc0ockLQqcBizWzmsuxnU4qf2qWG32Q1JD+wgAScuo\n",
-       "0HEjlCMSSFiA7aeBN4A78v7rpCqKu+zUmmn7TVK9+MdJVUYvkeqkB7VdJv+Q6+e/R2rAfQr4cz7n\n",
-       "f5XnFsMobI8DLss9hT5m+37gk8D3gVdJDauH5bLmkL41HwHMJlW//Kqjl9yJ/ZpjStqJq/L5ta5V\n",
-       "fM/eAHYD9iK9t0+RqhUrz5tOalw+BXiZ9C39CyyYNGqV8TzwoXz+bNKXg40L515H6uZ8fW6fqOWL\n",
-       "wBRSW9Ns0t+BbP8TGA38lFRV9SYLVjXVei9vJN3RvGR7yryT7RuAc4Cf515bU4APtBNX6AHKnwnd\n",
-       "f2HpYlJj3su227ozbkX6D7Yo8DYw2vZf8mNjgaOAd4ATbE/Ixzcn9dRZnNRgeGJTAg49QtIGpP/8\n",
-       "gxxjIFqapKeBT9n+Y4cnh36pmXcgl5CqPorOBU63PRI4I++Tb0vb6j33AC4s9EO/CDja9nBguKTK\n",
-       "a4YWJ+kjuSpmOdK3yBsjebS2XP3nSB6hPU1LILbvAP5RcfglYJm8vSzze8zsQ+r7P8f2NFKj59aS\n",
-       "VgEGF7owXg7s26yYQ9McQ2rLeAaYA3RmqpPQwyRNIjWcf7rkUEKL6+leWGOAOyV9i5S8ts3HVwXu\n",
-       "KZw3ndSbZg4LdvWbwcK9bEKLs/3BsmMI9bM9quwYQu/Q043oPyO1b7yHNMr24h4uP4QQQjfp6TuQ\n",
-       "rWzvmrd/SeqhAenOojg+YCjpzmNG3i4erxwoBoCk5vQGCCGEPs52Y4NtmzlPCmkw2pTC/gPAjnl7\n",
-       "F+AveXsE8BCpG+iapG6jbT3E7gW2JnVN/B2FOXoqynIzX0uDr39c2TFETH0rrogpYmpCXG70uU27\n",
-       "A5E0njQFxgp5Vs4zSI2pP5C0GGlahWNy9FOVZn2dyvzuvW13FKNJ3XiXoDDvTwghhHI1LYHYPqjG\n",
-       "Q1vXOP9rwELTQDgN0Npo4WeEEEIoU4xEb65JZQdQxaSyA6hiUtkB1DCp7ACqmFR2AFVMKjuAKiaV\n",
-       "HUAVk8oOoLs1bSR6T5NkN9oQFEII/VRXPjvjDiSEEEJDIoGEEEJoSCSQEEIIDYkEEkIIoSGRQEII\n",
-       "ITQklrQNIYR+SGI54NiuXCPuQEIIoR+RWF7iq6TlFYZ35VqRQEIIoR+QeLfEOaQlklcEtrA5qivX\n",
-       "jAQSQgh9mMQqEt8GngCWAja1+ZTNs129diSQEELogySGSnwPeIw0m/l7bY63eaG7yogEEkIIfYjE\n",
-       "6hIXAY8A/wNG2HzO5sXuLisSSAgh9AESa0v8lLTu0j+A9WxOspnZrDKjG28IIfRiEusCpwB7Aj8A\n",
-       "htu82hNlRwIJIYReSGIEcCqwO/A9YB2b13oyhqZVYUm6WNIsSVMqjn9G0uOSHpV0TuH4WElPS3pC\n",
-       "0u6F45tLmpIfO79Z8YYQQm8gsbHENcBtwBRgbZuzejp5QHPbQC4B9igekLQTsDewse33At/Kx0cA\n",
-       "B5LWRt8DuFBS2/z0FwFH2x4ODJe0wDVDCKE/kBgpcR1wM3AvsJbNN2xeLyumDhOIpGUlbZl/lqn3\n",
-       "wrbvIDXkFB0HfN32nHzOK/n4PsB423NsTyONkNxa0irAYNuT83mXA/vWG0MIIfR2EltJ3AT8Brid\n",
-       "dMdxns2/Sg6tdgKRtJikS4FpwI+BnwDPSbpE0qAGyxsOvF/SPZImSdoiH18VmF44bzqwWpXjM/Lx\n",
-       "EELo0yS2k/gD8Evg96TEcb7Nv0sObZ72GtFPAxYFhtl+A0DSYOBC4PT800h5y9neRtKWwDXAWg1c\n",
-       "pypJ4wq7k2xP6q5rhxBCT5DYkfT5ujbwNWBvm7e67/oaBYzqjmu1l0D2A7ayPe82yfYbko4j1b81\n",
-       "kkCmA9fla/1F0lxJK5DuLIYVzhuaz52Rt4vHZ9S6uO1xDcQUQgilkhCwM3AGqZblbOBKmzndXVb+\n",
-       "Yj1pftk6s9FrtdcG8k4xeRQKfxOY22B5N5DeJCStCwyy/XfgRuDjkgZJWpNU1TXZ9kzgdUlb50b1\n",
-       "Q/M1Qgih15OQxB7AXaQxHD8B1re5pBnJo7u1Ow5E0pBqhwF3dGFJ44EdgeUlvUDKrBcDF+euvW8B\n",
-       "hwHYnirpGmAq8DYw2nZbGaOBS4ElgN/Z/kMdryuEEFpWvuPYk1STsyTwVeBam3dKDayTNP9zuuIB\n",
-       "aRrtJArbazYppoZIsm11fGYIIZRDYgCp1+nppBqgs4Dr7YZrdbohpsY/O2smkN4mEkgIoVVJDAQ+\n",
-       "Skoc/wO+Atxkd1yb02xd+eysWYUlabP2nmj7gUYKDCGE/kJiEdIg6VOB14GTgd+3QuLoDu1VYU2i\n",
-       "/SqsnZoUU0PiDiSE0CokFgU+QUocs0h3HLe0YuKIKiwigYQQyicxiNQ56BTSIOyvALe3YuJo05Qq\n",
-       "rBBCCPWRWAw4ChhDWjr2MJs7y42q+SKBhBBCgySWAP6P1LbxMHCgzT3lRtVzIoGEEEInSSwFfAr4\n",
-       "IjAZ2Mfm/nKj6nn1zMY7QNKhks7I+++RtFXzQwshhNYiMVjiZOCvwLbAB2327Y/JA+pbD+RC0hv1\n",
-       "ibz/Zj4WQgj9gsQyEqeSEsemwK42+9s8XHJopaqnCmtr2yMlPQhg+1VJizY5rhBCKJ3EcsCJwPHA\n",
-       "74D32zxRblSto547kLckDWzbkbQijU+mGEIILU9iBYmzSYvbDQO2sTkskseC6kkgFwDXA++W9DXS\n",
-       "rJFfb2pUIYRQAol3S5wDPAWsAGxhc7TNMyWH1pLqGkgoaQNgl7x7q+3HmxpVA2IgYQihURKrACcB\n",
-       "RwBXA+faPF9qUD2kK5+d9dyBQJpueGA+f4lGCgohhFYjMVTiAuAx0ufbRjbH95fk0VX1dOM9g7Qe\n",
-       "xxDSLd0lkhpZjTCEEFqCxOoSFwGPAP8FRth81q694mlYWIdVWJKeAja2/d+8vwTwsO11eyC+ukUV\n",
-       "VgihIxJrA2OBjwA/Ar5j80q5UZWr2VVYM1iw2mpx0nrlHQV1saRZefXByse+kNdDH1I4NlbS05Ke\n",
-       "kLR74fjmkqbkx86vI94QQliAxLoSlwH3Ai8Cw21O6e/Jo6tqJhBJF0i6APgn8JikSyVdCjyaj3Xk\n",
-       "EmCPKtcdBuwGPFc4NoI0Z/6I/JwL8xroABcBR9seDgyXtNA1QwihGokREleReo8+A6xjc4bNqyWH\n",
-       "1ie0N5DwftJ6IPcDNxSOT6KONdFt3yFpjSoPfRv4EvDrwrF9gPG25wDTJD0DbC3pOWCw7cn5vMuB\n",
-       "fYFYFz2EUJPExsBpwI7Ad4DjbF4vN6q+p2YCsX1pdxcmaR9guu1H5t9gALAqLDCD5XRgNWAOC1aX\n",
-       "zcjHQwhhIRKbkZaN3QY4DzjK5s1yo+q7OpzKRNKzVQ7b9lqdKUjSkqRFVnYrHu7MNeooY1xhd5Lt\n",
-       "Sd15/RBCa5LYipQ4NgPOBQ62+Xe5UbUmSaOAUd1xrXrmwtqysL048DFg+QbKWhtYA3g4330MBe6X\n",
-       "tDXpzmJY4dyhpDuPGXm7eLxmNzvb4xqIK4TQS0lsB5xBaj/9BrC/zX/Ljaq15S/Wk9r2JZ3Z6LU6\n",
-       "7IVl+++Fn+m2vwt8uLMF2Z5ieyXba9pek5QgNrM9C7gR+LikQZLWBIYDk23PBF6XtHVuVD+UBdtj\n",
-       "Qgj9kMSOErcCVwHXkXpVXRjJo2fVU4W1OfMbzQcAW5BGpXf0vPGkBqzlJb0AnGH7ksIp8xribU+V\n",
-       "dA0wFXgbGO35A1RGkwYyLgH8znY0oIfQD0kI2Jl0x7EacDZwpc2cUgPrx+oZSDiJ+R/2b5MWiv+W\n",
-       "7SebGlknxUDCEPqmnDg+QEocQ4CvAj+3ebvUwPqIrnx21pNA1rL9t4pja9qu1rhemkggIfQtOXHs\n",
-       "SUocSwJnAdfavFNqYH1MsxPIA7Y3qzh2v+3NGymwWSKBhNA3SAwgjfc6jVRd/hXgejvWIWqGrnx2\n",
-       "1mwDyVO4jwCWlbQfqcutgXeRemOFEEK3kRgIfJTUHfd/wJeBmyJxtK72GtHXBfYClsn/tnkD+GQz\n",
-       "gwoh9B8Si5CmMjqNNE3SycDv7Y5nvAjlqqcKazvbd/dQPA2LKqwQeheJRYFPAKcCs0hVVbdE4uhZ\n",
-       "TW0D6S0igYTQO0gMAg4jzUwxjZQ4bo/EUY6mtIGEEEJ3klgMOAoYAzwJHG5zR7lRha6IBBJCaCqJ\n",
-       "xUntpicDDwMH2gtMnhp6qXqWtF1Z0s8k/SHvj5B0dPNDCyH0ZhIDJY4k3W3sDuxr8+FIHn1HPSsS\n",
-       "XgpMIE25DvA08LlmBRRC6N0kJLEvab3xI4GDbPayua/k0EI3qyeBrGD7F5BGf+ZFn2IKgRDCQiR2\n",
-       "BO4mjeE4CdjRpuV7cYbG1NMG8qakedO3S9qG+pa0DSH0ExKbAl8DNiANBLw6BgD2ffUkkC8ANwFr\n",
-       "SbobWJG0JkgIoZ+TWIs0R9UupNlx97V5q9yoQk+paxyIpEWB9fLuk7kaq6XEOJAQeo7ESqQ7jYOA\n",
-       "84Hv2LxRblShET0xDmQr0mqCiwCbScL25Y0UGELovSSWAb5IWqfncmB9m1fKjSqUpZ4Fpa4E1gIe\n",
-       "ggWmUY4EEkI/kcdyjCbPUwVsZvNcuVGFstVzB7I5MMKdnPNE0sWkpW9ftr1RPvZN0vz+bwF/BY60\n",
-       "/c/82FjSKNV3gBNsT8jHNyd1JV6ctCLhiZ2JI4TQuDxD7mHAONKXyF1sHi01qNAy6unG+yiwSgPX\n",
-       "vgTYo+LYBGBD25sATwFjIQ1OJM3GOSI/58K8BjrARcDRtocDwyVVXjOE0M1qjOXYJ5JHKGpvPZCb\n",
-       "8ubSwFRJk0lz9APY9t7tXdj2HZLWqDg2sbB7L2nuf4B9gPG5cX6apGeArSU9Bwy2PTmfdzlpoZlY\n",
-       "Fz2EJsljOb5BWgXwJGJq9VBDe1VY5+V/TVpMqqg7/piOAsbn7VVhgekNpgOrAXPydpsZ+XgIoZvF\n",
-       "WI7QWTUTiO1JAJLOtf2l4mOSzgFub7RQSacCb9m+utFr1LjuuMLupLbXEEKoLcZy9C+SRgGjuuNa\n",
-       "9TSi71bl2IdIvTE6TdIR+fm7FA7PAIYV9oeS7jxm5O3i8Rm1rm17XCMxhdAfVRnLcWyM5ej78hfr\n",
-       "SW37ks5s9Fo1G9ElHSdpCrCepCmFn2mkhrVOyw3gJwH72P5v4aEbgY9LGiRpTWA4MNn2TOB1SVvn\n",
-       "RvVDgRsaKTuEkEgsI3EWMJVUTby+zVcieYTOau8O5GpSf+9vkO422tpB3rA9u6MLSxoP7AisIOkF\n",
-       "4ExSr6tBwMTcyerPtkfbnirpGtIf9NvA6EK34dGkbrxLkLrxRgN6CA2IsRyhu8WStiH0cVXGcpwa\n",
-       "3XFDm1jSNoSwEAmRusifDcwmjeWIqdVDt4kEEkIfFGM5Qk+oK4FIWhnYkjT+Y7Ltl5saVQihITGW\n",
-       "I/SketZEP4A0anx/4ABgsqT9mx1YCKF+EmtJXEWapeH3wHo2V0byCM3UYSO6pEeAXdvuOiStCNxq\n",
-       "e+MeiK9u0Yge+qNYlyN0VVc+O+uZTFGwwHz/s1l4apMQQg+KsRyhFdTTBvIH4GZJV5MSx4GkW+QQ\n",
-       "Qg+LsRyhldS7pO1Hge3z7h22r29qVA2IKqzQl8VYjtAsXfnsrKcN5BzbJ3d0rGyRQEJfVGUsx5gY\n",
-       "yxG6U7MTyIO2R1Ycm9K2ymCriAQS+pqKsRxjibEcoQmaMhJd0nGkuta186SKbQYDdzVSWAihYzGW\n",
-       "I/QWNe9AJC0DLEeDkyn2tLgDCb1dlXU5fhTrcoRma2oVVm8RCST0VjGWI5Sp2eNAQghNEGM5Qm8X\n",
-       "CSSEHiaxuMTngadIK3FuZvM5e4EBuyG0vKYlEEkXS5pVbICXNETSRElPSZogadnCY2MlPS3pCUm7\n",
-       "F45vnldCfFrS+c2KN4RmkxgocSTwJGmxtV1sjoiBgKG3am9J2zclvVHj5/U6rn0JsEfFsTHARNvr\n",
-       "ArfmfSSNII1wH5Gfc2FewhbgIuBo28OB4XlZ3BB6DQlJ7EtaCvpI0roc+8RAwNDb1ezGa3tpAElf\n",
-       "BV4ErswPHQys2tGFbd8haY2Kw3uTvnkBXEZa2H0MaaDUeNtzgGmSngG2lvQcMNj25Pycy4F9SdOr\n",
-       "hNDyYl2O0JfVMxfW3hUz716UZ+g9vYHyVrI9K2/PAlbK26sC9xTOmw6sRmpYnF44PiMfD6GlxViO\n",
-       "0B/U0wbyL0mHSBqYfw4G3uxqwU79h+ObWOhTYl2O0J/UcwfyCVLf9O/m/bvysUbMkrSy7ZmSVgHa\n",
-       "VjacQeqN0mYo6c5jRt4uHp9R6+KSxhV2J9me1GCcIXRKlbEcx0Z33NCKJI0CRnXLtZo5kDC3gdzU\n",
-       "Nm+WpHOB2bbPkTQGWNb2mNyIfjWwFamK6hZgHduWdC9wAjAZ+C3wPdsLtYHEQMJQBollgC+Spv25\n",
-       "HPhadMcNvUlTBxJKWk/SrZIey/sbSzqtjueNB+4G1pP0gqQjSY2Ju0l6Ctg572N7KnANaUDV74HR\n",
-       "np/ZRgM/BZ4GnqmWPELoaTGWI4T6ZuP9E6n3yA9tj8zdax+1vWFPBFivuAMJPSHW5Qh9TVNm4y1Y\n",
-       "0va9bcMycrXSnEYKC6G3qrIux0GxLkfo7+pJIK9IWqdtR9LHgJeaF1IIrSXGcoRQXT1VWGsDPwa2\n",
-       "BV4DngUOtj2t6dF1QlRhhe4WYzlCf9C0KixJA4HjbO8iaWlggO16pjEJodeSWBn4JrAbqcpq31iX\n",
-       "I4SFtdsLy/Y7wA5KKerNSB6hL5MYIPEpYAppvNFwmwsieYRQXT1tIA8Bv5Z0LfDvfMy2r2teWCH0\n",
-       "LIkNgR+RvlTtbDOlg6eE0O/Vk0AWI/U62bnieCSQ0OtJLAGcBhwDnEFaRjbaOUKoQz1tIK/a/kIP\n",
-       "xRNCj5HYlbRcwIPAJjYvlhxSCL1KuwnE9juSts9tINFtMfQJEisC3wbeBxxv85uSQwqhV4o2kNBv\n",
-       "5MGAR5DGdFwBvNfu+szSIfRX9SSQxYFXiTaQ0ItJrEdqJF8K2MPmwZJDCqHXa+psvD0pBhKGaiQW\n",
-       "I616+RngLOD7Nu+UG1UIraMlZ+MNoWx5CpKHgc2AkTbnR/IIofvUsyLhT4BTYN5gqimkRXNCaEkS\n",
-       "QyR+BlwJjLXZx+aFsuMKoa+pJ4Esafvetp3cGytm4w0tR0ISh5DWlfkXsKHN9SWHFUKfFbPxhj5B\n",
-       "Ym3SmI53A3vbTC45pBD6vHruQI4n9V5ZT9KLwOeA47pSqKSxkh6TNEXS1ZIWkzRE0kRJT0maIGnZ\n",
-       "ivOflvSEpN27UnboWyQGSYwF7gUmAltG8gihZ9RMIJJOzJur2N6F9M1ufdvbd2Uq97xO+ieBzfJa\n",
-       "6QOBj5N6yky0vS5wa94nr5d+IDAC2AO4UFI9iS/0cRLbAfeTBgRuYfNNO6pXQ+gp7X0QH5X/vQCg\n",
-       "G2fjfZ3UhrKkpEVIi/S8COwNXJbPuQzYN2/vA4y3PScnrmeArbohjtBLSSwrcRHwS1LX3A/bTCs3\n",
-       "qhD6n/baQKZKehpYTVLlzKS2vXEjBdp+VdJ5wPPAf4CbbU+UtJLtWfm0WcBKeXtV4J7CJaYDqzVS\n",
-       "dujd8kjy/YHvADcBI2xeKzeqEPqvmgnE9kGSVgYmAHsB3TJIL69w+FlgDeCfwLWSDqko25LaG+HY\n",
-       "N0Y/hrpJrAH8gPR3c4DNXaUGFELocDLFmcDGkpYA3mP7yW4ocwvgbtuzASRdR1oud6aklW3PlLQK\n",
-       "8HI+fwYwrPD8ofnYQiSNK+xOsj2pG+INJZJYhPSFYwxpAsSPxAJPITRO0ihgVLdcq4410fcmLe+5\n",
-       "mO01JI0Evmx774YKlDYBrgK2BP4LXApMBlYHZts+R9IYYFnbY3Ij+tWkdo/VgFuAdSpnB46pTPoe\n",
-       "iS2BH5PWoznW5pmSQwqhz2namujZOGBr4DYA2w9KWquRwvLzH5Z0OXAfMBd4gPQhMRi4RtLRwDTg\n",
-       "gHz+VEnXkAaHvQ2Mjqnl+zaJwaS1yA8AvghcZUe1ZQitpp47kHttby3pQdsj87FHGm1Eb5a4A+kb\n",
-       "JPYl9fybCJxkM7vkkELo05p9B/KYpIOBRSQNB04A7m6ksBBqkRhKShwjgENtJpUbUQihI/WORN8Q\n",
-       "+B8wnjSO47PNDCr0HxIDJU4gLVz2MLBxJI8Qeod2q7DyQL+JtnfquZAaE1VYvY/ESFL7179IjeRP\n",
-       "lBxSCP1O09YDsf02MLc4L1UIXSWxlMS3gJtJEyDuFMkjhN6nnjaQfwFTJE3M25DG+p3QvLBCXyXx\n",
-       "IeBC4E7SmuQvd/CUEEKLqieBXJd/2uq6RIwED50ksQpwPml1wE/aTCw5pBBCF8Wa6KGpJAYAx5Am\n",
-       "Pfwx8FWb/5QbVQihTbO78YbQEIn3kpKGSe0cj5YcUgihG8W6GqHbSSwh8TXS7AWXAe+L5BFC39Pe\n",
-       "glJX5H9jzEeom8RuwBRgbdKYjh/ZzC05rBBCE9RsA5E0FdgV+ANVZm60/WpTI+ukaAMpl8S7SbPl\n",
-       "7gCMtvldySGFEOrQrDaQH5KWll2LtGxokfPx0M/lRZ6OAr5Oqq7a0J7X3TuE0IfVM5niD20f20Px\n",
-       "NCzuQHqexPrAj4AlgGNsHio5pBBCJ3Xls7OubrySBpKWmJ13x2L7+UYKbJZIID1HYnFgLPBp4MvA\n",
-       "hTbvlBtVCKERTe3GK+kzwJmkFQKLHxIbNVJg6N0kRpHuOqYCm9pMLzeiEEJZ6qnC+iuwVdsStK0q\n",
-       "7kCaS2J50sqUuwGfsbmh5JBCCN2gaZMpZs+TpnDvNpKWlfRLSY9Lmippa0lDJE2U9JSkCcUJHCWN\n",
-       "lfS0pCck7d6dsYT2SUjiUOAx4A1gRCSPEAK03433C3lzBLA+8BvgrXzMtr/dcKHSZcDtti/OU8Yv\n",
-       "BZwK/N32uZJOBparWBN9S+avib6u7bkV14w7kG4msQ6pN97ypEbyv5QcUgihmzXrDmQwsDTpDmQi\n",
-       "MCjvL50KByWiAAAY60lEQVQfa4ikZYD32b4Y0pTxtv8J7E3qBkr+d9+8vQ8w3vYc29OAZ4CtGi0/\n",
-       "dExikMSpwD3A74EtI3mEECrVbES3Pa5JZa4JvCLpEmAT0hiTzwIr2Z6Vz5lF6vUFsCrpg6zNdNKd\n",
-       "SGgCie1JjeTPAVvYTCs3ohBCqypjMsVFSFN6H2/7L5K+C4wpnmDbktpr3a/6mKRxhd1Jtid1MdZ+\n",
-       "Q2I54BvAnqSE/ks7pu0Poa+RNIoqs4s0oowEMh2YbrutSuSXpDEFMyWtbHumpFVg3kJDM4BhhecP\n",
-       "zccW0sS7pj4rjyQ/APgOcANpJPlr5UYVQmiW/MV6Utu+pDMbvVaHvbAk7VDl2PaNFmh7JvCCpHXz\n",
-       "oV1JPXxuAg7Pxw6HeT19bgQ+LmmQpDWB4cDkRssP80msCfwOOA34qM3oSB4hhHrVMw7kQdsjOzrW\n",
-       "qUKlTYCfkhrm/wocCQwErgHeA0wDDrD9Wj7/FNJ8S28DJ9q+uco1oxdWnSQWJVVTnQycB3zLZk65\n",
-       "UYUQytCUqUwkbQtsB3yONMtqWwGDgY/Y3qSRApslEkh9JLYiLfL0MnCczV9LDimEUKJmTWUyiJQs\n",
-       "BrJgt93XgY81Ulgoj8S7gLNJv7svAldHI3kIoSvqqcJaI4+/aGlxB1JdbiT/CPA90touX7JpqbVc\n",
-       "Qgjlafaa6ItJ+gmwRuF82965kQJDz5EYBnwfWA/4hM2fSg4phNCH1JNArgUuIjV6t83GG1UfLUxi\n",
-       "IHA8cDpwAXCAzf/KjSqE0NfUk0Dm2L6o6ZGEbiGxGamR/A1ge5snSw4phNBH1TMb702SPi1plTxj\n",
-       "7hBJQ5oeWegUiaUlziPNXfV9YOdIHiGEZqqnEX0aVaqsbK/ZpJga0p8b0SX2BH4A3A58weaVkkMK\n",
-       "IfQSTV/StjfojwlEYlXgfGAkcKzNLSWHFELoZZq6oJSkpSSdnntiIWm4pD0bKSx0D4kBEqOBh4En\n",
-       "gY0ieYQQelo9jeiXkKZc3y7vv0iaAPE3zQoq1CaxEamRfC4wyuaxkkMKIfRT9TSir237HPJqhLb/\n",
-       "1dyQQjUSS0p8A/gjKam/L5JHCKFM9SSQ/0laom1H0toQYwp6ksQHgCmkwZwb2fzYZm77zwohhOaq\n",
-       "pwprHGkKjKGSrga2B45oYkwhk1iJtE7HtsBom9+XHFIIIcxTVy8sSSsA2+Tde2z/valRNaAv9cKS\n",
-       "GECavv5rwKXAl22i6jCE0O2aNZ37BrYfl7Q5aRxIWwEGsP1AIwU2S19JIBIbkNYkXww4xubhkkMK\n",
-       "IfRhzUogP7H9SUmTqD6QcKdGCmyW3p5AJBYHTgFGk6oNL7LnzT0WQghN0SsHEkoaCNxHWh99rzw9\n",
-       "yi+A1Vl4RcKxpCqdd4ATbE+ocr1em0AkdiLddTwKfMauvuZ7CCF0t2YPJPy0pOUK+8tJGt1IYRVO\n",
-       "BKYy/+5mDDDR9rrArXkfSSOAA4ERwB7AhZLq6T3W8iRWkLgUuAw4yWa/SB4hhN6ing/iY2z/o20n\n",
-       "bx/TlUIlDQU+RJoivi3z7U36ICX/u2/e3gcYb3tOXtjqGWCrrpRfNglJHEa643gN2NDm1yWHFUII\n",
-       "nVJPN94BkgbYngvzqp4W7WK53wFOAt5VOLaS7Vl5exawUt5eFbincN50YLUull8aieHAD4HlgD1t\n",
-       "7is5pBBCaEg9CeRm4OeSfkS6W/gUaVxIQ/I8Wi/bflDSqGrn2Lak9hpnqj4maVxhd5LtSY3G2d0k\n",
-       "BgFfAj5LWpv8Apu3y40qhNDf5M/dUd1xrXoSyMmkKqvj8v5EUtVTo7YD9pb0IWBx4F2SrgBmSVrZ\n",
-       "9kxJqwAv5/NnAMMKzx+ajy3E9rguxNU0EjuQ5q/6K7C5zXMlhxRC6KfyF+tJbfuSzmz0WqVO5y5p\n",
-       "R+CLuRfWucBs2+dIGgMsa3tMbkS/mtTusRpwC7COKwJvxV5YEssB5wAfJnUa+JUdywGHEFpHVz47\n",
-       "a96BSLrW9v6SHmXhKiPb3riRAqtou/Y3gGskHU3uxpsLmirpGlKPrbeB0ZXJoxVJfBD4GXA9MMLm\n",
-       "nyWHFEII3aq9gYSr2n5R0urM7yk1T+4R1TJa6Q4k97A6F9jf5o6y4wkhhFqaNRL9AdubSbrC9qFd\n",
-       "irAHtEoCkfg8qaH8AzaPlx1PCCG0pylVWMBikg4Gtpe0Hwvehdj2dY0U2FdJiNS76iPADjbPlxxS\n",
-       "CCE0VXsJ5FjgYGAZYK8qj0cCySQGAhcBm5IWemq52YpDCKG7tZdAVrZ9bK7K+nGPRdTL5EkQryIl\n",
-       "2l1s3ig5pBBC6BHtTWVySv73uHbO6dckBgO/Ja1P/uFIHiGE/qS9O5DZkiYCa0q6qeIx2967iXG1\n",
-       "PIkVgd+TZhT+dEy9HkLob9pLIB8CNgOuBL5FRSN6M4NqdRLvIY3IvxY4PQYHhhD6ow5Hokta0fYr\n",
-       "kpay3bLLqvZUN16JEaS5wL5t891mlxdCCM3U1PVAgOGSpgJP5MI2lXRhI4X1dhJbA38ETo3kEULo\n",
-       "7+pJIN8lLeT0dwDbDwE7NjOoViSxO/Ab4GibK8qOJ4QQylbXyn62KwfF9atpyCUOBK4APmLz27Lj\n",
-       "CSGEVlDPdO7PS9oeQNIg4AToP1N0SIwGTgV2s3mk7HhCCKFV1NWIDpwP7ErqiTUBOMH27OaHV7/u\n",
-       "bkTPU5OcDhwG7G7zt+66dgghtIqmTKbY23RnApEYQEqa7wP2sJnZHdcNIYRW09ReWJKGSbpe0iv5\n",
-       "51eShjZSWG+Ql569EtgEGBXJI4QQqqunEf0S4EZg1fxzUz7W50gsBfwaWJo0HftrJYcUQggtq54E\n",
-       "sqLtS2zPyT+XAu9utMB8R3ObpMckPSrphHx8iKSJkp6SNEHSsoXnjJX0tKQnJO3eaNntx8UQ0ujy\n",
-       "WcB+Nv9pRjkhhNBX1JNAZks6VNJASYtIOgS6NF35HOBztjcEtgE+LWkDYAww0fa6wK15n7wm+oHA\n",
-       "CNJ4lAsl1dX9uF4SqwF/Au4GjrL7VzflEEJoRD0fxEeR1iefCbwE7A8c2WiBtmfmwYjYfpPUJXg1\n",
-       "YG/gsnzaZcC+eXsfYHy++5kGPANs1Wj5lSSGA3eSxnmcZDO3u64dQgh9WYfjQPKHdrUFpbpM0hrA\n",
-       "SOBeYCXbs/JDs4CV8vaqwD2Fp00nJZxuKJ/NSKPLz7D5aXdcM4QQ+osOE4iky0njPl7L+8sB59k+\n",
-       "qisFS1oa+BVwou03pPm9yGxbUnv9i6s+JmlcYXeS7Um1y2dz0nTsx9qxumIIoX+QNAoY1R3Xqmck\n",
-       "+sZtyQPA9j8kbdaVQiUtSkoeV9i+IR+eJWll2zMlrQK8nI/PAIYVnj40H1uI7XH1lc9g4BfAZyJ5\n",
-       "hBD6k/zFelLbvqQzG71WPW0gkjSksDMEGNhogUq3Gj8Dptouzmh7I3B43j4cuKFw/OOSBklaExgO\n",
-       "TG60/OwHwG02v+jidUIIod+q5w7kPODPkq4hTWWyP3B2F8rcHjgEeETSg/nYWOAbwDWSjgamkRru\n",
-       "sT01lz2VNInjaHdh+LzEocCWwBYNv4IQQgj1TWUiaUNgZ1Lbwx9tT212YJ1Vz3B8iXWAPwO72jzc\n",
-       "M5GFEELrirmw6PhNyFOU3AlcYXNBz0UWQgitq9krEvYVZ5G6B3+/7EBCCKEvqKcNpNfLqwkeDIy0\n",
-       "q3cBDiGE0Dl9PoFIvJs0+eNhNq+UHU8IIfQVfboKK6/rcSlwmc2tJYcTQgh9Sp9OIMBngCFAwwNl\n",
-       "QgghVNdne2FJLAP8FdjO5qnyIgshhNYVvbCqOw74QySPEEJojj55ByKxJPA30oDBR8uNLIQQWlfc\n",
-       "gSzsaOCeSB4hhNA8fe4OJI84fwb4mN3lSRdDCKFPizuQBR0MPBnJI4QQmqtPDSSUGEhaS/3YsmMJ\n",
-       "IYS+rq/dgewHvEphsZQQQgjN0dcSyKnA2THfVQghNF+vSSCS9pD0hKSnJZ1c47T/Ar/tybhCCKG/\n",
-       "6hUJRNJA0jTsewAjgIMkbVDl1O1a6e4jL17fUiKm+rViXBFTfSKmntErEgiwFfCM7Wm25wA/B/ap\n",
-       "PMlmbo9H1r5RZQdQxaiyA6hiVNkB1DCq7ACqGFV2AFWMKjuAKkaVHUAVo8oOoLv1lgSyGvBCYX96\n",
-       "PhZCCKEkvSWBtEy1VAghhKRXjESXtA0wzvYeeX8sMNf2OYVzWv+FhBBCC2p0JHpvSSCLAE8CuwAv\n",
-       "ApOBg2w/XmpgIYTQj/WKkei235Z0PHAzMBD4WSSPEEIoV6+4AwkhhNB6eksjek11DjBsRrkXS5ol\n",
-       "aUrh2BBJEyU9JWmCpGULj43NMT4hafcmxTRM0m2SHpP0qKQTWiSuxSXdK+khSVMlfb0V4srlDJT0\n",
-       "oKSbWiEmSdMkPZJjmtwiMS0r6ZeSHs+/v63LjEnSevn9afv5p6QTyn6fCuU8JmmKpKslLVZ2XJJO\n",
-       "zPE8KunEfKx7YrLda39I1VnPAGsAiwIPARv0UNnvA0YCUwrHzgW+lLdPBr6Rt0fk2BbNsT4DDGhC\n",
-       "TCsDm+btpUntRhuUHVcua8n87yLAPcAOLRLX54GrgBtb5Hf4LDCk4ljZMV0GHFX4/S1TdkyF2AYA\n",
-       "LwHDyo4pX/tvwGJ5/xfA4WXGBbwXmAIsTvq8nAis3V0xNeWX2lM/wLbAHwr7Y4AxPVj+GiyYQJ4A\n",
-       "VsrbKwNP5O2xwMmF8/4AbNMD8d0A7NpKcQFLAn8BNiw7LmAocAuwE3BTK/wOSQlk+YpjpcVEShZ/\n",
-       "q3K8Jf6mgN2BO1ohJmAI6UvbcqREexOwW8m/v48BPy3snwZ8qbti6u1VWK02wHAl27Py9ixgpby9\n",
-       "Kim2Nk2PU9IapDuke1shLkkDJD2Uy7/N9mMtENd3gJNggRkMyo7JwC2S7pP0yRaIaU3gFUmXSHpA\n",
-       "0k8kLVVyTEUfB8bn7VJjsv0qcB7wPKm36Gu2J5Yc16PA+3KV1ZLAh0hfnLolpt6eQFq2B4BT+m4v\n",
-       "vqbFLmlp4FfAibbfaIW4bM+1vSnpj/f9knYqMy5JewIv234QqNoHvqT3anvbI4EPAp+W9L6SY1oE\n",
-       "2Ay40PZmwL9Id/plxgSApEHAXsC1CxVYQkyS1gY+S6qZWBVYWtIhZcZl+wngHGAC8HtS9dQ73RVT\n",
-       "b08gM0h1n22GsWD27GmzJK0MIGkV4OV8vDLOoflYt5O0KCl5XGH7hlaJq43tf5JmTN685Li2A/aW\n",
-       "9CzpG+zOkq4oOSZsv5T/fQW4njQPXJkxTQem2/5L3v8lKaHMbIG/qQ8C9+f3Csr/O98CuNv2bNtv\n",
-       "A9eRqtlLfa9sX2x7C9s7Av8AnqKb3qvenkDuA4ZLWiN/GzkQuLHEeG4kNZqR/72hcPzjkgZJWhMY\n",
-       "Dt2/5K4kAT8Dptr+bgvFtUJbLw9JS5DqhR8sMy7bp9geZntNUjXIH20fWmZMkpaUNDhvL0Wq359S\n",
-       "Zky2ZwIvSFo3H9oVeIxUv1/a31R2EPOrr9rKLjOmJ4BtJC2R/y/uCkyl5PdK0rvzv+8hLbp3Nd31\n",
-       "XnV3Q1JP/5C+hTxJ6i0wtgfLHU+q53yL1A5zJKkR7RZShp8ALFs4/5Qc4xPAB5oU0w6k+vyHSB/Q\n",
-       "D5KmwC87ro2AB3JcjwAn5eOlxlUoa0fm98IqLSZSe8ND+efRtr/nst8nYBNSx4eHSd+ql2mBmJYC\n",
-       "/g4MLhwr/e+J1ED9GCnxX0bqzVT2e/WnHNNDwE7d+V7FQMIQQggN6e1VWCGEEEoSCSSEEEJDIoGE\n",
-       "EEJoSCSQEEIIDYkEEkIIoSGRQEIIITQkEkgLywMkp3R8Zl3X2lHStp19rDtJWl9pSvf7Ja3V7PI6\n",
-       "iOUEpanJr8iDpm7Jcz0dkOd72qCd5+6lBpcOkLSMpOM6+1gH1yy+lk7HJukdpWnR23432+bjq0s6\n",
-       "qBPXGSPpE3n7eElH5O0Ffu/VrinpzPaOSdotzw/2SP53p8Jjt7YNwKx1PaVp1W9XmpNtlPL0/XW8\n",
-       "pm9XTicT5otxIC1MaULEm2xv1A3XGge8Yfu8Tj420PY7lccbjGEMMND22Z14zgDbczs+s9OxPA7s\n",
-       "YvtFSdsAZ9nerbvLqVLuGtT4nTb6+y6+lgZjesN22wj43YFTbI+SNAr4gu296rzOH4H9gVdJA0e3\n",
-       "dFpNdN7vvfKaks4mTfi5G2kQ7MXAAVWOCZhpe6akDYGbbQ/N1/gkaUDhtyUdDKwCLJ/jeNH2VZKO\n",
-       "Is1y/M16X5ekAaSpz8+zvXc970G/06wRmfHTLSNI1yBNhfBj0sjkm4HF82NrkyZHu4800nS9fHwv\n",
-       "0nobD5Dm/n93vs5LpHmNHgR2qCij7bEHSKPZLwV+mK/zLWBL4O78+F3Auvm5R5BGJv+eNKL1nHx8\n",
-       "YL7GFNLI88+SZgxoK+fWfN4hpA+KB3N5A/LxN3O5DwHbVbwn65BG0D4E3A+smY9/s1DeAYXzTyJN\n",
-       "xfAwMC4f+yHwv3zul4Cngdfy61sLmARsns/dI5fzEDCx8LovyNsrkuaHmpx/tsvHx5E++G4D/gp8\n",
-       "Jh//OfDv/JrPqXhtCz1W63UVnlN8LZ+tiO1S4Pz8O/sr8NEaf2dvFLb3B67L2/fk9+XBfO3D266d\n",
-       "H/8NsGPefhdwZ97eARiftz9U+L3/Efhz4Zon5nMuIn3YDy9ce6FjhccEzAYWzfsrAZMLjx8EvF3x\n",
-       "dzCR+X+3o/Lv5VrgceDKwnnTgG/k3/kB+dgjFEZqx0/hd1F2APHTzi8nfbjPATbO+78ADs7btwLr\n",
-       "5O2tmf+hXJyS4P+Ab+XtM4HP1yhngceAS0hz4rTdoQ4mfYOENL/PL/P2EfmDaTCwWP7PN5Q0UeKE\n",
-       "wvXeVVkOaaGrGwvXvRA4NG/PBT5WI9Z7gX3y9iBgCeCjpOkYREqYz5HWONgd+FE+dwDpA+99ef9Z\n",
-       "8sJNpKlMbiqUcRtpwsAVSVNzr158byl8kJLmFdo+b7+HNA8ZpARyJ2kqi+VJ024MBFansIZMxWtb\n",
-       "4LFar6vK84qvpRjbpcAvCu/30zXKfZv0gf446cN9ZI33pTKB3AS8P2/vx/wEPYYF/56Kv/fKa54F\n",
-       "7A18j5TsNq52rCLej1H4+8rH/kZaRO0g4IvA10lfHg7K7/tLhXNH5de5an5v72Z+4n8W+GLFtS8D\n",
-       "Plj250Er/ixCaHXP2n4kb98PrJEn2tsOuDbN2QakD1OAYZKuIX2ADiL9x2pTddryGo9d6/y/B1gW\n",
-       "uFzSOqSpnYt/N7c6TxkvaSr5QxRYS9L3SDPvTqhSzi6kRHNffg1LADPzY++QZhReMMBUz72q7V8D\n",
-       "2H4rH98euDrH+7Kk20l3TTsCu0t6MF9iKdIdzB0dvPa2Y9sAf7L9XC7vtSrn7QpsUPg9DM6/HwO/\n",
-       "tT0HmC3pZdI35c78Dmq9rrrq73MMN+TYH5e0Uo3z/uM0hTy5Ou8K0kp27cVaaQ/SRJ6Q/gburHhc\n",
-       "Ff+S4zo9lzvS9pfz4UeqHCMf25B0h1BZ3TgLGGZ7fD7vTNvfzNsrAW9UnD/ZucpPaZ2aNUiJBNIX\n",
-       "taIX8+OhQiSQ1ve/wvY7pKUpBwD/aPtPX+EC0l3HbyTtSPom3Ih/F7bPIiWKj0hanVTFUyu+RWy/\n",
-       "JmkT4APAsaQ67aOrlHGZ7VOqHP9vIXnVq9aH3ddt/7iT12pTTwwCtm5LZvMOpoRSPPYOjf1/q3xd\n",
-       "nX1fijF0mBBs36M0e/IKVR5+mwU73ixe2N4S+FRnyqoo98sdHZM0lFRleqjtZytOF4WFwapcrzKe\n",
-       "hf5uC/v/qvLcaCyuInph9T7K3/iflfQxSNO4S9o4P/4u0jcmSFVMbd4gVTVV095jldc8sqP4JC1P\n",
-       "qpq6DjidVB0EC/4nvhX4mKQV85OGKE03XVN+3dMl7ZOfs5jS9PB3AAfmHjYrAu8nVXXdDByV7wiQ\n",
-       "tFpbeXUwqQ3g/blxG0lDqryOCcAJhRe/SQfX7czvodrr6mi677o+uCU9UeP4+qTPhdlV4pkGbJr/\n",
-       "3oaR1ippuyt4opD026oQq+nob61WvMuS7mZPtv3nKqesRO21gP5Oqt5q1Cqk1x4qRAJpfZXffNr2\n",
-       "DwaOzrffj5LqjCHdcVwr6T7glcL5NwEfyd01t6+4ZttjD0jaoUq55wJfl/QAqT7ZhXOqxbcacFuu\n",
-       "OrqC+SvYzTvf9uOk9ZknSHqY9EG8cuG8Wg4FTsjPuYu0NOf1pGqPh0mJ6STbLzstJ3o18GdJj5Aa\n",
-       "Tat9kFR7Hdj+O3AMcF1+n8dXOf8EYAtJD0t6jAW/hVe75mzgLklTJJ3T3mO1XleN+Gu9loW2q9xd\n",
-       "LJH/Lh4kNeQfnpPBw8A7Sl1wT7R9F6mNYCqpbeJ+UsL6IKkjRZs7SYsrVYtxgWtWeS21HE/qOHJm\n",
-       "W6yFLx8rA7NtV945pIJTL8JHJa1XiKUzdxQjSY3/oUJ04w2hn5H0YVLvte930/UmkKqVZuV9kXq0\n",
-       "LVS11wySjgGWsv2dds45gvRl45xa59R43rqkKuHoxltFJJAQQreTNJrUOH9JD5R1K6ln3pvtnDOI\n",
-       "1P17x860r0n6Nqlbc2WngEAkkBBCCA2KNpAQQggNiQQSQgihIZFAQgghNCQSSAghhIZEAgkhhNCQ\n",
-       "SCAhhBAa8v/Onrp6J+51IAAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaadcc88>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "from math import tanh\n",
-    "Af=(20*0.75*12*2)/(144);\n",
-    "Ao=((3.14*1.25)-(20*0.035))*(12/144);\n",
-    "print\"\\t fin surface is : %.1f ft**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  ft**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "Ai=(3.14*1.06*12)/(144);\n",
-    "print\"\\t total inside surface :  ft**2/lin ft \\t\",Ai\n",
-    "print\"\\t fin efficiencies \\t\"\n",
-    "b=0.0625; # ft\n",
-    "hf=4; # from table in solution\n",
-    "m=(5.24*(hf**(1/2))); # m=((hf*P)/(Kax))**(1/2), eq 16.8\n",
-    "n=(tanh(m*b))/(m*b); # efficiency , eq 16.26\n",
-    "print\"\\t hf      m      n \\t \"\n",
-    "print hf   \n",
-    "print m      \n",
-    "print n\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "print\"\\t weighted efficiency curve \\t\"\n",
-    "hfi=((n*Af)+(Ao))*(hf/Ai); # eq 16.34\n",
-    "print\"\\t hf      hfi \\t \"\n",
-    "print hf      \n",
-    "print hfi\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "hf=[4, 16, 36, 100, 400, 625, 900]; # from 2nd table in the solution\n",
-    "hfi=[35.4, 110.8, 193.5, 370, 935, 1295, 1700]; # from 2nd table in the solution\n",
-    "pyplot.plot(hf,hfi)\n",
-    "pyplot.xlabel('heat transfer coefficient to fin,Btu/(ft**2)*(hr)')\n",
-    "pyplot.ylabel('coefficient hf referred to the tube ID')\n",
-    "pyplot.title('weighted fin efficiency curve')\n",
-    "pyplot.show()\t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.2 pgno:525"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t annulus flow area : ft**2 \t0.0391482454167\n",
-      "\t wetted perimeter : ft \t2.76875\n",
-      "\t equivalent diameter : ft \t0.0565572845749\n",
-      "\t heat load : Btu/hr \t270286.4\n",
-      "\t delt1 is : F \t151.0\n",
-      "\t delt2 is : F \t117.0\n",
-      "\t LMTD is  F \t133.427780969\n",
-      "\t Ui : Btu/(hr)*(ft**2)*(F) \t365.652178958\n",
-      "\t hfi : Btu/(hr)*(ft**2)*(F) \t416.40535396\n",
-      "\t jf : \t36.7135894676\n",
-      "\t Ga : lb/(hr)*(ft**2) \t388267.720257\n",
-      "\t Rea : \t11319.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Ts=302.; # F\n",
-    "t1=151.;\n",
-    "t2=185.;\n",
-    "w=15200.; # lb/hr\n",
-    "from math import log10\n",
-    "# The dropwise condensation of steam was promoted with oil.\n",
-    "aa=(3.14*(3.068**2-1.25**2))/(4*144)-((20*0.035*0.75)/(144));\n",
-    "print\"\\t annulus flow area : ft**2 \\t\",aa\n",
-    "p=(3.14*(1.25/12))-(20*0.035/12)+(20*0.75*2/12);\n",
-    "print\"\\t wetted perimeter : ft \\t\",p\n",
-    "De=(4*aa/p);\n",
-    "print\"\\t equivalent diameter : ft \\t\",De\n",
-    "Q=w*0.523*(t2-t1);\n",
-    "print\"\\t heat load : Btu/hr \\t\",Q\n",
-    "delt1=Ts-t1; #F\n",
-    "delt2=Ts-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Ai=0.277; # ft**2/ft\n",
-    "n=20; # number of fins\n",
-    "Ui=(Q/(Ai*n*LMTD));\n",
-    "print\"\\t Ui : Btu/(hr)*(ft**2)*(F) \\t\",Ui\n",
-    "hi=3000; # assumed value for dropwise condensation of steam\n",
-    "hfi=(Ui*hi)/(hi-Ui);\n",
-    "print\"\\t hfi : Btu/(hr)*(ft**2)*(F) \\t\",hfi\n",
-    "hf=120; # from fig 16.7 for hfi=418\n",
-    "mu=1.94; # lb/(ft*hr)\n",
-    "k=0.079;\n",
-    "Z=2.34; # Z=((c*mu)/k)**(1/3)\n",
-    "jf=(hf*De/(Z*k)); # eq 16.36\n",
-    "print\"\\t jf : \\t\",jf\n",
-    "Ga=(w/aa);\n",
-    "print\"\\t Ga : lb/(hr)*(ft**2) \\t\",Ga\n",
-    "Rea=(De*Ga/mu);\n",
-    "print\"\\t Rea : \\t\",round(Rea)\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.3 pgno:530"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 12,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t477000.0\n",
-      "\t total heat required for water is :  Btu/hr \t478000.0\n",
-      "\t delt1 is :  F \t120.0\n",
-      "\t delt2 is :  F \t130.0\n",
-      "\t LMTD is :%.0f F \t125.073724087\n",
-      "\t ratio of two local temperature difference is :  \t0.923076923077\n",
-      "\t caloric temperature of hot fluid is :  F \t223.5\n",
-      "\t caloric temperature of cold fluid is :  F \t98.8\n",
-      "\t hot fluid:shell side,gas oil \t\n",
-      "\t flow area is :  ft**2 \t0.0287156933333\n",
-      "\t wetted perimeter :  in \t29.126\n",
-      "\t De :  ft \t0.0473238096546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t626834.943216\n",
-      "\t reynolds number is :  \t4903.1764525\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t97.2026562015\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.01409546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t847790.707079\n",
-      "\t V is :  fps \t3.76795869813\n",
-      "\t reynolds number is :  \t65199.6985471\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t795.4\n",
-      "\t calculation of tfw \t\n",
-      "\t phya is :  \t0.953986161765\n",
-      "\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t92.729988903\n",
-      "\t Rf :  \t0.0107839978396\n",
-      "\t hf1 :  \t78.2227916919\n",
-      "\t hfi2 :  \t450.563280145\n",
-      "\t Rmetal :  \t0.00170212455807\n",
-      "\t Ri :  \t0.00125722906714\n",
-      "\t hi1 :  \t234.894572087\n",
-      "\t UDi :  \t122.267359744\n",
-      "\t Ai :  ft**2 \t31.2572870644\n",
-      "\t length of pipe required :  lin ft \t74.0694006266\n",
-      "\t Q/Ai1 :  Btu/(hr)*(ft**2) \t14158.7677725\n",
-      "\t annulus film :  \t31.4245931625\n",
-      "\t annulus dirt :  \t4.9162388099\n",
-      "\t Tc-tfw :  \t36.3408319724\n",
-      "\t fin and tube metal :  \t24.0999863376\n",
-      "\t tube side dirt :  \t42.4763033175\n",
-      "\t tubeside film :  \t17.8008143984\n",
-      "\t total temperature drop :  F \t120.717936026\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t3719.56602669\n",
-      "\t delPs is :  psi \t7.7\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t1.6\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=18000; # lb/hr\n",
-    "w=11950; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is :%.0f F \\t\",LMTD\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.47; # from fig.17\n",
-    "Kc=0.27; \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,gas oil \\t\"\n",
-    "ID=3.068; # in, table 11\n",
-    "OD=1.9; # in, table 11\n",
-    "af=0.0175; # fin cross section,table 10\n",
-    "aa=((3.14*ID**2/(4))-(3.14*OD**2/(4))-(24*af))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "p=(3.14*(OD))-(24*0.035)+(24*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*aa*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=2.5*2.42; # at 224F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jf=18.4; # from fig.16.10\n",
-    "Z=0.25; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hf=((jf)*(1/De)*(Z)); # Hf=(hf/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hf\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "D=0.134; # ft\n",
-    "row=62.5;\n",
-    "at=(3.14*D**2/(4));\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.72*2.42; # at 99F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(970*0.82); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "print\"\\t calculation of tfw \\t\"\n",
-    "# Tc-tfw=40F assumption from fig 14\n",
-    "tfw=184;\n",
-    "mufw=3.5; # cp, at 184F\n",
-    "phya=(2.5/mufw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "hf=(Hf)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.002;\n",
-    "Rf=(1/hf);\n",
-    "print\"\\t Rf :  \\t\",Rf\n",
-    "hf1=(1/(Rdo+Rf)); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=255; # fig 16.9\n",
-    "hfi2=(hf1*5.76); # eq 16.38 and fig 16.9,((Af+Ao)/(Ai))=5.76 from previous prblm\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "Rmetal=(hfi2-hfi1)/(hfi2*hfi1)# eq 16.39\n",
-    "print\"\\t Rmetal :  \\t\",Rmetal\n",
-    "phyt=1; # for cooling water\n",
-    "Rdi=0.003;\n",
-    "Ri=(1/hi);\n",
-    "print\"\\t Ri :  \\t\",Ri\n",
-    "hi1=(1/(Rdi+Ri)); # eq 16.40\n",
-    "print\"\\t hi1 :  \\t\",hi1\n",
-    "UDi=(hi1*hfi1)/(hi1+hfi1); # eq 16.41\n",
-    "print\"\\t UDi :  \\t\",UDi\n",
-    "# To obtain the true flux the heat load must be divided by the actual heat-transfer surface.For a 1}2-in. IPS pipe there are 0.422 ft2/lin foot, from table 11\n",
-    "# trial\n",
-    "Ai=(Q/(UDi*LMTD)); # LMTD=delt\n",
-    "print\"\\t Ai :  ft**2 \\t\",Ai\n",
-    "L=(Ai/0.422);\n",
-    "print\"\\t length of pipe required :  lin ft \\t\",L\n",
-    "# Use two 20-ft hairpins = 80 lin ft\n",
-    "Ai1=(80*0.422); # ft**2\n",
-    "r=(Q/Ai1);\n",
-    "print\"\\t Q/Ai1 :  Btu/(hr)*(ft**2) \\t\",r\n",
-    "deltf=(r/hfi2);\n",
-    "deltdo=(r*Rdo/5.76);\n",
-    "print\"\\t annulus film :  \\t\",deltf\n",
-    "print\"\\t annulus dirt :  \\t\",deltdo\n",
-    "d=deltf+deltdo; # d=Tc-tfw\n",
-    "deltmetal=(r*Rmetal);\n",
-    "deltdi=(r*Rdi);\n",
-    "delti=(r/hi);\n",
-    "print\"\\t Tc-tfw :  \\t\",d\n",
-    "print\"\\t fin and tube metal :  \\t\",deltmetal\n",
-    "print\"\\t tube side dirt :  \\t\",deltdi\n",
-    "print\"\\t tubeside film :  \\t\",delti\n",
-    "Td=deltf+deltdo+deltmetal+deltdi+delti;\n",
-    "print\"\\t total temperature drop :  F \\t\",Td\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0359; # ft\n",
-    "Rea1=(De1*Ga/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Rea1\n",
-    "f=0.00036; # fig 16.10\n",
-    "s=0.82; #using fig.6\n",
-    "delPs=((f*(Ga**2)*(80))/(5.22*(10**10)*(De1)*(s)*(phya))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000192; # friction factor for reynolds number 65000, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(80))/(5.22*(10**10)*(0.134)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.4 pgno:535"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 13,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for oxygwn is :  Btu/hr \t1012500.0\n",
-      "\t total heat required for water is :  Btu/hr \t1010000\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t66.8818722257\n",
-      "\t R is :  \t7\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.87 \t\n",
-      "\t delt is :  F \t58.1872288364\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t flow area is :  ft**2 \t1.46834418403\n",
-      "\t wetted perimeter :  in \t1570.8\n",
-      "\t De :  ft \t0.0448691882056\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20431.1770539\n",
-      "\t reynolds number is :  \t16820.7399724\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t20.6536497998\n",
-      "\t hf1 :  \t19.4485963081\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0582118055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t867521.622428\n",
-      "\t V is :  fps \t3.85565165523\n",
-      "\t reynolds number is :  \t29155.8813311\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t902.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t243.418213207\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t89.6828045249\n",
-      "\t total surface area is :  ft**2 \t229.376\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t75.673831631\n",
-      "\t excess fouling factor :  \t0.00206419817483\n",
-      "\t Rdo :  \t0.0221351170807\n",
-      "\t hf2 :  \t14.1738000666\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t77.1741091592\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t16232.4764484\n",
-      "\t delPs is :  psi \t0.6\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=100; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=50500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.225; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oxygwn is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.87 \\t\"# from fig 18\n",
-    "delt=(0.87*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "ID=19.25; # in, table 11\n",
-    "OD=1; # in, table 11\n",
-    "As=((3.14*ID**2/(4))-(70*3.14*OD**2/(4))-(70*20*0.035*0.5))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "p=(70*3.14*(OD))-(70*20*0.035)+(70*20*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*As*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0545; # at 175F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=59.5; # from fig.16.10a\n",
-    "k=0.0175;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "hf=((jH)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.479; # table 10\n",
-    "L=16;\n",
-    "Nt=70;\n",
-    "n=4;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0652; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.94; # at 90F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(940*0.96); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi);\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "UDi=((hfi1)*(hi1)/(hi1+hfi1)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A2=0.2048; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UDi1=((Q)/((A)*(delt)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi1\n",
-    "Re=(1/UDi1)-(1/UDi);\n",
-    "print\"\\t excess fouling factor :  \\t\",Re\n",
-    "Ro=9.27; #Adding to the outside fouling factor\n",
-    "Rdo1=Rdo+(Re*Ro);\n",
-    "print\"\\t Rdo :  \\t\",Rdo1\n",
-    "hf2=(hf/(1+(hf*Rdo1)));\n",
-    "print\"\\t hf2 :  \\t\",hf2\n",
-    "hfi2=113;\n",
-    "UDi2=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi2\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0433; # ft\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.00025; # fig 16.10\n",
-    "s=0.00133;\n",
-    "delPs=((f*(Gs**2)*(L))/(5.22*(10**10)*(De1)*(s)*(1))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00021; # friction factor for reynolds number 29100, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(0.0625)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.5 pgno:556"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for air is :  Btu/hr \t1250000.0\n",
-      "\t total heat required for water is :  Btu/hr \t1248000.0\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t60.0\n",
-      "\t LMTD is : F \t54.9097962457\n",
-      "\t R is :  \t1.25\n",
-      "\t S is :  \t0.4\n",
-      "\t FT is 0.985 \t\n",
-      "\t delt is :  F \t54.086149302\n",
-      "\t caloric temperature of hot fluid is :  F \t225.0\n",
-      "\t caloric temperature of cold fluid is :  F \t170.0\n",
-      "\t fin surface is :  in**2/lin ft \t310.86\n",
-      "\t bare tube surface is :  in**2/lin ft \t27.1296\n",
-      "\t total outside surface :  ft**2/lin ft \t337.9896\n",
-      "\t projected perimeter :  in/ft \t161.28\n",
-      "\t De :  ft \t0.111235119048\n",
-      "\t flow area :  ft**2 \t7.53\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t13280.2124834\n",
-      "\t reynolds number is :  \t28408.1926263\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.9878748896\n",
-      "\t hf1 :  \t21.5048242607\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.079625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t391836.734694\n",
-      "\t V is :  fps \t1.74149659864\n",
-      "\t reynolds number is :  \t30427.5453198\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t667.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t222.303643994\n",
-      "\t X : \t0.03125\n",
-      "\t hfi2 :  \t212.371237248\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.611980947\n",
-      "\t inside surface per bank is :  ft**2 \t18.312\n",
-      "\t Ai1 :  ft**2 \t212.447090593\n",
-      "\t number of banks :  \t11.6015230774\n",
-      "\t net free volume :  ft**3 \t1.89483559028\n",
-      "\t frictional surface :  ft**2 \t191.88\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 :  ft \t0.0395004292324\n",
-      "\t reynolds number :  \t10087.9633345\n",
-      "\t delPs is :  psi \t0.232069401484\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.39\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=150.; # inlet cold fluid,F\n",
-    "t2=190.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=31200; # lb/hr\\\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for air is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.985 \\t\" # from fig 18\n",
-    "delt=(0.985*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "Af=(3.14*2*8*12*(1.75**2-1**2))/(4);\n",
-    "Ao=((3.14*1*12)-(3.14*1*8*0.035*12));\n",
-    "print\"\\t fin surface is :  in**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  in**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "p=(2*3*2*8*12/8)+(((12)-(8*0.035*12))*(2));\n",
-    "print\"\\t projected perimeter :  in/ft \\t\",p\n",
-    "De=(2*A/(3.14*p*12)); # eq 16.104\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "# 21 tubes may be fit in one :vertical bank (Fig. 16.19b) ,20 tubes in alternating banks for triangular pitch\n",
-    "As=((4**2*12**2)-(21*1*48)-((21)*(2*0.035*3*8*48/8)))/(144); # fig 16.19\n",
-    "print\"\\t flow area :  ft**2 \\t\",As\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.052; # at 225F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jf=157; # from fig.16.18a\n",
-    "k=0.0183;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "phys=1;\n",
-    "hf=((jf)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.546; # table 10\n",
-    "L=4;\n",
-    "Nt=21;\n",
-    "n=1;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0695; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.895; # at 170F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(710*0.94); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi); # 16.40\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "k1=60; # table 3 , for brass\n",
-    "# yb=0.00146 ft\n",
-    "X=((0.875-0.5)/12)*(21.5/(60*0.00146))**(1/2);\n",
-    "print\"\\t X : \\t\",X\n",
-    "nf=0.91; # from fig 16.13a , by comparing X value\n",
-    "Ai=0.218; # ft**2/ft\n",
-    "hfi2=((nf*Af/144)+(Ao/144))*(hf1/Ai); # eq 16.34\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "UDi=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A=(21*4*Ai); # ft**2\n",
-    "print\"\\t inside surface per bank is :  ft**2 \\t\",A\n",
-    "Ai1=(Q/(UDi*delt));\n",
-    "print\"\\t Ai1 :  ft**2 \\t\",Ai1\n",
-    "Nb=(Ai1/A);\n",
-    "print\"\\t number of banks :  \\t\",Nb\n",
-    "Vn=(4*4*1.95/12)-(41*3.14*1*4/(2*4*144))-((41*3.14*0.035*8*4/(144*2*4))*(1.75**2-1**2)); # fig 16.19b\n",
-    "print\"\\t net free volume :  ft**3 \\t\",Vn\n",
-    "Af1=(41*2.34*4/2);\n",
-    "print\"\\t frictional surface :  ft**2 \\t\",Af1\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=(4*Vn/Af1); # ft\n",
-    "print\"\\t De1 :  ft \\t\",De1\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.0024; # fig 16.18b\n",
-    "s=0.000928;\n",
-    "Lp=1.95;\n",
-    "R1=0.538; # R1=(De1/ST)**(0.4)\n",
-    "R2=1; # R2=(SL/ST)**0.6\n",
-    "delPs=((f*(Gs**2)*(Lp)*(R1)*(R2))/(5.22*(10**10)*(De1)*(s)*(1)));\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 30400, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(Nb))/(5.22*(10**10)*(0.0695)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_3.ipynb
deleted file mode 100755
index 4ffc6c97..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_16_Extented_Surfaces_3.ipynb
+++ /dev/null
@@ -1,1035 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 16: Extented Surfaces"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.1 pgno: 521"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t fin surface is : %.1f ft**2/lin ft \t2.5\n",
-      "\t bare tube surface is :  ft**2/lin ft \t0.0\n",
-      "\t total outside surface :  ft**2/lin ft \t2.5\n",
-      "\t total inside surface :  ft**2/lin ft \t0.277366666667\n",
-      "\t fin efficiencies \t\n",
-      "\t hf      m      n \t \n",
-      "4\n",
-      "5.24\n",
-      "0.965717954492\n",
-      "\t weighted efficiency curve \t\n",
-      "\t hf      hfi \t \n",
-      "4\n",
-      "34.8173760783\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAZAAAAEZCAYAAAC5AHPcAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XeYXGX5xvHvnUCoEQggLZEaSpASelNCFZUmCoh0+IkQ\n",
-       "EWxIQo0iKigqomClQxQUEGwkIEGKEOmBUJUACSRgEAEbgdy/P953k5PJzO7s7M6e2d3nc1175Zwz\n",
-       "Z877zOxmnjlvlW1CCCGEzhpQdgAhhBB6p0ggIYQQGhIJJIQQQkMigYQQQmhIJJAQQggNiQQSQgih\n",
-       "IZFAQreTdJGk0+o891JJZzUxlnavL+mrkl6R9KKkYZLekKQmxLGepIckvS7peEmLS7pJ0muSrpH0\n",
-       "CUk313GdsZJ+0t3xhdCIRcoOIPQ9to/rzOn5pypJc4F1bP+t0XBqXV/Se4DPA8Nsz86HBzdYTke+\n",
-       "BNxqe9Nc9qHAu4Ehtufmc67u6CK2v96k+ELotLgDCb1BV+8Iaj3/PcDsQvJoptWBqRX7TxWSR78m\n",
-       "aWDZMYTOiwQS5pF0pKQbC/tPS7qmsP+CpI3z9vqSJkqaLekJSfsXzlug2kjSl3IV0XRJ/ydprqS1\n",
-       "CkUPkfSbXL1zT9tjkv6UH384Vy3tn4/vmauD/iHpLkkbFcoaKemBfK2fA4vXeK27AhOAVfO1L5a0\n",
-       "Ro5tQD5nkqSvSLozX+9mScu38/5VjUvSH4FRwPdzWVcDpwMH5v2jJB0h6Y7CtTYsvL8zJY3Nx8dJ\n",
-       "uqJw3jaS7s5lPiRpx8Jj7cYvaYfCc5+XdLikLXN5Kpy3n6SHarzmJSSdJ2laro67I1fPjZL0QsW5\n",
-       "0yTtXHgdv5R0haR/AqdI+rek5Sp+l6+0JZf8Pk2V9KqkP+Q7yFAm2/ETP9gGWBP4R95eFZgGPJ/3\n",
-       "1wJezdtLAS8Ah5O+hGwKvAJskB+/BPhK3t4DeAnYAFgCuBKYC6yVH78U+DuwBTAwPz6+ENO8c/P+\n",
-       "SGAWsCXpzuIw4FlgUWAQ8BxwYr7WR4G32mKp8np3BF4o7K+RyxuQ9ycBTwPrkBLRbcDXa1yrZlz5\n",
-       "8duAowrnnwlcXtg/Argjbw/O79nn8mtaGtiq8Lwr8vZq+b3bI+/vmveX7yh+0h3Q68CB+b0aAmyc\n",
-       "H3us7Zp5/3rgczVe9w+APwKr5L+FbXLMo4rvbT73WWDnvD0u/272zvuLA7cC/1c4/5vAhXl7n/xa\n",
-       "1svlnArcVfb/mf7+E3cgYR7bzwJvSBoJvB+4GXhR0nqkD9u2O4I9gWdtX2Z7ru2HgOuA/atc9gDg\n",
-       "YtuP2/4P6QNwgWKB62zfZ/sd4CpSQqrlGOBHtv/i5HLgf8C2pA+vRWyfb/sd278C/tLOtTqqGjNw\n",
-       "ie1nbP8XuKad2GrFtU2N8tRO+XsCL9r+ju23bL9pe3KVaxwC/M72HwBs3wLcB3y4jvg/AUy0/Yv8\n",
-       "Xr1q+5H82OX52kgaAuxOlfaZfKd2JHCi7Zfy38I9tt+q8boq3W37xhz7f3MZB+Vri5Tc2so9lpT8\n",
-       "nnSq9vs6sKmkYXWWFZogGtFDpdtJ3x7XyduvkZLHtnkf0rfXrSX9o/C8RUgfPJVWASYX9qdXOWdW\n",
-       "Yfs/pG/ctawOHCbpM4Vji+ZyBMyoOP85utaGMrPO2GrFtWphv96ZS4cB9XQaWB3YX9JehWOLkO4I\n",
-       "2tSKv70yrgIek7Qk6QvAn2zPqnLeCqQ7h7/WEWs1lX8L1wEXSFqZdKcx1/ad+bHVgfMlnVfxnNVI\n",
-       "d8OhBJFAQqXbgb1J1TlnkxLIIaRv0hfkc54Hbre9ex3Xe4n0YdWmq98YnwfOtv21ygdy/f9qFYdX\n",
-       "B57pYpldiquG9pLJ86Rv3/WUeYXtY+oss/K5W1UNzJ4u6R5gP9Lv/sIa1/g78F/Sl41HKh77F7Bk\n",
-       "205ux1ixsqiKcv8haQLptY8AxlfEe5bt4rFQsqjCCpVuB3YCFrf9InAnqR1jCPBgPuc3wLqSDpG0\n",
-       "aP7ZUtL6+fFi9cw1wJFKje5LkhqPizq6O5gFrF3Y/wlwrKStlCwl6cOSlgbuBt6WdEKOaT9Sm0RX\n",
-       "1Hv30l5c1a7V3nV/C6wi6URJi0kaLKnah/2VwF6Sdpc0sNB4XUyitcq5GthV0v6SFpG0vKRNCo9f\n",
-       "DpwMvJd0Z7CQXJV0MfBtSavkGLaVNAh4Clhc0ockLQqcBizWzmsuxnU4qf2qWG32Q1JD+wgAScuo\n",
-       "0HEjlCMSSFiA7aeBN4A78v7rpCqKu+zUmmn7TVK9+MdJVUYvkeqkB7VdJv+Q6+e/R2rAfQr4cz7n\n",
-       "f5XnFsMobI8DLss9hT5m+37gk8D3gVdJDauH5bLmkL41HwHMJlW//Kqjl9yJ/ZpjStqJq/L5ta5V\n",
-       "fM/eAHYD9iK9t0+RqhUrz5tOalw+BXiZ9C39CyyYNGqV8TzwoXz+bNKXg40L515H6uZ8fW6fqOWL\n",
-       "wBRSW9Ns0t+BbP8TGA38lFRV9SYLVjXVei9vJN3RvGR7yryT7RuAc4Cf515bU4APtBNX6AHKnwnd\n",
-       "f2HpYlJj3su227ozbkX6D7Yo8DYw2vZf8mNjgaOAd4ATbE/Ixzcn9dRZnNRgeGJTAg49QtIGpP/8\n",
-       "gxxjIFqapKeBT9n+Y4cnh36pmXcgl5CqPorOBU63PRI4I++Tb0vb6j33AC4s9EO/CDja9nBguKTK\n",
-       "a4YWJ+kjuSpmOdK3yBsjebS2XP3nSB6hPU1LILbvAP5RcfglYJm8vSzze8zsQ+r7P8f2NFKj59aS\n",
-       "VgEGF7owXg7s26yYQ9McQ2rLeAaYA3RmqpPQwyRNIjWcf7rkUEKL6+leWGOAOyV9i5S8ts3HVwXu\n",
-       "KZw3ndSbZg4LdvWbwcK9bEKLs/3BsmMI9bM9quwYQu/Q043oPyO1b7yHNMr24h4uP4QQQjfp6TuQ\n",
-       "rWzvmrd/SeqhAenOojg+YCjpzmNG3i4erxwoBoCk5vQGCCGEPs52Y4NtmzlPCmkw2pTC/gPAjnl7\n",
-       "F+AveXsE8BCpG+iapG6jbT3E7gW2JnVN/B2FOXoqynIzX0uDr39c2TFETH0rrogpYmpCXG70uU27\n",
-       "A5E0njQFxgp5Vs4zSI2pP5C0GGlahWNy9FOVZn2dyvzuvW13FKNJ3XiXoDDvTwghhHI1LYHYPqjG\n",
-       "Q1vXOP9rwELTQDgN0Npo4WeEEEIoU4xEb65JZQdQxaSyA6hiUtkB1DCp7ACqmFR2AFVMKjuAKiaV\n",
-       "HUAVk8oOoLs1bSR6T5NkN9oQFEII/VRXPjvjDiSEEEJDIoGEEEJoSCSQEEIIDYkEEkIIoSGRQEII\n",
-       "ITQklrQNIYR+SGI54NiuXCPuQEIIoR+RWF7iq6TlFYZ35VqRQEIIoR+QeLfEOaQlklcEtrA5qivX\n",
-       "jAQSQgh9mMQqEt8GngCWAja1+ZTNs129diSQEELogySGSnwPeIw0m/l7bY63eaG7yogEEkIIfYjE\n",
-       "6hIXAY8A/wNG2HzO5sXuLisSSAgh9AESa0v8lLTu0j+A9WxOspnZrDKjG28IIfRiEusCpwB7Aj8A\n",
-       "htu82hNlRwIJIYReSGIEcCqwO/A9YB2b13oyhqZVYUm6WNIsSVMqjn9G0uOSHpV0TuH4WElPS3pC\n",
-       "0u6F45tLmpIfO79Z8YYQQm8gsbHENcBtwBRgbZuzejp5QHPbQC4B9igekLQTsDewse33At/Kx0cA\n",
-       "B5LWRt8DuFBS2/z0FwFH2x4ODJe0wDVDCKE/kBgpcR1wM3AvsJbNN2xeLyumDhOIpGUlbZl/lqn3\n",
-       "wrbvIDXkFB0HfN32nHzOK/n4PsB423NsTyONkNxa0irAYNuT83mXA/vWG0MIIfR2EltJ3AT8Brid\n",
-       "dMdxns2/Sg6tdgKRtJikS4FpwI+BnwDPSbpE0qAGyxsOvF/SPZImSdoiH18VmF44bzqwWpXjM/Lx\n",
-       "EELo0yS2k/gD8Evg96TEcb7Nv0sObZ72GtFPAxYFhtl+A0DSYOBC4PT800h5y9neRtKWwDXAWg1c\n",
-       "pypJ4wq7k2xP6q5rhxBCT5DYkfT5ujbwNWBvm7e67/oaBYzqjmu1l0D2A7ayPe82yfYbko4j1b81\n",
-       "kkCmA9fla/1F0lxJK5DuLIYVzhuaz52Rt4vHZ9S6uO1xDcQUQgilkhCwM3AGqZblbOBKmzndXVb+\n",
-       "Yj1pftk6s9FrtdcG8k4xeRQKfxOY22B5N5DeJCStCwyy/XfgRuDjkgZJWpNU1TXZ9kzgdUlb50b1\n",
-       "Q/M1Qgih15OQxB7AXaQxHD8B1re5pBnJo7u1Ow5E0pBqhwF3dGFJ44EdgeUlvUDKrBcDF+euvW8B\n",
-       "hwHYnirpGmAq8DYw2nZbGaOBS4ElgN/Z/kMdryuEEFpWvuPYk1STsyTwVeBam3dKDayTNP9zuuIB\n",
-       "aRrtJArbazYppoZIsm11fGYIIZRDYgCp1+nppBqgs4Dr7YZrdbohpsY/O2smkN4mEkgIoVVJDAQ+\n",
-       "Skoc/wO+Atxkd1yb02xd+eysWYUlabP2nmj7gUYKDCGE/kJiEdIg6VOB14GTgd+3QuLoDu1VYU2i\n",
-       "/SqsnZoUU0PiDiSE0CokFgU+QUocs0h3HLe0YuKIKiwigYQQyicxiNQ56BTSIOyvALe3YuJo05Qq\n",
-       "rBBCCPWRWAw4ChhDWjr2MJs7y42q+SKBhBBCgySWAP6P1LbxMHCgzT3lRtVzIoGEEEInSSwFfAr4\n",
-       "IjAZ2Mfm/nKj6nn1zMY7QNKhks7I+++RtFXzQwshhNYiMVjiZOCvwLbAB2327Y/JA+pbD+RC0hv1\n",
-       "ibz/Zj4WQgj9gsQyEqeSEsemwK42+9s8XHJopaqnCmtr2yMlPQhg+1VJizY5rhBCKJ3EcsCJwPHA\n",
-       "74D32zxRblSto547kLckDWzbkbQijU+mGEIILU9iBYmzSYvbDQO2sTkskseC6kkgFwDXA++W9DXS\n",
-       "rJFfb2pUIYRQAol3S5wDPAWsAGxhc7TNMyWH1pLqGkgoaQNgl7x7q+3HmxpVA2IgYQihURKrACcB\n",
-       "RwBXA+faPF9qUD2kK5+d9dyBQJpueGA+f4lGCgohhFYjMVTiAuAx0ufbRjbH95fk0VX1dOM9g7Qe\n",
-       "xxDSLd0lkhpZjTCEEFqCxOoSFwGPAP8FRth81q694mlYWIdVWJKeAja2/d+8vwTwsO11eyC+ukUV\n",
-       "VgihIxJrA2OBjwA/Ar5j80q5UZWr2VVYM1iw2mpx0nrlHQV1saRZefXByse+kNdDH1I4NlbS05Ke\n",
-       "kLR74fjmkqbkx86vI94QQliAxLoSlwH3Ai8Cw21O6e/Jo6tqJhBJF0i6APgn8JikSyVdCjyaj3Xk\n",
-       "EmCPKtcdBuwGPFc4NoI0Z/6I/JwL8xroABcBR9seDgyXtNA1QwihGokREleReo8+A6xjc4bNqyWH\n",
-       "1ie0N5DwftJ6IPcDNxSOT6KONdFt3yFpjSoPfRv4EvDrwrF9gPG25wDTJD0DbC3pOWCw7cn5vMuB\n",
-       "fYFYFz2EUJPExsBpwI7Ad4DjbF4vN6q+p2YCsX1pdxcmaR9guu1H5t9gALAqLDCD5XRgNWAOC1aX\n",
-       "zcjHQwhhIRKbkZaN3QY4DzjK5s1yo+q7OpzKRNKzVQ7b9lqdKUjSkqRFVnYrHu7MNeooY1xhd5Lt\n",
-       "Sd15/RBCa5LYipQ4NgPOBQ62+Xe5UbUmSaOAUd1xrXrmwtqysL048DFg+QbKWhtYA3g4330MBe6X\n",
-       "tDXpzmJY4dyhpDuPGXm7eLxmNzvb4xqIK4TQS0lsB5xBaj/9BrC/zX/Ljaq15S/Wk9r2JZ3Z6LU6\n",
-       "7IVl+++Fn+m2vwt8uLMF2Z5ieyXba9pek5QgNrM9C7gR+LikQZLWBIYDk23PBF6XtHVuVD+UBdtj\n",
-       "Qgj9kMSOErcCVwHXkXpVXRjJo2fVU4W1OfMbzQcAW5BGpXf0vPGkBqzlJb0AnGH7ksIp8xribU+V\n",
-       "dA0wFXgbGO35A1RGkwYyLgH8znY0oIfQD0kI2Jl0x7EacDZwpc2cUgPrx+oZSDiJ+R/2b5MWiv+W\n",
-       "7SebGlknxUDCEPqmnDg+QEocQ4CvAj+3ebvUwPqIrnx21pNA1rL9t4pja9qu1rhemkggIfQtOXHs\n",
-       "SUocSwJnAdfavFNqYH1MsxPIA7Y3qzh2v+3NGymwWSKBhNA3SAwgjfc6jVRd/hXgejvWIWqGrnx2\n",
-       "1mwDyVO4jwCWlbQfqcutgXeRemOFEEK3kRgIfJTUHfd/wJeBmyJxtK72GtHXBfYClsn/tnkD+GQz\n",
-       "gwoh9B8Si5CmMjqNNE3SycDv7Y5nvAjlqqcKazvbd/dQPA2LKqwQeheJRYFPAKcCs0hVVbdE4uhZ\n",
-       "TW0D6S0igYTQO0gMAg4jzUwxjZQ4bo/EUY6mtIGEEEJ3klgMOAoYAzwJHG5zR7lRha6IBBJCaCqJ\n",
-       "xUntpicDDwMH2gtMnhp6qXqWtF1Z0s8k/SHvj5B0dPNDCyH0ZhIDJY4k3W3sDuxr8+FIHn1HPSsS\n",
-       "XgpMIE25DvA08LlmBRRC6N0kJLEvab3xI4GDbPayua/k0EI3qyeBrGD7F5BGf+ZFn2IKgRDCQiR2\n",
-       "BO4mjeE4CdjRpuV7cYbG1NMG8qakedO3S9qG+pa0DSH0ExKbAl8DNiANBLw6BgD2ffUkkC8ANwFr\n",
-       "SbobWJG0JkgIoZ+TWIs0R9UupNlx97V5q9yoQk+paxyIpEWB9fLuk7kaq6XEOJAQeo7ESqQ7jYOA\n",
-       "84Hv2LxRblShET0xDmQr0mqCiwCbScL25Y0UGELovSSWAb5IWqfncmB9m1fKjSqUpZ4Fpa4E1gIe\n",
-       "ggWmUY4EEkI/kcdyjCbPUwVsZvNcuVGFstVzB7I5MMKdnPNE0sWkpW9ftr1RPvZN0vz+bwF/BY60\n",
-       "/c/82FjSKNV3gBNsT8jHNyd1JV6ctCLhiZ2JI4TQuDxD7mHAONKXyF1sHi01qNAy6unG+yiwSgPX\n",
-       "vgTYo+LYBGBD25sATwFjIQ1OJM3GOSI/58K8BjrARcDRtocDwyVVXjOE0M1qjOXYJ5JHKGpvPZCb\n",
-       "8ubSwFRJk0lz9APY9t7tXdj2HZLWqDg2sbB7L2nuf4B9gPG5cX6apGeArSU9Bwy2PTmfdzlpoZlY\n",
-       "Fz2EJsljOb5BWgXwJGJq9VBDe1VY5+V/TVpMqqg7/piOAsbn7VVhgekNpgOrAXPydpsZ+XgIoZvF\n",
-       "WI7QWTUTiO1JAJLOtf2l4mOSzgFub7RQSacCb9m+utFr1LjuuMLupLbXEEKoLcZy9C+SRgGjuuNa\n",
-       "9TSi71bl2IdIvTE6TdIR+fm7FA7PAIYV9oeS7jxm5O3i8Rm1rm17XCMxhdAfVRnLcWyM5ej78hfr\n",
-       "SW37ks5s9Fo1G9ElHSdpCrCepCmFn2mkhrVOyw3gJwH72P5v4aEbgY9LGiRpTWA4MNn2TOB1SVvn\n",
-       "RvVDgRsaKTuEkEgsI3EWMJVUTby+zVcieYTOau8O5GpSf+9vkO422tpB3rA9u6MLSxoP7AisIOkF\n",
-       "4ExSr6tBwMTcyerPtkfbnirpGtIf9NvA6EK34dGkbrxLkLrxRgN6CA2IsRyhu8WStiH0cVXGcpwa\n",
-       "3XFDm1jSNoSwEAmRusifDcwmjeWIqdVDt4kEEkIfFGM5Qk+oK4FIWhnYkjT+Y7Ltl5saVQihITGW\n",
-       "I/SketZEP4A0anx/4ABgsqT9mx1YCKF+EmtJXEWapeH3wHo2V0byCM3UYSO6pEeAXdvuOiStCNxq\n",
-       "e+MeiK9u0Yge+qNYlyN0VVc+O+uZTFGwwHz/s1l4apMQQg+KsRyhFdTTBvIH4GZJV5MSx4GkW+QQ\n",
-       "Qg+LsRyhldS7pO1Hge3z7h22r29qVA2IKqzQl8VYjtAsXfnsrKcN5BzbJ3d0rGyRQEJfVGUsx5gY\n",
-       "yxG6U7MTyIO2R1Ycm9K2ymCriAQS+pqKsRxjibEcoQmaMhJd0nGkuta186SKbQYDdzVSWAihYzGW\n",
-       "I/QWNe9AJC0DLEeDkyn2tLgDCb1dlXU5fhTrcoRma2oVVm8RCST0VjGWI5Sp2eNAQghNEGM5Qm8X\n",
-       "CSSEHiaxuMTngadIK3FuZvM5e4EBuyG0vKYlEEkXS5pVbICXNETSRElPSZogadnCY2MlPS3pCUm7\n",
-       "F45vnldCfFrS+c2KN4RmkxgocSTwJGmxtV1sjoiBgKG3am9J2zclvVHj5/U6rn0JsEfFsTHARNvr\n",
-       "ArfmfSSNII1wH5Gfc2FewhbgIuBo28OB4XlZ3BB6DQlJ7EtaCvpI0roc+8RAwNDb1ezGa3tpAElf\n",
-       "BV4ErswPHQys2tGFbd8haY2Kw3uTvnkBXEZa2H0MaaDUeNtzgGmSngG2lvQcMNj25Pycy4F9SdOr\n",
-       "hNDyYl2O0JfVMxfW3hUz716UZ+g9vYHyVrI9K2/PAlbK26sC9xTOmw6sRmpYnF44PiMfD6GlxViO\n",
-       "0B/U0wbyL0mHSBqYfw4G3uxqwU79h+ObWOhTYl2O0J/UcwfyCVLf9O/m/bvysUbMkrSy7ZmSVgHa\n",
-       "VjacQeqN0mYo6c5jRt4uHp9R6+KSxhV2J9me1GCcIXRKlbEcx0Z33NCKJI0CRnXLtZo5kDC3gdzU\n",
-       "Nm+WpHOB2bbPkTQGWNb2mNyIfjWwFamK6hZgHduWdC9wAjAZ+C3wPdsLtYHEQMJQBollgC+Spv25\n",
-       "HPhadMcNvUlTBxJKWk/SrZIey/sbSzqtjueNB+4G1pP0gqQjSY2Ju0l6Ctg572N7KnANaUDV74HR\n",
-       "np/ZRgM/BZ4GnqmWPELoaTGWI4T6ZuP9E6n3yA9tj8zdax+1vWFPBFivuAMJPSHW5Qh9TVNm4y1Y\n",
-       "0va9bcMycrXSnEYKC6G3qrIux0GxLkfo7+pJIK9IWqdtR9LHgJeaF1IIrSXGcoRQXT1VWGsDPwa2\n",
-       "BV4DngUOtj2t6dF1QlRhhe4WYzlCf9C0KixJA4HjbO8iaWlggO16pjEJodeSWBn4JrAbqcpq31iX\n",
-       "I4SFtdsLy/Y7wA5KKerNSB6hL5MYIPEpYAppvNFwmwsieYRQXT1tIA8Bv5Z0LfDvfMy2r2teWCH0\n",
-       "LIkNgR+RvlTtbDOlg6eE0O/Vk0AWI/U62bnieCSQ0OtJLAGcBhwDnEFaRjbaOUKoQz1tIK/a/kIP\n",
-       "xRNCj5HYlbRcwIPAJjYvlhxSCL1KuwnE9juSts9tINFtMfQJEisC3wbeBxxv85uSQwqhV4o2kNBv\n",
-       "5MGAR5DGdFwBvNfu+szSIfRX9SSQxYFXiTaQ0ItJrEdqJF8K2MPmwZJDCqHXa+psvD0pBhKGaiQW\n",
-       "I616+RngLOD7Nu+UG1UIraMlZ+MNoWx5CpKHgc2AkTbnR/IIofvUsyLhT4BTYN5gqimkRXNCaEkS\n",
-       "QyR+BlwJjLXZx+aFsuMKoa+pJ4Esafvetp3cGytm4w0tR0ISh5DWlfkXsKHN9SWHFUKfFbPxhj5B\n",
-       "Ym3SmI53A3vbTC45pBD6vHruQI4n9V5ZT9KLwOeA47pSqKSxkh6TNEXS1ZIWkzRE0kRJT0maIGnZ\n",
-       "ivOflvSEpN27UnboWyQGSYwF7gUmAltG8gihZ9RMIJJOzJur2N6F9M1ufdvbd2Uq97xO+ieBzfJa\n",
-       "6QOBj5N6yky0vS5wa94nr5d+IDAC2AO4UFI9iS/0cRLbAfeTBgRuYfNNO6pXQ+gp7X0QH5X/vQCg\n",
-       "G2fjfZ3UhrKkpEVIi/S8COwNXJbPuQzYN2/vA4y3PScnrmeArbohjtBLSSwrcRHwS1LX3A/bTCs3\n",
-       "qhD6n/baQKZKehpYTVLlzKS2vXEjBdp+VdJ5wPPAf4CbbU+UtJLtWfm0WcBKeXtV4J7CJaYDqzVS\n",
-       "dujd8kjy/YHvADcBI2xeKzeqEPqvmgnE9kGSVgYmAHsB3TJIL69w+FlgDeCfwLWSDqko25LaG+HY\n",
-       "N0Y/hrpJrAH8gPR3c4DNXaUGFELocDLFmcDGkpYA3mP7yW4ocwvgbtuzASRdR1oud6aklW3PlLQK\n",
-       "8HI+fwYwrPD8ofnYQiSNK+xOsj2pG+INJZJYhPSFYwxpAsSPxAJPITRO0ihgVLdcq4410fcmLe+5\n",
-       "mO01JI0Evmx774YKlDYBrgK2BP4LXApMBlYHZts+R9IYYFnbY3Ij+tWkdo/VgFuAdSpnB46pTPoe\n",
-       "iS2BH5PWoznW5pmSQwqhz2namujZOGBr4DYA2w9KWquRwvLzH5Z0OXAfMBd4gPQhMRi4RtLRwDTg\n",
-       "gHz+VEnXkAaHvQ2Mjqnl+zaJwaS1yA8AvghcZUe1ZQitpp47kHttby3pQdsj87FHGm1Eb5a4A+kb\n",
-       "JPYl9fybCJxkM7vkkELo05p9B/KYpIOBRSQNB04A7m6ksBBqkRhKShwjgENtJpUbUQihI/WORN8Q\n",
-       "+B8wnjSO47PNDCr0HxIDJU4gLVz2MLBxJI8Qeod2q7DyQL+JtnfquZAaE1VYvY/ESFL7179IjeRP\n",
-       "lBxSCP1O09YDsf02MLc4L1UIXSWxlMS3gJtJEyDuFMkjhN6nnjaQfwFTJE3M25DG+p3QvLBCXyXx\n",
-       "IeBC4E7SmuQvd/CUEEKLqieBXJd/2uq6RIwED50ksQpwPml1wE/aTCw5pBBCF8Wa6KGpJAYAx5Am\n",
-       "Pfwx8FWb/5QbVQihTbO78YbQEIn3kpKGSe0cj5YcUgihG8W6GqHbSSwh8TXS7AWXAe+L5BFC39Pe\n",
-       "glJX5H9jzEeom8RuwBRgbdKYjh/ZzC05rBBCE9RsA5E0FdgV+ANVZm60/WpTI+ukaAMpl8S7SbPl\n",
-       "7gCMtvldySGFEOrQrDaQH5KWll2LtGxokfPx0M/lRZ6OAr5Oqq7a0J7X3TuE0IfVM5niD20f20Px\n",
-       "NCzuQHqexPrAj4AlgGNsHio5pBBCJ3Xls7OubrySBpKWmJ13x2L7+UYKbJZIID1HYnFgLPBp4MvA\n",
-       "hTbvlBtVCKERTe3GK+kzwJmkFQKLHxIbNVJg6N0kRpHuOqYCm9pMLzeiEEJZ6qnC+iuwVdsStK0q\n",
-       "7kCaS2J50sqUuwGfsbmh5JBCCN2gaZMpZs+TpnDvNpKWlfRLSY9Lmippa0lDJE2U9JSkCcUJHCWN\n",
-       "lfS0pCck7d6dsYT2SUjiUOAx4A1gRCSPEAK03433C3lzBLA+8BvgrXzMtr/dcKHSZcDtti/OU8Yv\n",
-       "BZwK/N32uZJOBparWBN9S+avib6u7bkV14w7kG4msQ6pN97ypEbyv5QcUgihmzXrDmQwsDTpDmQi\n",
-       "MCjvL50KByWiAAAY60lEQVQfa4ikZYD32b4Y0pTxtv8J7E3qBkr+d9+8vQ8w3vYc29OAZ4CtGi0/\n",
-       "dExikMSpwD3A74EtI3mEECrVbES3Pa5JZa4JvCLpEmAT0hiTzwIr2Z6Vz5lF6vUFsCrpg6zNdNKd\n",
-       "SGgCie1JjeTPAVvYTCs3ohBCqypjMsVFSFN6H2/7L5K+C4wpnmDbktpr3a/6mKRxhd1Jtid1MdZ+\n",
-       "Q2I54BvAnqSE/ks7pu0Poa+RNIoqs4s0oowEMh2YbrutSuSXpDEFMyWtbHumpFVg3kJDM4BhhecP\n",
-       "zccW0sS7pj4rjyQ/APgOcANpJPlr5UYVQmiW/MV6Utu+pDMbvVaHvbAk7VDl2PaNFmh7JvCCpHXz\n",
-       "oV1JPXxuAg7Pxw6HeT19bgQ+LmmQpDWB4cDkRssP80msCfwOOA34qM3oSB4hhHrVMw7kQdsjOzrW\n",
-       "qUKlTYCfkhrm/wocCQwErgHeA0wDDrD9Wj7/FNJ8S28DJ9q+uco1oxdWnSQWJVVTnQycB3zLZk65\n",
-       "UYUQytCUqUwkbQtsB3yONMtqWwGDgY/Y3qSRApslEkh9JLYiLfL0MnCczV9LDimEUKJmTWUyiJQs\n",
-       "BrJgt93XgY81Ulgoj8S7gLNJv7svAldHI3kIoSvqqcJaI4+/aGlxB1JdbiT/CPA90touX7JpqbVc\n",
-       "Qgjlafaa6ItJ+gmwRuF82965kQJDz5EYBnwfWA/4hM2fSg4phNCH1JNArgUuIjV6t83GG1UfLUxi\n",
-       "IHA8cDpwAXCAzf/KjSqE0NfUk0Dm2L6o6ZGEbiGxGamR/A1ge5snSw4phNBH1TMb702SPi1plTxj\n",
-       "7hBJQ5oeWegUiaUlziPNXfV9YOdIHiGEZqqnEX0aVaqsbK/ZpJga0p8b0SX2BH4A3A58weaVkkMK\n",
-       "IfQSTV/StjfojwlEYlXgfGAkcKzNLSWHFELoZZq6oJSkpSSdnntiIWm4pD0bKSx0D4kBEqOBh4En\n",
-       "gY0ieYQQelo9jeiXkKZc3y7vv0iaAPE3zQoq1CaxEamRfC4wyuaxkkMKIfRT9TSir237HPJqhLb/\n",
-       "1dyQQjUSS0p8A/gjKam/L5JHCKFM9SSQ/0laom1H0toQYwp6ksQHgCmkwZwb2fzYZm77zwohhOaq\n",
-       "pwprHGkKjKGSrga2B45oYkwhk1iJtE7HtsBom9+XHFIIIcxTVy8sSSsA2+Tde2z/valRNaAv9cKS\n",
-       "GECavv5rwKXAl22i6jCE0O2aNZ37BrYfl7Q5aRxIWwEGsP1AIwU2S19JIBIbkNYkXww4xubhkkMK\n",
-       "IfRhzUogP7H9SUmTqD6QcKdGCmyW3p5AJBYHTgFGk6oNL7LnzT0WQghN0SsHEkoaCNxHWh99rzw9\n",
-       "yi+A1Vl4RcKxpCqdd4ATbE+ocr1em0AkdiLddTwKfMauvuZ7CCF0t2YPJPy0pOUK+8tJGt1IYRVO\n",
-       "BKYy/+5mDDDR9rrArXkfSSOAA4ERwB7AhZLq6T3W8iRWkLgUuAw4yWa/SB4hhN6ing/iY2z/o20n\n",
-       "bx/TlUIlDQU+RJoivi3z7U36ICX/u2/e3gcYb3tOXtjqGWCrrpRfNglJHEa643gN2NDm1yWHFUII\n",
-       "nVJPN94BkgbYngvzqp4W7WK53wFOAt5VOLaS7Vl5exawUt5eFbincN50YLUull8aieHAD4HlgD1t\n",
-       "7is5pBBCaEg9CeRm4OeSfkS6W/gUaVxIQ/I8Wi/bflDSqGrn2Lak9hpnqj4maVxhd5LtSY3G2d0k\n",
-       "BgFfAj5LWpv8Apu3y40qhNDf5M/dUd1xrXoSyMmkKqvj8v5EUtVTo7YD9pb0IWBx4F2SrgBmSVrZ\n",
-       "9kxJqwAv5/NnAMMKzx+ajy3E9rguxNU0EjuQ5q/6K7C5zXMlhxRC6KfyF+tJbfuSzmz0WqVO5y5p\n",
-       "R+CLuRfWucBs2+dIGgMsa3tMbkS/mtTusRpwC7COKwJvxV5YEssB5wAfJnUa+JUdywGHEFpHVz47\n",
-       "a96BSLrW9v6SHmXhKiPb3riRAqtou/Y3gGskHU3uxpsLmirpGlKPrbeB0ZXJoxVJfBD4GXA9MMLm\n",
-       "nyWHFEII3aq9gYSr2n5R0urM7yk1T+4R1TJa6Q4k97A6F9jf5o6y4wkhhFqaNRL9AdubSbrC9qFd\n",
-       "irAHtEoCkfg8qaH8AzaPlx1PCCG0pylVWMBikg4Gtpe0Hwvehdj2dY0U2FdJiNS76iPADjbPlxxS\n",
-       "CCE0VXsJ5FjgYGAZYK8qj0cCySQGAhcBm5IWemq52YpDCKG7tZdAVrZ9bK7K+nGPRdTL5EkQryIl\n",
-       "2l1s3ig5pBBC6BHtTWVySv73uHbO6dckBgO/Ja1P/uFIHiGE/qS9O5DZkiYCa0q6qeIx2967iXG1\n",
-       "PIkVgd+TZhT+dEy9HkLob9pLIB8CNgOuBL5FRSN6M4NqdRLvIY3IvxY4PQYHhhD6ow5Hokta0fYr\n",
-       "kpay3bLLqvZUN16JEaS5wL5t891mlxdCCM3U1PVAgOGSpgJP5MI2lXRhI4X1dhJbA38ETo3kEULo\n",
-       "7+pJIN8lLeT0dwDbDwE7NjOoViSxO/Ab4GibK8qOJ4QQylbXyn62KwfF9atpyCUOBK4APmLz27Lj\n",
-       "CSGEVlDPdO7PS9oeQNIg4AToP1N0SIwGTgV2s3mk7HhCCKFV1NWIDpwP7ErqiTUBOMH27OaHV7/u\n",
-       "bkTPU5OcDhwG7G7zt+66dgghtIqmTKbY23RnApEYQEqa7wP2sJnZHdcNIYRW09ReWJKGSbpe0iv5\n",
-       "51eShjZSWG+Ql569EtgEGBXJI4QQqqunEf0S4EZg1fxzUz7W50gsBfwaWJo0HftrJYcUQggtq54E\n",
-       "sqLtS2zPyT+XAu9utMB8R3ObpMckPSrphHx8iKSJkp6SNEHSsoXnjJX0tKQnJO3eaNntx8UQ0ujy\n",
-       "WcB+Nv9pRjkhhNBX1JNAZks6VNJASYtIOgS6NF35HOBztjcEtgE+LWkDYAww0fa6wK15n7wm+oHA\n",
-       "CNJ4lAsl1dX9uF4SqwF/Au4GjrL7VzflEEJoRD0fxEeR1iefCbwE7A8c2WiBtmfmwYjYfpPUJXg1\n",
-       "YG/gsnzaZcC+eXsfYHy++5kGPANs1Wj5lSSGA3eSxnmcZDO3u64dQgh9WYfjQPKHdrUFpbpM0hrA\n",
-       "SOBeYCXbs/JDs4CV8vaqwD2Fp00nJZxuKJ/NSKPLz7D5aXdcM4QQ+osOE4iky0njPl7L+8sB59k+\n",
-       "qisFS1oa+BVwou03pPm9yGxbUnv9i6s+JmlcYXeS7Um1y2dz0nTsx9qxumIIoX+QNAoY1R3Xqmck\n",
-       "+sZtyQPA9j8kbdaVQiUtSkoeV9i+IR+eJWll2zMlrQK8nI/PAIYVnj40H1uI7XH1lc9g4BfAZyJ5\n",
-       "hBD6k/zFelLbvqQzG71WPW0gkjSksDMEGNhogUq3Gj8Dptouzmh7I3B43j4cuKFw/OOSBklaExgO\n",
-       "TG60/OwHwG02v+jidUIIod+q5w7kPODPkq4hTWWyP3B2F8rcHjgEeETSg/nYWOAbwDWSjgamkRru\n",
-       "sT01lz2VNInjaHdh+LzEocCWwBYNv4IQQgj1TWUiaUNgZ1Lbwx9tT212YJ1Vz3B8iXWAPwO72jzc\n",
-       "M5GFEELrirmw6PhNyFOU3AlcYXNBz0UWQgitq9krEvYVZ5G6B3+/7EBCCKEvqKcNpNfLqwkeDIy0\n",
-       "q3cBDiGE0Dl9PoFIvJs0+eNhNq+UHU8IIfQVfboKK6/rcSlwmc2tJYcTQgh9Sp9OIMBngCFAwwNl\n",
-       "QgghVNdne2FJLAP8FdjO5qnyIgshhNYVvbCqOw74QySPEEJojj55ByKxJPA30oDBR8uNLIQQWlfc\n",
-       "gSzsaOCeSB4hhNA8fe4OJI84fwb4mN3lSRdDCKFPizuQBR0MPBnJI4QQmqtPDSSUGEhaS/3YsmMJ\n",
-       "IYS+rq/dgewHvEphsZQQQgjN0dcSyKnA2THfVQghNF+vSSCS9pD0hKSnJZ1c47T/Ar/tybhCCKG/\n",
-       "6hUJRNJA0jTsewAjgIMkbVDl1O1a6e4jL17fUiKm+rViXBFTfSKmntErEgiwFfCM7Wm25wA/B/ap\n",
-       "PMlmbo9H1r5RZQdQxaiyA6hiVNkB1DCq7ACqGFV2AFWMKjuAKkaVHUAVo8oOoLv1lgSyGvBCYX96\n",
-       "PhZCCKEkvSWBtEy1VAghhKRXjESXtA0wzvYeeX8sMNf2OYVzWv+FhBBCC2p0JHpvSSCLAE8CuwAv\n",
-       "ApOBg2w/XmpgIYTQj/WKkei235Z0PHAzMBD4WSSPEEIoV6+4AwkhhNB6eksjek11DjBsRrkXS5ol\n",
-       "aUrh2BBJEyU9JWmCpGULj43NMT4hafcmxTRM0m2SHpP0qKQTWiSuxSXdK+khSVMlfb0V4srlDJT0\n",
-       "oKSbWiEmSdMkPZJjmtwiMS0r6ZeSHs+/v63LjEnSevn9afv5p6QTyn6fCuU8JmmKpKslLVZ2XJJO\n",
-       "zPE8KunEfKx7YrLda39I1VnPAGsAiwIPARv0UNnvA0YCUwrHzgW+lLdPBr6Rt0fk2BbNsT4DDGhC\n",
-       "TCsDm+btpUntRhuUHVcua8n87yLAPcAOLRLX54GrgBtb5Hf4LDCk4ljZMV0GHFX4/S1TdkyF2AYA\n",
-       "LwHDyo4pX/tvwGJ5/xfA4WXGBbwXmAIsTvq8nAis3V0xNeWX2lM/wLbAHwr7Y4AxPVj+GiyYQJ4A\n",
-       "VsrbKwNP5O2xwMmF8/4AbNMD8d0A7NpKcQFLAn8BNiw7LmAocAuwE3BTK/wOSQlk+YpjpcVEShZ/\n",
-       "q3K8Jf6mgN2BO1ohJmAI6UvbcqREexOwW8m/v48BPy3snwZ8qbti6u1VWK02wHAl27Py9ixgpby9\n",
-       "Kim2Nk2PU9IapDuke1shLkkDJD2Uy7/N9mMtENd3gJNggRkMyo7JwC2S7pP0yRaIaU3gFUmXSHpA\n",
-       "0k8kLVVyTEUfB8bn7VJjsv0qcB7wPKm36Gu2J5Yc16PA+3KV1ZLAh0hfnLolpt6eQFq2B4BT+m4v\n",
-       "vqbFLmlp4FfAibbfaIW4bM+1vSnpj/f9knYqMy5JewIv234QqNoHvqT3anvbI4EPAp+W9L6SY1oE\n",
-       "2Ay40PZmwL9Id/plxgSApEHAXsC1CxVYQkyS1gY+S6qZWBVYWtIhZcZl+wngHGAC8HtS9dQ73RVT\n",
-       "b08gM0h1n22GsWD27GmzJK0MIGkV4OV8vDLOoflYt5O0KCl5XGH7hlaJq43tf5JmTN685Li2A/aW\n",
-       "9CzpG+zOkq4oOSZsv5T/fQW4njQPXJkxTQem2/5L3v8lKaHMbIG/qQ8C9+f3Csr/O98CuNv2bNtv\n",
-       "A9eRqtlLfa9sX2x7C9s7Av8AnqKb3qvenkDuA4ZLWiN/GzkQuLHEeG4kNZqR/72hcPzjkgZJWhMY\n",
-       "Dt2/5K4kAT8Dptr+bgvFtUJbLw9JS5DqhR8sMy7bp9geZntNUjXIH20fWmZMkpaUNDhvL0Wq359S\n",
-       "Zky2ZwIvSFo3H9oVeIxUv1/a31R2EPOrr9rKLjOmJ4BtJC2R/y/uCkyl5PdK0rvzv+8hLbp3Nd31\n",
-       "XnV3Q1JP/5C+hTxJ6i0wtgfLHU+q53yL1A5zJKkR7RZShp8ALFs4/5Qc4xPAB5oU0w6k+vyHSB/Q\n",
-       "D5KmwC87ro2AB3JcjwAn5eOlxlUoa0fm98IqLSZSe8ND+efRtr/nst8nYBNSx4eHSd+ql2mBmJYC\n",
-       "/g4MLhwr/e+J1ED9GCnxX0bqzVT2e/WnHNNDwE7d+V7FQMIQQggN6e1VWCGEEEoSCSSEEEJDIoGE\n",
-       "EEJoSCSQEEIIDYkEEkIIoSGRQEIIITQkEkgLywMkp3R8Zl3X2lHStp19rDtJWl9pSvf7Ja3V7PI6\n",
-       "iOUEpanJr8iDpm7Jcz0dkOd72qCd5+6lBpcOkLSMpOM6+1gH1yy+lk7HJukdpWnR23432+bjq0s6\n",
-       "qBPXGSPpE3n7eElH5O0Ffu/VrinpzPaOSdotzw/2SP53p8Jjt7YNwKx1PaVp1W9XmpNtlPL0/XW8\n",
-       "pm9XTicT5otxIC1MaULEm2xv1A3XGge8Yfu8Tj420PY7lccbjGEMMND22Z14zgDbczs+s9OxPA7s\n",
-       "YvtFSdsAZ9nerbvLqVLuGtT4nTb6+y6+lgZjesN22wj43YFTbI+SNAr4gu296rzOH4H9gVdJA0e3\n",
-       "dFpNdN7vvfKaks4mTfi5G2kQ7MXAAVWOCZhpe6akDYGbbQ/N1/gkaUDhtyUdDKwCLJ/jeNH2VZKO\n",
-       "Is1y/M16X5ekAaSpz8+zvXc970G/06wRmfHTLSNI1yBNhfBj0sjkm4HF82NrkyZHu4800nS9fHwv\n",
-       "0nobD5Dm/n93vs5LpHmNHgR2qCij7bEHSKPZLwV+mK/zLWBL4O78+F3Auvm5R5BGJv+eNKL1nHx8\n",
-       "YL7GFNLI88+SZgxoK+fWfN4hpA+KB3N5A/LxN3O5DwHbVbwn65BG0D4E3A+smY9/s1DeAYXzTyJN\n",
-       "xfAwMC4f+yHwv3zul4Cngdfy61sLmARsns/dI5fzEDCx8LovyNsrkuaHmpx/tsvHx5E++G4D/gp8\n",
-       "Jh//OfDv/JrPqXhtCz1W63UVnlN8LZ+tiO1S4Pz8O/sr8NEaf2dvFLb3B67L2/fk9+XBfO3D266d\n",
-       "H/8NsGPefhdwZ97eARiftz9U+L3/Efhz4Zon5nMuIn3YDy9ce6FjhccEzAYWzfsrAZMLjx8EvF3x\n",
-       "dzCR+X+3o/Lv5VrgceDKwnnTgG/k3/kB+dgjFEZqx0/hd1F2APHTzi8nfbjPATbO+78ADs7btwLr\n",
-       "5O2tmf+hXJyS4P+Ab+XtM4HP1yhngceAS0hz4rTdoQ4mfYOENL/PL/P2EfmDaTCwWP7PN5Q0UeKE\n",
-       "wvXeVVkOaaGrGwvXvRA4NG/PBT5WI9Z7gX3y9iBgCeCjpOkYREqYz5HWONgd+FE+dwDpA+99ef9Z\n",
-       "8sJNpKlMbiqUcRtpwsAVSVNzr158byl8kJLmFdo+b7+HNA8ZpARyJ2kqi+VJ024MBFansIZMxWtb\n",
-       "4LFar6vK84qvpRjbpcAvCu/30zXKfZv0gf446cN9ZI33pTKB3AS8P2/vx/wEPYYF/56Kv/fKa54F\n",
-       "7A18j5TsNq52rCLej1H4+8rH/kZaRO0g4IvA10lfHg7K7/tLhXNH5de5an5v72Z+4n8W+GLFtS8D\n",
-       "Plj250Er/ixCaHXP2n4kb98PrJEn2tsOuDbN2QakD1OAYZKuIX2ADiL9x2pTddryGo9d6/y/B1gW\n",
-       "uFzSOqSpnYt/N7c6TxkvaSr5QxRYS9L3SDPvTqhSzi6kRHNffg1LADPzY++QZhReMMBUz72q7V8D\n",
-       "2H4rH98euDrH+7Kk20l3TTsCu0t6MF9iKdIdzB0dvPa2Y9sAf7L9XC7vtSrn7QpsUPg9DM6/HwO/\n",
-       "tT0HmC3pZdI35c78Dmq9rrrq73MMN+TYH5e0Uo3z/uM0hTy5Ou8K0kp27cVaaQ/SRJ6Q/gburHhc\n",
-       "Ff+S4zo9lzvS9pfz4UeqHCMf25B0h1BZ3TgLGGZ7fD7vTNvfzNsrAW9UnD/ZucpPaZ2aNUiJBNIX\n",
-       "taIX8+OhQiSQ1ve/wvY7pKUpBwD/aPtPX+EC0l3HbyTtSPom3Ih/F7bPIiWKj0hanVTFUyu+RWy/\n",
-       "JmkT4APAsaQ67aOrlHGZ7VOqHP9vIXnVq9aH3ddt/7iT12pTTwwCtm5LZvMOpoRSPPYOjf1/q3xd\n",
-       "nX1fijF0mBBs36M0e/IKVR5+mwU73ixe2N4S+FRnyqoo98sdHZM0lFRleqjtZytOF4WFwapcrzKe\n",
-       "hf5uC/v/qvLcaCyuInph9T7K3/iflfQxSNO4S9o4P/4u0jcmSFVMbd4gVTVV095jldc8sqP4JC1P\n",
-       "qpq6DjidVB0EC/4nvhX4mKQV85OGKE03XVN+3dMl7ZOfs5jS9PB3AAfmHjYrAu8nVXXdDByV7wiQ\n",
-       "tFpbeXUwqQ3g/blxG0lDqryOCcAJhRe/SQfX7czvodrr6mi677o+uCU9UeP4+qTPhdlV4pkGbJr/\n",
-       "3oaR1ippuyt4opD026oQq+nob61WvMuS7mZPtv3nKqesRO21gP5Oqt5q1Cqk1x4qRAJpfZXffNr2\n",
-       "DwaOzrffj5LqjCHdcVwr6T7glcL5NwEfyd01t6+4ZttjD0jaoUq55wJfl/QAqT7ZhXOqxbcacFuu\n",
-       "OrqC+SvYzTvf9uOk9ZknSHqY9EG8cuG8Wg4FTsjPuYu0NOf1pGqPh0mJ6STbLzstJ3o18GdJj5Aa\n",
-       "Tat9kFR7Hdj+O3AMcF1+n8dXOf8EYAtJD0t6jAW/hVe75mzgLklTJJ3T3mO1XleN+Gu9loW2q9xd\n",
-       "LJH/Lh4kNeQfnpPBw8A7Sl1wT7R9F6mNYCqpbeJ+UsL6IKkjRZs7SYsrVYtxgWtWeS21HE/qOHJm\n",
-       "W6yFLx8rA7NtV945pIJTL8JHJa1XiKUzdxQjSY3/oUJ04w2hn5H0YVLvte930/UmkKqVZuV9kXq0\n",
-       "LVS11wySjgGWsv2dds45gvRl45xa59R43rqkKuHoxltFJJAQQreTNJrUOH9JD5R1K6ln3pvtnDOI\n",
-       "1P17x860r0n6Nqlbc2WngEAkkBBCCA2KNpAQQggNiQQSQgihIZFAQgghNCQSSAghhIZEAgkhhNCQ\n",
-       "SCAhhBAa8v/Onrp6J+51IAAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaadcc88>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "from math import tanh\n",
-    "Af=(20*0.75*12*2)/(144);\n",
-    "Ao=((3.14*1.25)-(20*0.035))*(12/144);\n",
-    "print\"\\t fin surface is : %.1f ft**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  ft**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "Ai=(3.14*1.06*12)/(144);\n",
-    "print\"\\t total inside surface :  ft**2/lin ft \\t\",Ai\n",
-    "print\"\\t fin efficiencies \\t\"\n",
-    "b=0.0625; # ft\n",
-    "hf=4; # from table in solution\n",
-    "m=(5.24*(hf**(1/2))); # m=((hf*P)/(Kax))**(1/2), eq 16.8\n",
-    "n=(tanh(m*b))/(m*b); # efficiency , eq 16.26\n",
-    "print\"\\t hf      m      n \\t \"\n",
-    "print hf   \n",
-    "print m      \n",
-    "print n\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "print\"\\t weighted efficiency curve \\t\"\n",
-    "hfi=((n*Af)+(Ao))*(hf/Ai); # eq 16.34\n",
-    "print\"\\t hf      hfi \\t \"\n",
-    "print hf      \n",
-    "print hfi\n",
-    "# similarly efficiencies values are calculated at different hf values\n",
-    "hf=[4, 16, 36, 100, 400, 625, 900]; # from 2nd table in the solution\n",
-    "hfi=[35.4, 110.8, 193.5, 370, 935, 1295, 1700]; # from 2nd table in the solution\n",
-    "pyplot.plot(hf,hfi)\n",
-    "pyplot.xlabel('heat transfer coefficient to fin,Btu/(ft**2)*(hr)')\n",
-    "pyplot.ylabel('coefficient hf referred to the tube ID')\n",
-    "pyplot.title('weighted fin efficiency curve')\n",
-    "pyplot.show()\t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.2 pgno:525"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t annulus flow area : ft**2 \t0.0391482454167\n",
-      "\t wetted perimeter : ft \t2.76875\n",
-      "\t equivalent diameter : ft \t0.0565572845749\n",
-      "\t heat load : Btu/hr \t270286.4\n",
-      "\t delt1 is : F \t151.0\n",
-      "\t delt2 is : F \t117.0\n",
-      "\t LMTD is  F \t133.427780969\n",
-      "\t Ui : Btu/(hr)*(ft**2)*(F) \t365.652178958\n",
-      "\t hfi : Btu/(hr)*(ft**2)*(F) \t416.40535396\n",
-      "\t jf : \t36.7135894676\n",
-      "\t Ga : lb/(hr)*(ft**2) \t388267.720257\n",
-      "\t Rea : \t11319.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Ts=302.; # F\n",
-    "t1=151.;\n",
-    "t2=185.;\n",
-    "w=15200.; # lb/hr\n",
-    "from math import log10\n",
-    "# The dropwise condensation of steam was promoted with oil.\n",
-    "aa=(3.14*(3.068**2-1.25**2))/(4*144)-((20*0.035*0.75)/(144));\n",
-    "print\"\\t annulus flow area : ft**2 \\t\",aa\n",
-    "p=(3.14*(1.25/12))-(20*0.035/12)+(20*0.75*2/12);\n",
-    "print\"\\t wetted perimeter : ft \\t\",p\n",
-    "De=(4*aa/p);\n",
-    "print\"\\t equivalent diameter : ft \\t\",De\n",
-    "Q=w*0.523*(t2-t1);\n",
-    "print\"\\t heat load : Btu/hr \\t\",Q\n",
-    "delt1=Ts-t1; #F\n",
-    "delt2=Ts-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Ai=0.277; # ft**2/ft\n",
-    "n=20; # number of fins\n",
-    "Ui=(Q/(Ai*n*LMTD));\n",
-    "print\"\\t Ui : Btu/(hr)*(ft**2)*(F) \\t\",Ui\n",
-    "hi=3000; # assumed value for dropwise condensation of steam\n",
-    "hfi=(Ui*hi)/(hi-Ui);\n",
-    "print\"\\t hfi : Btu/(hr)*(ft**2)*(F) \\t\",hfi\n",
-    "hf=120; # from fig 16.7 for hfi=418\n",
-    "mu=1.94; # lb/(ft*hr)\n",
-    "k=0.079;\n",
-    "Z=2.34; # Z=((c*mu)/k)**(1/3)\n",
-    "jf=(hf*De/(Z*k)); # eq 16.36\n",
-    "print\"\\t jf : \\t\",jf\n",
-    "Ga=(w/aa);\n",
-    "print\"\\t Ga : lb/(hr)*(ft**2) \\t\",Ga\n",
-    "Rea=(De*Ga/mu);\n",
-    "print\"\\t Rea : \\t\",round(Rea)\n",
-    "# end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.3 pgno:530"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 12,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for gas oil is :  Btu/hr \t477000.0\n",
-      "\t total heat required for water is :  Btu/hr \t478000.0\n",
-      "\t delt1 is :  F \t120.0\n",
-      "\t delt2 is :  F \t130.0\n",
-      "\t LMTD is :%.0f F \t125.073724087\n",
-      "\t ratio of two local temperature difference is :  \t0.923076923077\n",
-      "\t caloric temperature of hot fluid is :  F \t223.5\n",
-      "\t caloric temperature of cold fluid is :  F \t98.8\n",
-      "\t hot fluid:shell side,gas oil \t\n",
-      "\t flow area is :  ft**2 \t0.0287156933333\n",
-      "\t wetted perimeter :  in \t29.126\n",
-      "\t De :  ft \t0.0473238096546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t626834.943216\n",
-      "\t reynolds number is :  \t4903.1764525\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t97.2026562015\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.01409546\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t847790.707079\n",
-      "\t V is :  fps \t3.76795869813\n",
-      "\t reynolds number is :  \t65199.6985471\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t795.4\n",
-      "\t calculation of tfw \t\n",
-      "\t phya is :  \t0.953986161765\n",
-      "\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t92.729988903\n",
-      "\t Rf :  \t0.0107839978396\n",
-      "\t hf1 :  \t78.2227916919\n",
-      "\t hfi2 :  \t450.563280145\n",
-      "\t Rmetal :  \t0.00170212455807\n",
-      "\t Ri :  \t0.00125722906714\n",
-      "\t hi1 :  \t234.894572087\n",
-      "\t UDi :  \t122.267359744\n",
-      "\t Ai :  ft**2 \t31.2572870644\n",
-      "\t length of pipe required :  lin ft \t74.0694006266\n",
-      "\t Q/Ai1 :  Btu/(hr)*(ft**2) \t14158.7677725\n",
-      "\t annulus film :  \t31.4245931625\n",
-      "\t annulus dirt :  \t4.9162388099\n",
-      "\t Tc-tfw :  \t36.3408319724\n",
-      "\t fin and tube metal :  \t24.0999863376\n",
-      "\t tube side dirt :  \t42.4763033175\n",
-      "\t tubeside film :  \t17.8008143984\n",
-      "\t total temperature drop :  F \t120.717936026\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t3719.56602669\n",
-      "\t delPs is :  psi \t7.7\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t1.6\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=80.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=18000; # lb/hr\n",
-    "w=11950; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for gas oil is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is :%.0f F \\t\",LMTD\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",X\n",
-    "Fc=0.47; # from fig.17\n",
-    "Kc=0.27; \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,gas oil \\t\"\n",
-    "ID=3.068; # in, table 11\n",
-    "OD=1.9; # in, table 11\n",
-    "af=0.0175; # fin cross section,table 10\n",
-    "aa=((3.14*ID**2/(4))-(3.14*OD**2/(4))-(24*af))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "p=(3.14*(OD))-(24*0.035)+(24*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*aa*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=2.5*2.42; # at 224F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jf=18.4; # from fig.16.10\n",
-    "Z=0.25; # Z=k*((c)*(mu1)/k)**(1/3), fig 16\n",
-    "Hf=((jf)*(1/De)*(Z)); # Hf=(hf/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Hf\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "D=0.134; # ft\n",
-    "row=62.5;\n",
-    "at=(3.14*D**2/(4));\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.72*2.42; # at 99F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(970*0.82); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "print\"\\t calculation of tfw \\t\"\n",
-    "# Tc-tfw=40F assumption from fig 14\n",
-    "tfw=184;\n",
-    "mufw=3.5; # cp, at 184F\n",
-    "phya=(2.5/mufw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "hf=(Hf)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct hf to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.002;\n",
-    "Rf=(1/hf);\n",
-    "print\"\\t Rf :  \\t\",Rf\n",
-    "hf1=(1/(Rdo+Rf)); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=255; # fig 16.9\n",
-    "hfi2=(hf1*5.76); # eq 16.38 and fig 16.9,((Af+Ao)/(Ai))=5.76 from previous prblm\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "Rmetal=(hfi2-hfi1)/(hfi2*hfi1)# eq 16.39\n",
-    "print\"\\t Rmetal :  \\t\",Rmetal\n",
-    "phyt=1; # for cooling water\n",
-    "Rdi=0.003;\n",
-    "Ri=(1/hi);\n",
-    "print\"\\t Ri :  \\t\",Ri\n",
-    "hi1=(1/(Rdi+Ri)); # eq 16.40\n",
-    "print\"\\t hi1 :  \\t\",hi1\n",
-    "UDi=(hi1*hfi1)/(hi1+hfi1); # eq 16.41\n",
-    "print\"\\t UDi :  \\t\",UDi\n",
-    "# To obtain the true flux the heat load must be divided by the actual heat-transfer surface.For a 1}2-in. IPS pipe there are 0.422 ft2/lin foot, from table 11\n",
-    "# trial\n",
-    "Ai=(Q/(UDi*LMTD)); # LMTD=delt\n",
-    "print\"\\t Ai :  ft**2 \\t\",Ai\n",
-    "L=(Ai/0.422);\n",
-    "print\"\\t length of pipe required :  lin ft \\t\",L\n",
-    "# Use two 20-ft hairpins = 80 lin ft\n",
-    "Ai1=(80*0.422); # ft**2\n",
-    "r=(Q/Ai1);\n",
-    "print\"\\t Q/Ai1 :  Btu/(hr)*(ft**2) \\t\",r\n",
-    "deltf=(r/hfi2);\n",
-    "deltdo=(r*Rdo/5.76);\n",
-    "print\"\\t annulus film :  \\t\",deltf\n",
-    "print\"\\t annulus dirt :  \\t\",deltdo\n",
-    "d=deltf+deltdo; # d=Tc-tfw\n",
-    "deltmetal=(r*Rmetal);\n",
-    "deltdi=(r*Rdi);\n",
-    "delti=(r/hi);\n",
-    "print\"\\t Tc-tfw :  \\t\",d\n",
-    "print\"\\t fin and tube metal :  \\t\",deltmetal\n",
-    "print\"\\t tube side dirt :  \\t\",deltdi\n",
-    "print\"\\t tubeside film :  \\t\",delti\n",
-    "Td=deltf+deltdo+deltmetal+deltdi+delti;\n",
-    "print\"\\t total temperature drop :  F \\t\",Td\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0359; # ft\n",
-    "Rea1=(De1*Ga/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Rea1\n",
-    "f=0.00036; # fig 16.10\n",
-    "s=0.82; #using fig.6\n",
-    "delPs=((f*(Ga**2)*(80))/(5.22*(10**10)*(De1)*(s)*(phya))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000192; # friction factor for reynolds number 65000, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(80))/(5.22*(10**10)*(0.134)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.4 pgno:535"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 13,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for oxygwn is :  Btu/hr \t1012500.0\n",
-      "\t total heat required for water is :  Btu/hr \t1010000\n",
-      "\t delt1 is :  F \t20\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t66.8818722257\n",
-      "\t R is :  \t7\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.87 \t\n",
-      "\t delt is :  F \t58.1872288364\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t flow area is :  ft**2 \t1.46834418403\n",
-      "\t wetted perimeter :  in \t1570.8\n",
-      "\t De :  ft \t0.0448691882056\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t20431.1770539\n",
-      "\t reynolds number is :  \t16820.7399724\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t20.6536497998\n",
-      "\t hf1 :  \t19.4485963081\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0582118055556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t867521.622428\n",
-      "\t V is :  fps \t3.85565165523\n",
-      "\t reynolds number is :  \t29155.8813311\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t902.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t243.418213207\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t89.6828045249\n",
-      "\t total surface area is :  ft**2 \t229.376\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t75.673831631\n",
-      "\t excess fouling factor :  \t0.00206419817483\n",
-      "\t Rdo :  \t0.0221351170807\n",
-      "\t hf2 :  \t14.1738000666\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t77.1741091592\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t reynolds number :  \t16232.4764484\n",
-      "\t delPs is :  psi \t0.6\n",
-      "\t allowable delPa is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.0\n",
-      "\t allowable delPa is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=100; # outlet cold fluid,F\n",
-    "W=30000; # lb/hr\n",
-    "w=50500; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.225; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oxygwn is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.87 \\t\"# from fig 18\n",
-    "delt=(0.87*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "ID=19.25; # in, table 11\n",
-    "OD=1; # in, table 11\n",
-    "As=((3.14*ID**2/(4))-(70*3.14*OD**2/(4))-(70*20*0.035*0.5))/(144);\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "p=(70*3.14*(OD))-(70*20*0.035)+(70*20*0.5*2);\n",
-    "print\"\\t wetted perimeter :  in \\t\",p\n",
-    "De=(4*As*12/(p));\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.0545; # at 175F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=59.5; # from fig.16.10a\n",
-    "k=0.0175;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "hf=((jH)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.479; # table 10\n",
-    "L=16;\n",
-    "Nt=70;\n",
-    "n=4;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0652; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=1.94; # at 90F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(940*0.96); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi);\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "UDi=((hfi1)*(hi1)/(hi1+hfi1)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A2=0.2048; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UDi1=((Q)/((A)*(delt)));\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi1\n",
-    "Re=(1/UDi1)-(1/UDi);\n",
-    "print\"\\t excess fouling factor :  \\t\",Re\n",
-    "Ro=9.27; #Adding to the outside fouling factor\n",
-    "Rdo1=Rdo+(Re*Ro);\n",
-    "print\"\\t Rdo :  \\t\",Rdo1\n",
-    "hf2=(hf/(1+(hf*Rdo1)));\n",
-    "print\"\\t hf2 :  \\t\",hf2\n",
-    "hfi2=113;\n",
-    "UDi2=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi2\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=0.0433; # ft\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.00025; # fig 16.10\n",
-    "s=0.00133;\n",
-    "delPs=((f*(Gs**2)*(L))/(5.22*(10**10)*(De1)*(s)*(1))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",round(delPs,1)\n",
-    "print\"\\t allowable delPa is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00021; # friction factor for reynolds number 29100, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(0.0625)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 16.5 pgno:556"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 16.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t total heat required for air is :  Btu/hr \t1250000.0\n",
-      "\t total heat required for water is :  Btu/hr \t1248000.0\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t60.0\n",
-      "\t LMTD is : F \t54.9097962457\n",
-      "\t R is :  \t1.25\n",
-      "\t S is :  \t0.4\n",
-      "\t FT is 0.985 \t\n",
-      "\t delt is :  F \t54.086149302\n",
-      "\t caloric temperature of hot fluid is :  F \t225.0\n",
-      "\t caloric temperature of cold fluid is :  F \t170.0\n",
-      "\t fin surface is :  in**2/lin ft \t310.86\n",
-      "\t bare tube surface is :  in**2/lin ft \t27.1296\n",
-      "\t total outside surface :  ft**2/lin ft \t337.9896\n",
-      "\t projected perimeter :  in/ft \t161.28\n",
-      "\t De :  ft \t0.111235119048\n",
-      "\t flow area :  ft**2 \t7.53\n",
-      "\t hot fluid:shell side,oxygen \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t13280.2124834\n",
-      "\t reynolds number is :  \t28408.1926263\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t22.9878748896\n",
-      "\t hf1 :  \t21.5048242607\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.079625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t391836.734694\n",
-      "\t V is :  fps \t1.74149659864\n",
-      "\t reynolds number is :  \t30427.5453198\n",
-      "\t hi :  Btu/(hr)*(ft**2)*(F) \t667.4\n",
-      "\t hi1 :  Btu/(hr)*(ft**2)*(F) \t222.303643994\n",
-      "\t X : \t0.03125\n",
-      "\t hfi2 :  \t212.371237248\n",
-      "\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t108.611980947\n",
-      "\t inside surface per bank is :  ft**2 \t18.312\n",
-      "\t Ai1 :  ft**2 \t212.447090593\n",
-      "\t number of banks :  \t11.6015230774\n",
-      "\t net free volume :  ft**3 \t1.89483559028\n",
-      "\t frictional surface :  ft**2 \t191.88\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 :  ft \t0.0395004292324\n",
-      "\t reynolds number :  \t10087.9633345\n",
-      "\t delPs is :  psi \t0.232069401484\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t0.39\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 16.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=250.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=150.; # inlet cold fluid,F\n",
-    "t2=190.; # outlet cold fluid,F\n",
-    "W=100000; # lb/hr\n",
-    "w=31200; # lb/hr\\\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "C=0.25; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for air is :  Btu/hr \\t\",Q\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.985 \\t\" # from fig 18\n",
-    "delt=(0.985*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=(T2+T1)/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "Af=(3.14*2*8*12*(1.75**2-1**2))/(4);\n",
-    "Ao=((3.14*1*12)-(3.14*1*8*0.035*12));\n",
-    "print\"\\t fin surface is :  in**2/lin ft \\t\",Af\n",
-    "print\"\\t bare tube surface is :  in**2/lin ft \\t\",Ao\n",
-    "A=(Af+Ao);\n",
-    "print\"\\t total outside surface :  ft**2/lin ft \\t\",A\n",
-    "p=(2*3*2*8*12/8)+(((12)-(8*0.035*12))*(2));\n",
-    "print\"\\t projected perimeter :  in/ft \\t\",p\n",
-    "De=(2*A/(3.14*p*12)); # eq 16.104\n",
-    "print\"\\t De :  ft \\t\",De\n",
-    "# 21 tubes may be fit in one :vertical bank (Fig. 16.19b) ,20 tubes in alternating banks for triangular pitch\n",
-    "As=((4**2*12**2)-(21*1*48)-((21)*(2*0.035*3*8*48/8)))/(144); # fig 16.19\n",
-    "print\"\\t flow area :  ft**2 \\t\",As\n",
-    "print\"\\t hot fluid:shell side,oxygen \\t\"\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.052; # at 225F,lb/(ft)*(hr), from fig.15\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jf=157; # from fig.16.18a\n",
-    "k=0.0183;\n",
-    "Z=0.89; # Z=((c)*(mu1)/k)**(1/3), fig\n",
-    "phys=1;\n",
-    "hf=((jf)*(k/De)*(Z)); #using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hf\n",
-    "Rdo=0.003;\n",
-    "hdo=(1/Rdo);\n",
-    "hf1=(hdo*hf)/(hdo+hf); # eq 16.37\n",
-    "print\"\\t hf1 :  \\t\",hf1\n",
-    "hfi1=142; # fig 16.9\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "at1=0.546; # table 10\n",
-    "L=4;\n",
-    "Nt=21;\n",
-    "n=1;\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "D=0.0695; # ft\n",
-    "row=62.5;\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*row));\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.895; # at 170F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=(710*0.94); # fig 25\n",
-    "print\"\\t hi :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "Rdi=0.003;\n",
-    "hdi=(1/Rdi);\n",
-    "hi1=(hdi*hi)/(hdi+hi); # 16.40\n",
-    "print\"\\t hi1 :  Btu/(hr)*(ft**2)*(F) \\t\",hi1\n",
-    "k1=60; # table 3 , for brass\n",
-    "# yb=0.00146 ft\n",
-    "X=((0.875-0.5)/12)*(21.5/(60*0.00146))**(1/2);\n",
-    "print\"\\t X : \\t\",X\n",
-    "nf=0.91; # from fig 16.13a , by comparing X value\n",
-    "Ai=0.218; # ft**2/ft\n",
-    "hfi2=((nf*Af/144)+(Ao/144))*(hf1/Ai); # eq 16.34\n",
-    "print\"\\t hfi2 :  \\t\",hfi2\n",
-    "UDi=((hfi2)*(hi1)/(hi1+hfi2)); # eq 16.41,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UDi\n",
-    "A=(21*4*Ai); # ft**2\n",
-    "print\"\\t inside surface per bank is :  ft**2 \\t\",A\n",
-    "Ai1=(Q/(UDi*delt));\n",
-    "print\"\\t Ai1 :  ft**2 \\t\",Ai1\n",
-    "Nb=(Ai1/A);\n",
-    "print\"\\t number of banks :  \\t\",Nb\n",
-    "Vn=(4*4*1.95/12)-(41*3.14*1*4/(2*4*144))-((41*3.14*0.035*8*4/(144*2*4))*(1.75**2-1**2)); # fig 16.19b\n",
-    "print\"\\t net free volume :  ft**3 \\t\",Vn\n",
-    "Af1=(41*2.34*4/2);\n",
-    "print\"\\t frictional surface :  ft**2 \\t\",Af1\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=(4*Vn/Af1); # ft\n",
-    "print\"\\t De1 :  ft \\t\",De1\n",
-    "Res1=(De1*Gs/mu1);\n",
-    "print\"\\t reynolds number :  \\t\",Res1\n",
-    "f=0.0024; # fig 16.18b\n",
-    "s=0.000928;\n",
-    "Lp=1.95;\n",
-    "R1=0.538; # R1=(De1/ST)**(0.4)\n",
-    "R2=1; # R2=(SL/ST)**0.6\n",
-    "delPs=((f*(Gs**2)*(Lp)*(R1)*(R2))/(5.22*(10**10)*(De1)*(s)*(1)));\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.0002; # friction factor for reynolds number 30400, using fig.26\n",
-    "s=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(Nb))/(5.22*(10**10)*(0.0695)*(s)*(1))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,2)\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower.ipynb
deleted file mode 100755
index b1b667a8..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower.ipynb
+++ /dev/null
@@ -1,865 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 17 Direct Contact Transfer : Cooling Tower"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 71.1 pgno:585"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.1 \n",
-      "\n",
-      "\t humidity is :  lb water/lb air  0.0186996126364\n",
-      "\t enthalpy at 75F is :  Btu/lb dry air  39.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.1 \\n\"\n",
-    "pw=0.4298; # psia, at 75F, table 7\n",
-    "pt=14.696; # psia\n",
-    "t=75.;\n",
-    "Mw=18.;\n",
-    "Ma=29.;\n",
-    "X=(pw/(pt-pw))*(Mw/Ma);\n",
-    "print\"\\t humidity is :  lb water/lb air \",X\n",
-    "H=(X*t)+(1051.5*X)+(0.24*t); # eq 17.54\n",
-    "print\"\\t enthalpy at 75F is :  Btu/lb dry air \",round(H,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.2 Pgno:602"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 15,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t by numerical integration \t\n",
-      "\t R is :  \t0.93005952381\n",
-      "\t H2 is :  Btu \t71.6520833333\n",
-      "\t difference is :  \t10.9\n",
-      "\t difference is :  \t13.0\n",
-      "\t average of difference is :  \t11.95\n",
-      "\t nd1 is :  \t0.418410041841\n",
-      "\t number of diffusing units :  \t1.7\n",
-      "\t log mean enthalpy difference \t\n",
-      "\t log mean of enthalpy :  Btu/lb \t25.6654878432\n",
-      "\t number of diffusing units are :  \t1.36\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t by numerical integration \\t\"\n",
-    "T1=85.;\n",
-    "T2=120.;\n",
-    "A=576.; # ground area, from fig 17.12\n",
-    "L=1500.*(500./576.);\n",
-    "G=1400.;\n",
-    "R=(L/G);\n",
-    "from math import log10\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "H1=39.1; # fig 17.12\n",
-    "H2=H1+(R*(T2-T1));\n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # fig 17.12\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=43.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=5; # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.70;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "print\"\\t log mean enthalpy difference \\t\"\n",
-    "dt=49.9; # diff. of enthalpies at top of the tower, from table in solution\n",
-    "db=10.9; # diff of enthalpies at bottom of the tower,from table in solution\n",
-    "LME=(dt-db)/(2.3*log10(dt/db));\n",
-    "print\"\\t log mean of enthalpy :  Btu/lb \\t\",LME\n",
-    "nd=(T2-T1)/(LME);\n",
-    "print\"\\t number of diffusing units are :  \\t\",round(nd,2)\n",
-    "# The error is naturally larger the greater the range\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.3 pgno:604"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 16,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Z is : ft \t19.2469565217\n",
-      "\t height of diffusion unit :  ft \t11.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# Since the loading is based on 1 ft2 of ground area\n",
-    "nd=1.7;\n",
-    "L=1302;\n",
-    "Kxa=115;\n",
-    "Z=(nd*L)/(Kxa);\n",
-    "print\"\\t Z is : ft \\t\",Z\n",
-    "HDU=(Z/nd);\n",
-    "print\"\\t height of diffusion unit :  ft \\t\",round(HDU,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.4 pgno:605"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t difference is :  \t13.0\n",
-      "\t difference is :  \t14.3\n",
-      "\t average of difference is :  \t13.65\n",
-      "\t nd1 is :  \t0.417582417582\n",
-      "\t number of diffusing units :  \t1.72\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=79.3F\n",
-    "Hs=43.4; # fig 17.12\n",
-    "H=30.4; # fig 17.12\n",
-    "d1=(Hs-H);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=35.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-79.3); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.72;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.5 pgno:609"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for 120percent of design \t\n",
-      "\t R is : %.3f \t1.116\n",
-      "\t H2 is : %.1f Btu \t78.16\n",
-      "\t difference is : %.1f \t14.0\n",
-      "\t difference is : %.1f \t14.7\n",
-      "\t average of difference is : %.1f \t14.35\n",
-      "\t nd1 is : %.3f \t0.19512195122\n",
-      "\t number of diffusing units : %.2f \t1.53\n",
-      "\t for 80 percent of design \t\n",
-      "\t R is : %.3f \t0.744\n",
-      "\t H2 is :  Btu \t65.14\n",
-      "\t difference is :  \t8.1\n",
-      "\t difference is :  \t9.2\n",
-      "\t average of difference is :  \t8.65\n",
-      "\t nd1 is :  \t0.28901734104\n",
-      "\t number of diffusing units :  \t1.92\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAYQAAAEZCAYAAACXRVJOAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XuYXVV9//H3pwHEULk1SC2gqYjIrYBIVC4yBYSAF7wD\n",
-       "XpDG8osWLFaoVJ4qsWrRKogCLXgJxQIBFREQ5GYZDXciIQQhCJLUIBi5CxIggc/vj7UDY5jJnEnm\n",
-       "zDpn5vN6nnlyzt77nPPJfpL5nrX2XmvJNhEREX9WO0BERHSGFISIiABSECIiopGCEBERQApCREQ0\n",
-       "UhAiIgJIQYiIiEYKQkREACkI0aUkLZC0R5/nB0h6SNKuq/CeB0ia38/21ST9XtK+fbZ9WtIXJfVI\n",
-       "Wriyn7kSGQ+WNHMF+9eQdL+k8c3zN0u6UtIfJD0gabakT0l60Uhlju6RghDdys0Pkj4MnATsa3vA\n",
-       "X5YtOA9YV9Juy22fDDwDXNJn277ARavwWe3yJmC27SckvRf4PnAG8HLbE4D9gY2BTSpmjA6VghDd\n",
-       "TJKmAl8F9rJ9XbNxf0l3S3pJ83wfSfdJ+ovm+dcl/UbSo5JmSdoFwPZTwPeAg5b7nIOAs2w/27x+\n",
-       "PeDVwLVDCLq/pBuX2/ZPks5vHu8r6ZfNN/l7JB0x9NMBlEJ1cfP4eOBztr9j+xEA27+y/Y+271rJ\n",
-       "949RLAUhutk/AJ8Ddrd907KNts8BrgG+0RSBbwMfsf1gc8gNwLbAesBZwPclrdHsOx14j6Q1ASSt\n",
-       "A7y12b7M3sAVHtpEYBcAm0t6VZ9t7wfObB5/B/h/ttcGtgL+dwjv3dc+wEWSXgNsBJy7ku8TY1AK\n",
-       "QnQrAXtSvqXf2s/+Q4HdgSuBC2wv+9aM7TNtP2z7WdvHAy8CNm/2XQMsAt7ZHP4+4A7bt/R577fw\n",
-       "/LfwltheDJwPHAggabPmMy9oDnka2ErS2rYftT17KO/fvOemwGq27wQmNJt/12f/2ZIelvRHSR8c\n",
-       "6vvH6JeCEN3KwEcpv1S//YKd9qPAD4CtgeP67pN0pKTbJD0i6WFgHZ7/BQrwXZ7vNvpQ83zZa/+M\n",
-       "Uoj6Xk9o1Vk0BYHSOjjP9pPN83dTunsWSOqV9IaVeP++3UXLWkMvW7bT9gG21wNuIv/3ox/5RxHd\n",
-       "bBGwB7CrpP/su0PSdsDfUX4Jn9hn+67APwPvtb1u8wvyUUqLY5kzgD0kvRF4Pc936wDsCPxfn+6n\n",
-       "obgC2EDStsABTTYAbM+y/Q5gA+BHlGsZQ9W3INwB/JZSaCJakoIQXc32fZSiMFnS8QBN//8ZwKeB\n",
-       "KcBGkj7WvOQlwFLggeYWzc8Cay/3nguAq4AZwGW2f99n977Aj5fPIelFktZc9jNA1iWUu36+Srl+\n",
-       "cXnz2tUlfUDSOrafAR6j3NU0EC3/ec1tpjtSushoLoAfARwj6e8lradiM2DDFbx3jGGrteuNJU2n\n",
-       "9LX+3vY2/exfD5gOvBJ4Ephi+5fNvgXAHyj/KZbYntSunNH9bC+UtDvwc0lPAmtSvsWfCtD0l18p\n",
-       "6TJKV88lwK+APwJfA37Tz9ueTvn3+c/Lbd8XmNr34ykXbxf33SZpM9t39/O+ZwE/B05edtdS44PA\n",
-       "iZLGAfOADwz01wV2Wv7zgLcD19p++rmN9vckPUopjF8Dnmr+rqdSutMi/oTatWJa0zR/HPjuAAXh\n",
-       "K8AfbH9e0uaU/yB7NvvmAzvYfqgt4SJWgqQNgZtsb1Q7y/IknQzMtX1K7SzRvdrWZdQMEHp4BYds\n",
-       "wfPN2zuAiZI26LNf/b4qop61gU/WDjGAmykD6yJWWs1rCHOAdwFImgS8gjKCEkoT+Ipm0NAhlfJF\n",
-       "/AnbdzZjHDqO7W/ZXlQ7R3S3tl1DaMGXgK9Lmg3MBWbz/IW0XWzf27QYLpc0bxWnJIiIiEFUKwi2\n",
-       "H6PcAQI8d93g7mbfvc2f90s6D5gEvKAgSGrPBZCIiFHO9gu65asVhGZKgMW2n266hX5m+/Hm9rlx\n",
-       "th+TtBawF2V6gn7195eKPyVpmu1ptXN0g5yr1uQ8taZTz9NAX6bbedvpDGA3YEIzPfAxwOoAze2A\n",
-       "WwL/3QS7FfhI89INgfMkLct3pu3L2pUzIiKKthUE2wcOsv9amvljlts+H9iuXbkiIqJ/Gak8NvTW\n",
-       "DtBFemsH6BK9tQN0id7aAYaibQPTRoIk5xpCRMTQDPS7My2EiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICSEGIiIhGCkJERAApCEMm/elyixERo0UKwhBIrAvcLg24vGFERNdKQRgCm0coa+pOkzhZ4kW1\n",
-       "M0VEDJcUhCGymQPsSFlY/ecSL68cKSJiWKQgrISmpfBO4FzgBom9KkeKiFhlmdxulTPQA5wFnAJ8\n",
-       "webZmnkiIgYz0O/OFIRhycHLgO8BjwMftHmwcqSIiAGN+GynkqZLWiRp7gD715N0nqQ5kq6XtFWf\n",
-       "fZMlzZN0p6Sj2pVxuNjcB+wO/BL4hcSOlSNFRAxZO68hnAZMXsH+o4GbbG8LHAR8HUDSOOCk5rVb\n",
-       "AgdK2qKNOYeFzRKbI4EjgIslpkpUb71ERLSqbQXB9kzg4RUcsgVwZXPsHcBESS8FJgF32V5gewlw\n",
-       "NrBfu3ION5tzgZ2Bw4DTJcZXjhQR0ZKadxnNAd4FIGkS8ApgY8rtnAv7HHdPs61r2PwKeAMg4HqJ\n",
-       "V1eOFBExqNUqfvaXgK9Lmg3MBWYDzwBDusotaVqfp722e4cr4Kqw+aPEQcBU4GqJqTY/rJ0rIsYe\n",
-       "ST1Az2DHVSsIth8Dpix7Lmk+8GvgxcAmfQ7dhNJKGOh9prUp4iqzMXCKxC+A70vsBHzaZknlaBEx\n",
-       "hjRflHuXPZd0TH/HVesykrSOpDWax4cAP7P9ODAL2EzSxGb//sAFtXIOB5sbgR2ArYCfNrepRkR0\n",
-       "lHbedjoDuAbYXNJCSVMkTZU0tTlkS2CupHnA3sDhALaXUi7IXgrcBpxj+/Z25RwpzdiEtwBXUG5N\n",
-       "3a1ypIiIP5GBaRVI7A2cDhwHfLXpWoqIGBEZqdxhmknxvg/cCxxs82jlSBExRoz4SOVYMZvfAG+i\n",
-       "FIRZEn9TOVJEjHEpCBXZPGVzKDCNcrH5w5UjRcQYli6jDiGxNWU67V7gcJsn6yaKiNEqXUYdzuZW\n",
-       "ysI76wNXSUysmygixpoUhA5i8wfgfcCZlCkv9q0cKSLGkHQZdSiJXSgT+00HPmfzTOVIETFK5LbT\n",
-       "LiTxl8AMYAnwAZv7K0eKiFEg1xC6kM3vgDcDN1FGN7+hcqSIGMVSEDqczVKbfwE+DlwgcVgW3omI\n",
-       "dkiXUReR2JRya+rtwCE2j1eOFBFdKF1Go4DNr4E3AouBGyReUzlSRIwiKQhdxmaxzRTKxHgzJd5X\n",
-       "O1NEjA7pMupiEq8FfkBZL+JTNk9XjhQRXSBdRqOQzU2UhXc2Ba6Uumvt6YjoLCkIXc7mYWA/4CLK\n",
-       "rKl7VI4UEV2qnSumTZe0SNLcAfZPkHSJpJsl3Srp4D77Fki6RdJsSTe0K+NoYfOszb8DHwTOkDha\n",
-       "SrGPiKFp2zUESbsCjwPftb1NP/unAS+y/WlJE4A7gA1tL5U0H9jB9kODfMaYvobQH4mNge8BDwIH\n",
-       "NS2IiIjnjPg1BNszYYW/jO4D1m4erw082KynvEx+0a8Em3uAHuBuShfS9nUTRUS3qNmt8C1gK0n3\n",
-       "AnOAw/vsM3CFpFmSDqmSrovZPG1zOHA0cJnER2pniojOt1rFzz4auNl2j6RNgcslbWv7MWBn2/dJ\n",
-       "2qDZPq9pcbxA0/W0TK/t3rYn7xI250jcApwrsRNwmM3i2rkiYmRJ6qH0HKz4uHaOQ5A0EbhwgGsI\n",
-       "FwNftH118/ynwFG2Zy133DHA47aP6+c9cg2hBRJ/TmmRvQZ4TzPiOSLGqE4chzAP2BNA0obA5sDd\n",
-       "ksZLekmzfS1gL6DfO5WiNc2cR++nrK1wrcTbK0eKiA7UzruMZgC7AROARcAxwOoAtk9t7iw6DXg5\n",
-       "pTAda/ssSa8Efti8zWrAmbaPHeAz0kIYIok3AudQVmX7jM3SQV4SEaNMFsiJ50hsAJwFjAMOtFlU\n",
-       "OVJEjKBO7DKKSpqV1yYDV1MW3tm5cqSI6ABpIYxxEm+hXFv4EnCCTff+g4iIlqTLKAYk8deUWVPv\n",
-       "Bj5i84fKkSKijdJlFAOymQ/sDDxEWXhnq8qRIqKCFIQAwOZJm6mUrqNeiQ/UzhQRIytdRvECEttS\n",
-       "upAuBY6weapypIgYRukyipbZzAF2BDYGfi7x8sqRImIEpCBEv2weAd4JnEu5rrBX5UgR0WbpMopB\n",
-       "SfRQBrKdAnzB5tm6iSJiVeS201glEi+jLLzzGPAhmwcrR4qIlZRrCLFKbO4Ddgduo4xu3rFypIgY\n",
-       "ZikI0TKbJTZHAkcAF0tMlbKyXcRokS6jWCkSr6ZccJ4NfNTmicqRIqJF6TKKYWXzK+ANlLWvr28K\n",
-       "RER0sRSEWGk2fwQOAk4GrpZ4V+VIEbEK0mUUw6K5yPx9ygjnT9ssqRwpIgYw4l1GkqZLWiSp3+Uv\n",
-       "JU2QdImkmyXdKungPvsmS5on6U5JR7UrYwwfmxuBHYCtgJ82t6lGRBdpZ5fRaZRFWAZyGDDb9nZA\n",
-       "D3CcpNUkjQNOal67JXCgpC3amDOGSTM24S3AFcAsid0qR4qIIWhbQbA9E3h4BYfcB6zdPF4beND2\n",
-       "UmAScJftBbaXAGcD+7UrZwwvm2dt/g2YApwj8c+5NTWiO9S8qPwtYCtJ9wJzgMOb7RsBC/scd0+z\n",
-       "LbqIzaWU4v4e4IcS61SOFBGDWK3iZx8N3Gy7R9KmwOWSth3qm0ia1udpr+3eYcoXq8jmNxJvAo6n\n",
-       "dCG92+aW2rkixhpJPZSu+RWqWRB2Ar4IYPvXkuYDm1NaBJv0OW6TZlu/bE9rY8ZYRc1aCoc2C+78\n",
-       "VOJIm9Nr54oYS5ovyr3Lnks6pr/janYZzQP2BJC0IaUY3A3MAjaTNFHSGsD+wAXVUsawsDkT+Fvg\n",
-       "aIlTJdasnSki/lTbxiFImgHsBkwAFgHHAKsD2D5V0gTKnUgvpxSmY22f1bx2H+AEYBzwHdvHDvAZ\n",
-       "GYfQZSTWBr4D/DXwHpsFdRNFjD2Z/jo6RnPX0SeAfwH+zubiypEixpQUhOg4ErtQbiueDnzO5pnK\n",
-       "kSLGhBSE6EgSG1KKwhLgAzb3V44UMeplttPoSDaLgDcDN1EW3nlD5UgRY1YKQlRns9TmXyjTmVwg\n",
-       "cVhGN0eMvHQZRUeR2JSy8M7twCE2j1eOFDHqpMsouoLNr4E3AouBGyReUzlSxJiRghAdx2axzRTg\n",
-       "OGCmxPtqZ4oYC9JlFB1N4rWURXcuAD5l83TlSBFdL11G0ZVsbqIsvLMpcKWUmW8j2iUFITqezcOU\n",
-       "NTEuosyaukflSBGjUrqMoqs0xeAM4BvAl22erRwpoutkpHKMGhIbA98DHgQOaloQEdGiXEOIUcPm\n",
-       "HspiH7+mdCFtXzdRxOiQghBdyeZpm09QVt67TOIjtTNFdLt0GUXXk9iCMrr5WuAwm8WVI0V0tBHv\n",
-       "MpI0XdIiSXMH2H+kpNnNz1xJSyWt2+xbIOmWZt8N7coYo4PN7cAkYDxwTTP9RUQMUTtXTNsVeBz4\n",
-       "ru1tBjn2rcAnbC9bUnM+sIPthwZ5XVoI8ZxmQrzDgM8Af29n6dWI/ox4C8H2TGj57o/3AzOW25Zf\n",
-       "9DEkNrY5EXg7cJLEsRKr1c4V0S2qX1SWNB7Ym9IHvIyBKyTNknRInWTRrWyuo4xufh3lgvOGlSNF\n",
-       "dIXqBQF4G3CV7Uf6bNvZ9vbAPsChTfdTRMualdcmA1dTbk3duXKkiI7XCc3pA1iuu8j2fc2f90s6\n",
-       "j3LBcGZ/L5Y0rc/TXtu97YkZ3aZZo/kzEtcBP5T4EnCCTffeWhexEiT1UMburPi4dt52KmkicOFA\n",
-       "F5UlrQPcDWxse3GzbTwwzvZjktYCLgM+Z/uyfl6fi8rREom/psyaejcwxeaxypEiqqlx2+kM4Bpg\n",
-       "c0kLJU2RNFXS1D6HvQO4dFkxaGwIzJR0M3A98OP+ikHEUNjMB3YGHgJulNiqcqSIjpOBaTHmSBwM\n",
-       "fAX4hM2ZleNEjLhMbhfRh8S2lC6kS4EjbJ6qHClixGRyu4g+bOYAOwIbAT+XeHnlSBHVpSDEmGXz\n",
-       "CPAuSkvhBom9KkeKqCpdRhGARA9wFnAK8IUsvBOj2ZCvIQw0KV3Dtv9muMKtrBSEGE4SLwPOoczB\n",
-       "9SGbBytHimiLgX53rmhg2tuaP/+h+fN/KPMLfWCYs0V0BJv7miU6/x34hcR7bW6snStipAzaZSTp\n",
-       "ZtvbLbdtdjO1RFVpIUS7SLwb+C/KzKnfzOjmGE1W5S4jSdqlz5OdyUykMcrZnAvsQplO+3SJ8ZUj\n",
-       "RbRdKy2EHYDpwLrNpoeBKbZvanO2QaWFEO0msRblQvO2wLtt7qwcKWKVrfTANElrAu8GJgITgEco\n",
-       "F5X/rQ05hyQFIUZCs/DOVODfgI/a/LBypIhVsjIXlZc5n1IEfgHcM9zBIjpdc/3gFIlfAN+X2An4\n",
-       "tM2SytEihlUrLYRbbW89QnmGJC2EGGkSfwGcAawF7G9zX+VIEUO2KheVr5FUfcxBRCdoxia8BbiC\n",
-       "svDObpUjRQybVloItwOvAubDcxOAZWBajHkSewOnA8cBX82tqdEtVuWi8sT+ttteMBzBVkUKQtTW\n",
-       "TIr3feBe4GCbRytHihhUpr+OaBOJFwHHA3tRbk29pXKkiBWqsWLadEmLBpoTSdKRkmY3P3MlLZW0\n",
-       "brNvsqR5ku6UdFS7MkYMB5unbA4FpgE/lTiocqSIldK2FoKkXSmThH13oDWV+xz7VuATtveUNA64\n",
-       "A9gT+C1wI3Cg7dv7eV1aCNFRJLYGzgV6gcNtnqybKOKFRryFYHsmZVRzK94PzGgeTwLusr3A9hLg\n",
-       "bGC/NkSMGHY2t1IW3lkfuEpiYt1EEa2rvkCOpPHA3pRvVVBWsFrY55B7mm0RXcHmD8D7KOMVrpfY\n",
-       "t3KkiJZULwiUabavsv1I87x7r3JHNGxscwJl2pdvSpwosU7tXBEr0srUFe12AM93F0G5brBJn+eb\n",
-       "sIIpMyRN6/O013bvcIaLWBU2V0lsC3wJuE3iSODsjFmIkSSpB+gZ9Lh23nbajGG4cKCLypLWAe4G\n",
-       "Nra9uNm2GuWi8h6Ue7tvIBeVYxRo5kD6L+B+4FCbOypHijGqxm2nM4BrgM0lLZQ0RdJUSVP7HPYO\n",
-       "4NJlxQDA9lLKHPSXArcB5/RXDCK6jc01wA7ARcDVEp+XeHHlWBHPycC0iAokNga+BrwWOMzmJ5Uj\n",
-       "xRiSkcoRHUhiMnAyMBv4hJ0p5qP9RrzLKCIGZ3MJsDWle/RmiU9KHXGzR4xBaSFEdAiJVwP/CWwA\n",
-       "fKy55hAx7NJlFNEFmuU696dMqf0T4KhmDYaIYZMuo4gu0AxoOxvYEniCMnZhipT/q9F+aSFEdDCJ\n",
-       "11LGLiyhdCP1O3twxFCkhRDRhWxuAnaizIv0U4mvSvx55VgxSqUgRHQ4m2dsTgG2AV5K6UZ6V3O9\n",
-       "IWLYpMsoostI9FDuRpoPfNzm7rqJotukyyhilLDpBbYDrgJulPjXZhnPiFWSghDRhWyetjmWMjfS\n",
-       "JGCOxO6VY0WXS5dRxCggsR/wDUqr4Qib31WOFB0sXUYRo5jN+ZSxCwuBuRKHSoyrHCu6TFoIEaOM\n",
-       "xFaUi85rAR+1mVU5UnSYtBAixgibX1JWxzoR+LHEyRLr1k0V3SAFIWIUaqbAOJ3SjTQOuF3igxm7\n",
-       "ECvSti4jSdOBtwC/X8ESmj2URUJWBx6w3dNsXwD8AXgGWGJ70gCvT5dRRAsk3kCZAuNh4B9s5lWO\n",
-       "FBWN+GynknYFHge+219BkLQucDWwt+17JE2w/UCzbz6wg+2HBvmMFISIFjXrLBwKfAY4FfiizRN1\n",
-       "U0UNI34NwfZMyreRgbwfONf2Pc3xDyy3P7/oI4aRzVKbrwPbAq8CbpV4S+VY0UFqXkPYDFhf0pWS\n",
-       "Zkn6UJ99Bq5oth9SKV/EqGTzW5v9gY8CJ0j8UGKT2rmivppL9a1OWWB8D2A8cK2k62zfCexi+15J\n",
-       "GwCXS5rXtDheQNK0Pk97bfe2OXfEqGBzmcQ2wFHAbIkvAyfYLKkcLYZZc722Z9Dj2jkOQdJE4MIB\n",
-       "riEcBbzY9rTm+beBS2z/YLnjjgEet31cP++RawgRw0BiM+Ak4K8o6y5cVTlStFEnjkM4H9hF0jhJ\n",
-       "44HXA7dJGi/pJQCS1gL2giwKEtFONncCk4HPA2dLTJfYoHKsGGFtKwiSZgDXAJtLWihpiqSpkqYC\n",
-       "2J4HXALcAlwPfMv2bcBfAjMl3dxs/7Hty9qVMyKKZuzC9yhjFx4FfilxSJbvHDsydUVE9EtiO8rY\n",
-       "BVO6keZUjhTDpBO7jCKig9ncDOwM/DdwucTxEi+pmyraKQUhIgZk86zNN4GtgfUpU2C8J1NgjE7p\n",
-       "MoqIlkm8idKN9BvgMJtfV44UKyFdRhGxymx+Tlm+80rgeonPZvnO0SMFISKGxGaJzX9Qlu98LWVB\n",
-       "nj0rx4phkC6jiFglEm+jLN95HWX5znsrR4pBpMsoItrC5kJgK2A+cIvEPzYzq0aXSQshIoaNxBaU\n",
-       "5TvXoSzfeUPlSNGPtBAiou1sbgd2pyx8db7EKRLrVY4VLUpBiIhh1UyB8T+UKTBMGbtwUMYudL50\n",
-       "GUVEW0lMooxdeIyyfOdtlSONeekyiogqmusIk4BzgZ9JHCsxvnKs6EcKQkS0nc0zNicCfwO8Arit\n",
-       "uV01Oki6jCJixDUD2U4G5gH/aPN/lSONKekyioiOYXMFpbUwC/iFxFESa1SONealhRARVUlsSlm+\n",
-       "8+WUi84/qxxp1BvxFoKk6ZIWSRpw+UtJPZJmS7pVUm+f7ZMlzZN0Z7P2ckSMUs2MqfsCnwXOkDhd\n",
-       "4qWVY41J7ewyOo2yRmu/JK1L6UN8m+2tgfc028dRvi1MptzHfKCkLdqYMyIqa8YunEv5P/8AcKvE\n",
-       "1CzfObLadrJtzwQeXsEh7wfOtX1Pc/wDzfZJwF22F9heApwN7NeunBHROWweszkCeDPwYeAaie0r\n",
-       "xxozalbfzYD1JV0paZakDzXbNwIW9jnunmZbRIwRzfrNuwDfBi6ROEFi7cqxRr2aMxKuTplLfQ9g\n",
-       "PHCtpOsoQ91bJmlan6e9tnuHK2BE1GPzLPBtiR8BX6aMXTgC+J49tN8TY52kHqBnsONqFoSFwAO2\n",
-       "FwOLJf0c2JbSItikz3GbNNv6ZXtaO0NGRF02DwAfkdiFMgXGFInDbO6sHK1rNF+Ue5c9l3RMf8fV\n",
-       "7DI6H9hF0jhJ44HXA7dR7kveTNJESWsA+wMXVMwZER3A5ipKr8LlwLUS0yTWrBxrVGnnbaczgGuA\n",
-       "zSUtlDRF0lRJUwFszwMuAW4Brge+Zfs220uBw4BLKQXiHNu3tytnRHSPZvnOrwLbA9tQ7kbau3Ks\n",
-       "USMD0yKia0nsS7lNfRbwTza/rRypK2TqiogYdWwuBrYGfgXMkfhElu9ceWkhRMSoIPEayvKd6wMf\n",
-       "s7m2cqSOlRZCRIxqNvMot7F/BThX4psS61eO1VVSECJi1GimwDiTMgXG05SxCwdn+c7WpMsoIkYt\n",
-       "idcBpwBPULqRflk5UkdIl1FEjDk2syhjnM4GeiW+LLFW5VgdKwUhIka1ZvnO/6SMW9iI0o30jnQj\n",
-       "vVC6jCJiTJHYnXI30p3Ax20W1E008tJlFBEB2PwvZd606yjLdx6d5TuLFISIGHNsnrL5IrAjsDNl\n",
-       "UNvfVo5VXbqMImJMa64lvAP4OvAz4EibRXVTtVe6jCIi+tGMXTiPMnbhd5QJ8z4mMa5ytBGXFkJE\n",
-       "RB8S21DWXVgD+KjNTZUjDbu0ECIiWmAzF3gTpSj8ROJEiXUqxxoRKQgREcuxedbmNEo30pqUsQsH\n",
-       "jvaxC+kyiogYhMROlBbD/cChNndUjrRKRrzLSNJ0SYskzR1gf4+kRyXNbn4+02ffAkm3NNtvaFfG\n",
-       "iIhW2FwD7ABcBFwt8XmJF1eONeza2WV0GjB5kGN+Znv75ufzfbYb6Gm2T2pfxIiI1tgstfkasB3w\n",
-       "GsrdSPtUjjWs2lYQbM8EHh7ksBV196QrKCI6js09Nu+lrP1+ksQPJDaunWs41LyobGAnSXMkXSxp\n",
-       "y+X2XSFplqRDKuWLiBiQzU8oy3feBtws8cluX76zZvibgE1sPyFpH+BHwKubfTvbvk/SBsDlkuY1\n",
-       "LY4XkDStz9Ne273tDB0RsYzNYuCzEmdQJsz7sMTHmmsOHUNSD9Az6HHtvMtI0kTgQtvbtHDsfGAH\n",
-       "2w8tt/0Y4HHbx/XzmtxlFBEdobkldX/gOOAnwFE2D9ZN1b+OG5gmaUNJah5PohSnhySNl/SSZvta\n",
-       "wF5Av3cqRUR0imYKjLMpYxeeoIxdmCJ1z3ivtrUQJM0AdgMmAIuAY4DVAWyfKulQ4GPAUsrJ+6Tt\n",
-       "6yS9Evhh8zarAWfaPnaAz0gLISI6ksRrKWMXllCW7+yYL7YD/e7MwLSIiDZpJsg7BPg8cDowzebx\n",
-       "uqk6sMsoImK0a5bvPIVyN9JLKd1I7+rUKTDSQoiIGCESPZS7keZTlu+8u06OtBAiIqqy6aWMdL4K\n",
-       "uFHiXyVeVDfV81IQIiJGkM3TNsdS5kaaRFm+c/fKsYB0GUVEVCWxH/ANSqthis1T7f/MdBlFRHQc\n",
-       "m/MpYxcuH4lisCJpIUREjDFpIURExAqlIEREBJCCEBERjRSEiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICaGNBkDRd0iJJ/S4KIalH0qOSZjc//9pn32RJ8yTdKemodmWMiIjntbOFcBoweZBjfmZ7++bn\n",
-       "CwCSxgEnNa/dEjhQ0hZtzDnqNQtsRwtyrlqT89SabjtPbSsItmcCDw9yWH/TTkwC7rK9wPYS4Gxg\n",
-       "v+HON8b01A7QRXpqB+gSPbUDdIme2gGGouY1BAM7SZoj6WJJWzbbNwIW9jnunmZbRES00WoVP/sm\n",
-       "YBPbT0jaB/gR8OqKeSIixrS2znYqaSJwoe1tWjh2PmXBiFcD02xPbrZ/GnjW9pf7eU33TtUaEVFR\n",
-       "f7OdVmshSNoQ+L1tS5pEKU4PSZoFbNYUk3uB/YED+3uPTH0dETF82lYQJM0AdgMmSFoIHAOsDmD7\n",
-       "VOA9wMdO9LNwAAAD3ElEQVQkLQWeAA5o9i2VdBhwKTAO+I7t29uVMyIiiq5eICciIoZPx49UHmyQ\n",
-       "mqQj+wxumytpqaR1a2StrYVzNUHSJZJulnSrpIMrxKyuhfO0nqTzmjvgrpe0VY2ctQ02uLQ55hvN\n",
-       "eZwjafuRzNcpWhiE+xpJ10p6UtIRI51vSGx37A+ly+guYCKlu+lmYIsVHP9W4IrauTv1XAHTgGOb\n",
-       "xxOAB4HVamfvwPP0FeAzzePNx/C/qV2B7YG5A+zfF7i4efx64LramTv0PG0AvA74AnBE7bwr+un0\n",
-       "FsJQB6m9H5gxIsk6Tyvn6j5g7ebx2sCDtpeOYMZO0Mp52gK4EsD2HcBESRuMbMz6PPjg0rcDpzfH\n",
-       "Xg+s29wsMqYMdp5s3297FrBk5FKtnE4vCC0PUpM0HtgbOHcEcnWiVs7Vt4CtJN0LzAEOH6FsnaSV\n",
-       "8zQHeBdAcwfcK4CNRyRdd+nvXOY8dbFOLwhDueL9NuAq24+0K0yHa+VcHQ3cbPuvgO2AkyW9pL2x\n",
-       "Ok4r5+lLlG+7s4HDgNnAM21N1b2Wv/U7d6l0sZojlVvxW2CTPs83oXwL6c8BjN3uImjtXO0EfBHA\n",
-       "9q+bwYCbA7NGJGFnGPQ82X4MmLLseXOe7h6RdN1l+XO5cbMtulSntxCeG6QmaQ3KILULlj9I0jrA\n",
-       "m4DzRzhfJ2nlXM0D9oTnBgZuztj7RTfoeZK0TrMPSYdQZuV9fOSjdrwLgIMAJL0BeMT2orqROlrH\n",
-       "D6Tt6BaCBxikJmlqs//U5tB3AJfaXlwpanUtnqt/B06TNIfyZeBTth+qFrqCFs/TlsB/N1Oj3Ap8\n",
-       "pFrgigYbXGr7Ykn7SroL+CPwd/XS1jPYeZL0l8CNlBs5npV0OLBlJ37JyMC0iIgAOr/LKCIiRkgK\n",
-       "QkREACkIERHRSEGIiAggBSEiIhopCBERAaQgRKw0Sf3eRy7pZZIubR5vJunHku6SNEvS/0radWST\n",
-       "RrQmBSFi5Q00iGcycImkNYGLgFNsv8r264CPA68cqYARQ5GBaRErSdJjtl8wOaCksylrT+wM7GJ7\n",
-       "TI7gje6TFkLEMJI0Dtjc9jxgK+CmypEiWpaCEDG8Xg9c1zw2fSY0a5blnCtprK7ZER0uBSFieO0D\n",
-       "XNI8/iXw2mU7bL8TOBhYf+RjRQwuBSFieO0OXNE8PgvYWdLb+uxfa+QjRbSmo6e/juhw45vpjpc5\n",
-       "EXjS9h8BbD8p6a3A8ZJOABYBjwGfH/moEYPLXUYRw0TSB4CNbP9H7SwRKyMFISIigFxDiIiIRgpC\n",
-       "REQAKQgREdFIQYiICCAFISIiGikIEREBpCBERETj/wPQ8mh2PbtLiwAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaaff1d0>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    },
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t trial 1 \t\n",
-      "\t R is :  \t1.1\n",
-      "\t H2 is :  Btu \t73.0\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.7\n",
-      "\t average of difference is :  \t16.1\n",
-      "\t nd1 is :  \t0.310559006211\n",
-      "\t number of diffusing units :  \t1.48\n",
-      "\t L/G is :  \t1.19\n",
-      "\t trial 2 \t\n",
-      "\t R4 is :  \t1.2\n",
-      "\t H2 is :  Btu \t76.5\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.2\n",
-      "\t average of difference is :  \t15.85\n",
-      "\t nd1 is :  \t0.315457413249\n",
-      "\t number of diffusing units :  \t1.56\n",
-      "\t L/G is :  \t1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=85;\n",
-    "T2=120;\n",
-    "R=0.93; # R=(L/G), for 1500 gpm\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "print\"\\t for 120percent of design \\t\"\n",
-    "R1=1.2*R;\n",
-    "print\"\\t R is : %.3f \\t\",R1\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R1*(T2-T1)); \n",
-    "print\"\\t H2 is : %.1f Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=87.2F\n",
-    "Hs=53.1; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is : %.1f \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=42; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is : %.1f \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is : %.1f \\t\",d\n",
-    "dT=(90-87.2); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is : %.3f \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.53;\n",
-    "print\"\\t number of diffusing units : %.2f \\t\",nd\n",
-    "print\"\\t for 80 percent of design \\t\"\n",
-    "R2=0.8*R;\n",
-    "print\"\\t R is : %.3f \\t\",R2\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R2*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=82.5F\n",
-    "Hs=47.2; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=40.8; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-82.5); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.92;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "X=[1.115, 0.93, 0.74];\n",
-    "Y=[1.53, 1.70, 1.92];\n",
-    "pyplot.plot(X,Y)\n",
-    "pyplot.xlabel('L/G')\n",
-    "pyplot.ylabel('nd')\n",
-    "pyplot.title('KxaV/L vs L/G')\n",
-    "pyplot.show()\n",
-    "print\"\\t trial 1 \\t\"\n",
-    "R3=1.1;\n",
-    "print\"\\t R is :  \\t\",R3\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R3*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.48;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.19; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "print\"\\t trial 2 \\t\"\n",
-    "R4=1.2;\n",
-    "print\"\\t R4 is :  \\t\",R4\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R4*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40.5; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.56;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.08; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.6 pgno:615"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t X1 :  lb/lb \t0.0806276339156\n",
-      "\t total water in inlet gas :  lb/hr \t120.941450873\n",
-      "\t H1 :  Btu/lb dry air \t174.00276\n",
-      "\t outlet gas humidity :  lb/lb \t0.0645021071324\n",
-      "\t pw :  psia \t1.38381840969\n",
-      "\t H2 :  Btu/lb dry air \t126.234717909\n",
-      "\t total heat load :  Btu/hr \t71652.063136\n",
-      "\t water loading :  lb/hr \t2047.20180389\n",
-      "\t interval 1 \t\n",
-      "\t C :  Btu/(lb)*(F) \t0.286282435262\n",
-      "\t haV :  Btu/(hr)*(F) \t27.2526231819\n",
-      "\t qc :  Btu/hr \t4905.47217274\n",
-      "\t delT :  F \t11.4233860657\n",
-      "\t T(0.05) :  F \t288.576613934\n",
-      "\t delt :  F \t2.39618398314\n",
-      "\t t(0.05) :  F \t117.603816017\n",
-      "\t interval 2 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc1 :  Btu/hr \t9318.91447199\n",
-      "\t delT1 :  F \t21.7009808594\n",
-      "\t T(0.15) :  F \t266.875633075\n",
-      "\t water diffused during interval :  lb/hr \t1.20784906429\n",
-      "\t water remaining :  lb/hr \t119.733601809\n",
-      "\t qd :  Btu/hr \t1240.46098903\n",
-      "\t q1 :  Btu/hr \t10559.375461\n",
-      "\t delt1 :  F \t5.15795533248\n",
-      "\t t(0.15) :  F \t112.445860684\n",
-      "\t X(112.5F) :  lb/lb \t0.079822401206\n",
-      "\t interval 3 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc2 :  Btu/hr \t8417.23279004\n",
-      "\t delT2 :  F \t19.6012323339\n",
-      "\t T(0.25) :  F \t247.274400741\n",
-      "\t water diffused during interval :  lb/hr \t3.23916482908\n",
-      "\t water remaining :  lb/hr \t116.49443698\n",
-      "\t qd1 :  Btu/hr \t3336.33977395\n",
-      "\t q2 :  Btu/hr \t11753.572564\n",
-      "\t delt2 :  F \t5.7412867367\n",
-      "\t t(0.25) :  F \t106.704573948\n",
-      "\t X(106.5F) :  lb/lb \t0.0776629579866\n",
-      "\t calculated diffusion :  \t18.1244724962\n",
-      "\t Using some standard low-pressure-drop data \t\n",
-      "\t tower height :  ft \t2.16762543941\n",
-      "\t cross section :  ft^2 \t33.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# basis 1ft^2 ground area\n",
-    "#Assumption: 20 per cent of the initial vapor content of the gas enters the water body\n",
-    "X1=(1.69/(14.7-1.69))*(18./29.);\n",
-    "print\"\\t X1 :  lb/lb \\t\",X1\n",
-    "G=1500.;\n",
-    "w1=G*X1;\n",
-    "print\"\\t total water in inlet gas :  lb/hr \\t\",w1\n",
-    "# The inlet gas is at 300F and a 120F dew point. Use 0.25 Btu/(lb)(DegF) for the specific heat of nitrogen\n",
-    "H1=(0.0807*120)+(0.0807*1025.8)+(0.45*0.0807*(300-120))+(0.25*300); # eq 17.55\n",
-    "print\"\\t H1 :  Btu/lb dry air \\t\",H1\n",
-    "X2=(w1*(1-.2)/G);\n",
-    "print\"\\t outlet gas humidity :  lb/lb \\t\",X2\n",
-    "pw=(X2*29*14.7/18)/(1+(X2*29/18));\n",
-    "print\"\\t pw :  psia \\t\",pw\n",
-    "Tw=112.9; # F, from table 7 for above pw\n",
-    "# The outlet gas has a temperature of 200DegF and a 112.9DegF dew point\n",
-    "H2=(X2*Tw)+(X2*1029.8)+(X2*0.45*(200-Tw))+(0.25*200); # eq 17.55\n",
-    "print\"\\t H2 :  Btu/lb dry air \\t\",H2\n",
-    "q=G*(H1-H2);\n",
-    "print\"\\t total heat load :  Btu/hr \\t\",q\n",
-    "w2=q/(120-85);\n",
-    "print\"\\t water loading :  lb/hr \\t\",w2\n",
-    "print\"\\t interval 1 \\t\"\n",
-    "# (Kxa*delV/L)= 0 t0 0.05\n",
-    "nd=0.05; # nd=Kxa*V/L\n",
-    "Le=0.93; # fig 17.4 at 300F\n",
-    "C=(0.25)+(0.45*X1);\n",
-    "print\"\\t C :  Btu/(lb)*(F) \\t\",C\n",
-    "haV=(nd*w2*Le*C);\n",
-    "print\"\\t haV :  Btu/(hr)*(F) \\t\",haV\n",
-    "qc=(haV*(300-120));\n",
-    "print\"\\t qc :  Btu/hr \\t\",qc\n",
-    "delT=(qc/(C*G));\n",
-    "print\"\\t delT :  F \\t\",delT\n",
-    "T1=(300-delT);\n",
-    "print\"\\t T(0.05) :  F \\t\",T1\n",
-    "delt=(qc/w2);\n",
-    "print\"\\t delt :  F \\t\",delt\n",
-    "t1=(120-delt);\n",
-    "print\"\\t t(0.05) :  F \\t\",t1\n",
-    "print\"\\t interval 2 \\t\"\n",
-    "# (Kxa*delV/L)= 0.05 to 0.15\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc1=(haV1*(T1-t1));\n",
-    "print\"\\t qc1 :  Btu/hr \\t\",qc1\n",
-    "delT1=(qc1/(C*G));\n",
-    "print\"\\t delT1 :  F \\t\",delT1\n",
-    "T2=(T1-delT1);\n",
-    "print\"\\t T(0.15) :  F \\t\",T2\n",
-    "X3=0.0748; # at 117.6F\n",
-    "w3=(nd1*w2*(0.0807-X3));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w3\n",
-    "w4=(w1-w3);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w4\n",
-    "l1=1027; # Btu/lb, l1= lamda at 117.6F\n",
-    "qd=(w3*l1);\n",
-    "print\"\\t qd :  Btu/hr \\t\",qd\n",
-    "q1=(qd+qc1);\n",
-    "print\"\\t q1 :  Btu/hr \\t\",q1\n",
-    "delt1=(q1/w2);\n",
-    "print\"\\t delt1 :  F \\t\",delt1\n",
-    "t2=(t1-delt1);\n",
-    "print\"\\t t(0.15) :  F \\t\",t2\n",
-    "X4=0.0640; # at 112.5\n",
-    "X5=(w4/G);\n",
-    "print\"\\t X(112.5F) :  lb/lb \\t\",X5\n",
-    "print\"\\t interval 3 \\t\"\n",
-    "# (Kxa*delV/L)= 0.15 to 0.25\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc2=(haV1*(T2-t2));\n",
-    "print\"\\t qc2 :  Btu/hr \\t\",qc2\n",
-    "delT2=(qc2/(C*G));\n",
-    "print\"\\t delT2 :  F \\t\",delT2\n",
-    "T3=(T2-delT2);\n",
-    "print\"\\t T(0.25) :  F \\t\",T3\n",
-    "w5=(nd1*w2*(X5-X4));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w5\n",
-    "w6=(w4-w5);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w6\n",
-    "l2=1030; # Btu/lb, l1= lamda at 112.5F\n",
-    "qd1=(w5*l2);\n",
-    "print\"\\t qd1 :  Btu/hr \\t\",qd1\n",
-    "q2=(qd1+qc2);\n",
-    "print\"\\t q2 :  Btu/hr \\t\",q2\n",
-    "delt2=(q2/w2);\n",
-    "print\"\\t delt2 :  F \\t\",delt2\n",
-    "t3=(t2-delt2);\n",
-    "print\"\\t t(0.25) :  F \\t\",t3\n",
-    "X6=0.0533; # at 106.5\n",
-    "X7=(w6/G);\n",
-    "print\"\\t X(106.5F) :  lb/lb \\t\",X7\n",
-    "# The calculations of the remaining intervals until a. gas temperature of 200DegF is reached are shown in Fig. 17.17\n",
-    "w7=21.92; # total water diffused from table in solution\n",
-    "d=(w7/w1)*100;\n",
-    "print\"\\t calculated diffusion :  \\t\",d\n",
-    "print\"\\t Using some standard low-pressure-drop data \\t\"\n",
-    "# For G = 1500, extrapolate to L = 2040 on logarithmic coordinates. Kxa = 510.\n",
-    "ndt=.54; # from 1st table in solution\n",
-    "Kxa=510; # from 2nd table in solution\n",
-    "Z=(ndt*w2/Kxa);\n",
-    "print\"\\t tower height :  ft \\t\",Z\n",
-    "A=(50000/G);\n",
-    "print\"\\t cross section :  ft^2 \\t\",round(A,1)\n",
-    "# end\n",
-    "\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.7 pgno:620"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t sensible heat :  Btu/hr \t4200000.0\n",
-      "\t approximate diffusion :  Btu/hr \t756166.666667\n",
-      "\t total heat :  Btu/hr \t4956166.66667\n",
-      "\t total water quantity :  lb/hr \t141604.761905\n",
-      "\t tower cross section :  ft**2 \t69.4140989729\n",
-      "\t new gas rate :  lb/(hr)(ft**2) \t720.314759391\n",
-      "\t LMTD :  \t241.213395056\n",
-      "\t haV/L :  \t0.145099736239\n",
-      "\t number diffusion units :  \t0.557218649152\n",
-      "\t height of tower :  ft \t5.28709788033\n",
-      " ground dimensions :  ft \t1.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "C=0.28; # assumption\n",
-    "w=50000.; # lb/hr\n",
-    "G=1500.;\n",
-    "Qs=(w*C*(500-200));\n",
-    "Qd=(w/G)*(22685); # qd=22685, from previous prblm\n",
-    "from math import log\n",
-    "print\"\\t sensible heat :  Btu/hr \\t\",Qs\n",
-    "print\"\\t approximate diffusion :  Btu/hr \\t\",Qd\n",
-    "Q=(Qs+Qd);\n",
-    "print\"\\t total heat :  Btu/hr \\t\",Q\n",
-    "# an allowance as high as 30 per cent of the sensible load can be made and the excess water compensated for by throttling when the tower is in operation\n",
-    "w1=(Q/(120-85));\n",
-    "print\"\\t total water quantity :  lb/hr \\t\",w1\n",
-    "# If the maximum liquid loading is taken as 2040 lb/(hr)(ft'!), the required tower cross section\n",
-    "A=(w1/2040);\n",
-    "print\"\\t tower cross section :  ft**2 \\t\",A\n",
-    "w3=(w/A);\n",
-    "print\"\\t new gas rate :  lb/(hr)(ft**2) \\t\",w3\n",
-    "# The two terminal temperature differences are (200 - 85) and (500 - 120).\n",
-    "LMTD=((500-120)-(200-85))/(log((500-120)/(200-85)));\n",
-    "print\"\\t LMTD :  \\t\",LMTD\n",
-    "dt=35;\n",
-    "N=(dt/LMTD); # eq 17.88\n",
-    "print\"\\t haV/L :  \\t\",N\n",
-    "Le=0.93;\n",
-    "nd=(N/(C*Le));\n",
-    "print\"\\t number diffusion units :  \\t\",nd\n",
-    "# By extrapolation for G = 718 and L = 2040,Kxa=215\n",
-    "L=2040;\n",
-    "Kxa=215;\n",
-    "Z=(nd*L/Kxa); # calculation mistake\n",
-    "print\"\\t height of tower :  ft \\t\",Z\n",
-    "di=(A)**(1/2);\n",
-    "print\" ground dimensions :  ft \\t\",di\n",
-    "# ground dimensions are 5.8*8.3*8.3 ft\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_1.ipynb
deleted file mode 100755
index 45f8b0e5..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_1.ipynb
+++ /dev/null
@@ -1,856 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 17 Direct Contact Transfer : Cooling Tower"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 71.1 pgno:585"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.1 \n",
-      "\n",
-      "\t humidity is :  lb water/lb air  0.0186996126364\n",
-      "\t enthalpy at 75F is :  Btu/lb dry air  39.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.1 \\n\"\n",
-    "pw=0.4298; # psia, at 75F, table 7\n",
-    "pt=14.696; # psia\n",
-    "t=75.;\n",
-    "Mw=18.;\n",
-    "Ma=29.;\n",
-    "X=(pw/(pt-pw))*(Mw/Ma);\n",
-    "print\"\\t humidity is :  lb water/lb air \",X\n",
-    "H=(X*t)+(1051.5*X)+(0.24*t); # eq 17.54\n",
-    "print\"\\t enthalpy at 75F is :  Btu/lb dry air \",round(H,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.2 Pgno:602"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 15,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t by numerical integration \t\n",
-      "\t R is :  \t0.93005952381\n",
-      "\t H2 is :  Btu \t71.6520833333\n",
-      "\t difference is :  \t10.9\n",
-      "\t difference is :  \t13.0\n",
-      "\t average of difference is :  \t11.95\n",
-      "\t nd1 is :  \t0.418410041841\n",
-      "\t number of diffusing units :  \t1.7\n",
-      "\t log mean enthalpy difference \t\n",
-      "\t log mean of enthalpy :  Btu/lb \t25.6654878432\n",
-      "\t number of diffusing units are :  \t1.36\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t by numerical integration \\t\"\n",
-    "T1=85.;\n",
-    "T2=120.;\n",
-    "A=576.; # ground area, from fig 17.12\n",
-    "L=1500.*(500./576.);\n",
-    "G=1400.;\n",
-    "R=(L/G);\n",
-    "from math import log10\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "H1=39.1; # fig 17.12\n",
-    "H2=H1+(R*(T2-T1));\n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # fig 17.12\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=43.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=5; # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.70;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "print\"\\t log mean enthalpy difference \\t\"\n",
-    "dt=49.9; # diff. of enthalpies at top of the tower, from table in solution\n",
-    "db=10.9; # diff of enthalpies at bottom of the tower,from table in solution\n",
-    "LME=(dt-db)/(2.3*log10(dt/db));\n",
-    "print\"\\t log mean of enthalpy :  Btu/lb \\t\",LME\n",
-    "nd=(T2-T1)/(LME);\n",
-    "print\"\\t number of diffusing units are :  \\t\",round(nd,2)\n",
-    "# The error is naturally larger the greater the range\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.3 pgno:604"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 16,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Z is : ft \t19.2469565217\n",
-      "\t height of diffusion unit :  ft \t11.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# Since the loading is based on 1 ft2 of ground area\n",
-    "nd=1.7;\n",
-    "L=1302;\n",
-    "Kxa=115;\n",
-    "Z=(nd*L)/(Kxa);\n",
-    "print\"\\t Z is : ft \\t\",Z\n",
-    "HDU=(Z/nd);\n",
-    "print\"\\t height of diffusion unit :  ft \\t\",round(HDU,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.4 pgno:605"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t difference is :  \t13.0\n",
-      "\t difference is :  \t14.3\n",
-      "\t average of difference is :  \t13.65\n",
-      "\t nd1 is :  \t0.417582417582\n",
-      "\t number of diffusing units :  \t1.72\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=79.3F\n",
-    "Hs=43.4; # fig 17.12\n",
-    "H=30.4; # fig 17.12\n",
-    "d1=(Hs-H);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=35.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-79.3); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.72;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.5 pgno:609"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for 120percent of design \t\n",
-      "\t R is : %.3f \t1.116\n",
-      "\t H2 is : %.1f Btu \t78.16\n",
-      "\t difference is : %.1f \t14.0\n",
-      "\t difference is : %.1f \t14.7\n",
-      "\t average of difference is : %.1f \t14.35\n",
-      "\t nd1 is : %.3f \t0.19512195122\n",
-      "\t number of diffusing units : %.2f \t1.53\n",
-      "\t for 80 percent of design \t\n",
-      "\t R is : %.3f \t0.744\n",
-      "\t H2 is :  Btu \t65.14\n",
-      "\t difference is :  \t8.1\n",
-      "\t difference is :  \t9.2\n",
-      "\t average of difference is :  \t8.65\n",
-      "\t nd1 is :  \t0.28901734104\n",
-      "\t number of diffusing units :  \t1.92\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAYQAAAEZCAYAAACXRVJOAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XuYXVV9//H3pwHEULk1SC2gqYjIrYBIVC4yBYSAF7wD\n",
-       "XpDG8osWLFaoVJ4qsWrRKogCLXgJxQIBFREQ5GYZDXciIQQhCJLUIBi5CxIggc/vj7UDY5jJnEnm\n",
-       "zDpn5vN6nnlyzt77nPPJfpL5nrX2XmvJNhEREX9WO0BERHSGFISIiABSECIiopGCEBERQApCREQ0\n",
-       "UhAiIgJIQYiIiEYKQkREACkI0aUkLZC0R5/nB0h6SNKuq/CeB0ia38/21ST9XtK+fbZ9WtIXJfVI\n",
-       "Wriyn7kSGQ+WNHMF+9eQdL+k8c3zN0u6UtIfJD0gabakT0l60Uhlju6RghDdys0Pkj4MnATsa3vA\n",
-       "X5YtOA9YV9Juy22fDDwDXNJn277ARavwWe3yJmC27SckvRf4PnAG8HLbE4D9gY2BTSpmjA6VghDd\n",
-       "TJKmAl8F9rJ9XbNxf0l3S3pJ83wfSfdJ+ovm+dcl/UbSo5JmSdoFwPZTwPeAg5b7nIOAs2w/27x+\n",
-       "PeDVwLVDCLq/pBuX2/ZPks5vHu8r6ZfNN/l7JB0x9NMBlEJ1cfP4eOBztr9j+xEA27+y/Y+271rJ\n",
-       "949RLAUhutk/AJ8Ddrd907KNts8BrgG+0RSBbwMfsf1gc8gNwLbAesBZwPclrdHsOx14j6Q1ASSt\n",
-       "A7y12b7M3sAVHtpEYBcAm0t6VZ9t7wfObB5/B/h/ttcGtgL+dwjv3dc+wEWSXgNsBJy7ku8TY1AK\n",
-       "QnQrAXtSvqXf2s/+Q4HdgSuBC2wv+9aM7TNtP2z7WdvHAy8CNm/2XQMsAt7ZHP4+4A7bt/R577fw\n",
-       "/LfwltheDJwPHAggabPmMy9oDnka2ErS2rYftT17KO/fvOemwGq27wQmNJt/12f/2ZIelvRHSR8c\n",
-       "6vvH6JeCEN3KwEcpv1S//YKd9qPAD4CtgeP67pN0pKTbJD0i6WFgHZ7/BQrwXZ7vNvpQ83zZa/+M\n",
-       "Uoj6Xk9o1Vk0BYHSOjjP9pPN83dTunsWSOqV9IaVeP++3UXLWkMvW7bT9gG21wNuIv/3ox/5RxHd\n",
-       "bBGwB7CrpP/su0PSdsDfUX4Jn9hn+67APwPvtb1u8wvyUUqLY5kzgD0kvRF4Pc936wDsCPxfn+6n\n",
-       "obgC2EDStsABTTYAbM+y/Q5gA+BHlGsZQ9W3INwB/JZSaCJakoIQXc32fZSiMFnS8QBN//8ZwKeB\n",
-       "KcBGkj7WvOQlwFLggeYWzc8Cay/3nguAq4AZwGW2f99n977Aj5fPIelFktZc9jNA1iWUu36+Srl+\n",
-       "cXnz2tUlfUDSOrafAR6j3NU0EC3/ec1tpjtSushoLoAfARwj6e8lradiM2DDFbx3jGGrteuNJU2n\n",
-       "9LX+3vY2/exfD5gOvBJ4Ephi+5fNvgXAHyj/KZbYntSunNH9bC+UtDvwc0lPAmtSvsWfCtD0l18p\n",
-       "6TJKV88lwK+APwJfA37Tz9ueTvn3+c/Lbd8XmNr34ykXbxf33SZpM9t39/O+ZwE/B05edtdS44PA\n",
-       "iZLGAfOADwz01wV2Wv7zgLcD19p++rmN9vckPUopjF8Dnmr+rqdSutMi/oTatWJa0zR/HPjuAAXh\n",
-       "K8AfbH9e0uaU/yB7NvvmAzvYfqgt4SJWgqQNgZtsb1Q7y/IknQzMtX1K7SzRvdrWZdQMEHp4BYds\n",
-       "wfPN2zuAiZI26LNf/b4qop61gU/WDjGAmykD6yJWWs1rCHOAdwFImgS8gjKCEkoT+Ipm0NAhlfJF\n",
-       "/AnbdzZjHDqO7W/ZXlQ7R3S3tl1DaMGXgK9Lmg3MBWbz/IW0XWzf27QYLpc0bxWnJIiIiEFUKwi2\n",
-       "H6PcAQI8d93g7mbfvc2f90s6D5gEvKAgSGrPBZCIiFHO9gu65asVhGZKgMW2n266hX5m+/Hm9rlx\n",
-       "th+TtBawF2V6gn7195eKPyVpmu1ptXN0g5yr1uQ8taZTz9NAX6bbedvpDGA3YEIzPfAxwOoAze2A\n",
-       "WwL/3QS7FfhI89INgfMkLct3pu3L2pUzIiKKthUE2wcOsv9amvljlts+H9iuXbkiIqJ/Gak8NvTW\n",
-       "DtBFemsH6BK9tQN0id7aAYaibQPTRoIk5xpCRMTQDPS7My2EiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICSEGIiIhGCkJERAApCEMm/elyixERo0UKwhBIrAvcLg24vGFERNdKQRgCm0coa+pOkzhZ4kW1\n",
-       "M0VEDJcUhCGymQPsSFlY/ecSL68cKSJiWKQgrISmpfBO4FzgBom9KkeKiFhlmdxulTPQA5wFnAJ8\n",
-       "webZmnkiIgYz0O/OFIRhycHLgO8BjwMftHmwcqSIiAGN+GynkqZLWiRp7gD715N0nqQ5kq6XtFWf\n",
-       "fZMlzZN0p6Sj2pVxuNjcB+wO/BL4hcSOlSNFRAxZO68hnAZMXsH+o4GbbG8LHAR8HUDSOOCk5rVb\n",
-       "AgdK2qKNOYeFzRKbI4EjgIslpkpUb71ERLSqbQXB9kzg4RUcsgVwZXPsHcBESS8FJgF32V5gewlw\n",
-       "NrBfu3ION5tzgZ2Bw4DTJcZXjhQR0ZKadxnNAd4FIGkS8ApgY8rtnAv7HHdPs61r2PwKeAMg4HqJ\n",
-       "V1eOFBExqNUqfvaXgK9Lmg3MBWYDzwBDusotaVqfp722e4cr4Kqw+aPEQcBU4GqJqTY/rJ0rIsYe\n",
-       "ST1Az2DHVSsIth8Dpix7Lmk+8GvgxcAmfQ7dhNJKGOh9prUp4iqzMXCKxC+A70vsBHzaZknlaBEx\n",
-       "hjRflHuXPZd0TH/HVesykrSOpDWax4cAP7P9ODAL2EzSxGb//sAFtXIOB5sbgR2ArYCfNrepRkR0\n",
-       "lHbedjoDuAbYXNJCSVMkTZU0tTlkS2CupHnA3sDhALaXUi7IXgrcBpxj+/Z25RwpzdiEtwBXUG5N\n",
-       "3a1ypIiIP5GBaRVI7A2cDhwHfLXpWoqIGBEZqdxhmknxvg/cCxxs82jlSBExRoz4SOVYMZvfAG+i\n",
-       "FIRZEn9TOVJEjHEpCBXZPGVzKDCNcrH5w5UjRcQYli6jDiGxNWU67V7gcJsn6yaKiNEqXUYdzuZW\n",
-       "ysI76wNXSUysmygixpoUhA5i8wfgfcCZlCkv9q0cKSLGkHQZdSiJXSgT+00HPmfzTOVIETFK5LbT\n",
-       "LiTxl8AMYAnwAZv7K0eKiFEg1xC6kM3vgDcDN1FGN7+hcqSIGMVSEDqczVKbfwE+DlwgcVgW3omI\n",
-       "dkiXUReR2JRya+rtwCE2j1eOFBFdKF1Go4DNr4E3AouBGyReUzlSRIwiKQhdxmaxzRTKxHgzJd5X\n",
-       "O1NEjA7pMupiEq8FfkBZL+JTNk9XjhQRXSBdRqOQzU2UhXc2Ba6Uumvt6YjoLCkIXc7mYWA/4CLK\n",
-       "rKl7VI4UEV2qnSumTZe0SNLcAfZPkHSJpJsl3Srp4D77Fki6RdJsSTe0K+NoYfOszb8DHwTOkDha\n",
-       "SrGPiKFp2zUESbsCjwPftb1NP/unAS+y/WlJE4A7gA1tL5U0H9jB9kODfMaYvobQH4mNge8BDwIH\n",
-       "NS2IiIjnjPg1BNszYYW/jO4D1m4erw082KynvEx+0a8Em3uAHuBuShfS9nUTRUS3qNmt8C1gK0n3\n",
-       "AnOAw/vsM3CFpFmSDqmSrovZPG1zOHA0cJnER2pniojOt1rFzz4auNl2j6RNgcslbWv7MWBn2/dJ\n",
-       "2qDZPq9pcbxA0/W0TK/t3rYn7xI250jcApwrsRNwmM3i2rkiYmRJ6qH0HKz4uHaOQ5A0EbhwgGsI\n",
-       "FwNftH118/ynwFG2Zy133DHA47aP6+c9cg2hBRJ/TmmRvQZ4TzPiOSLGqE4chzAP2BNA0obA5sDd\n",
-       "ksZLekmzfS1gL6DfO5WiNc2cR++nrK1wrcTbK0eKiA7UzruMZgC7AROARcAxwOoAtk9t7iw6DXg5\n",
-       "pTAda/ssSa8Efti8zWrAmbaPHeAz0kIYIok3AudQVmX7jM3SQV4SEaNMFsiJ50hsAJwFjAMOtFlU\n",
-       "OVJEjKBO7DKKSpqV1yYDV1MW3tm5cqSI6ABpIYxxEm+hXFv4EnCCTff+g4iIlqTLKAYk8deUWVPv\n",
-       "Bj5i84fKkSKijdJlFAOymQ/sDDxEWXhnq8qRIqKCFIQAwOZJm6mUrqNeiQ/UzhQRIytdRvECEttS\n",
-       "upAuBY6weapypIgYRukyipbZzAF2BDYGfi7x8sqRImIEpCBEv2weAd4JnEu5rrBX5UgR0WbpMopB\n",
-       "SfRQBrKdAnzB5tm6iSJiVeS201glEi+jLLzzGPAhmwcrR4qIlZRrCLFKbO4Ddgduo4xu3rFypIgY\n",
-       "ZikI0TKbJTZHAkcAF0tMlbKyXcRokS6jWCkSr6ZccJ4NfNTmicqRIqJF6TKKYWXzK+ANlLWvr28K\n",
-       "RER0sRSEWGk2fwQOAk4GrpZ4V+VIEbEK0mUUw6K5yPx9ygjnT9ssqRwpIgYw4l1GkqZLWiSp3+Uv\n",
-       "JU2QdImkmyXdKungPvsmS5on6U5JR7UrYwwfmxuBHYCtgJ82t6lGRBdpZ5fRaZRFWAZyGDDb9nZA\n",
-       "D3CcpNUkjQNOal67JXCgpC3amDOGSTM24S3AFcAsid0qR4qIIWhbQbA9E3h4BYfcB6zdPF4beND2\n",
-       "UmAScJftBbaXAGcD+7UrZwwvm2dt/g2YApwj8c+5NTWiO9S8qPwtYCtJ9wJzgMOb7RsBC/scd0+z\n",
-       "LbqIzaWU4v4e4IcS61SOFBGDWK3iZx8N3Gy7R9KmwOWSth3qm0ia1udpr+3eYcoXq8jmNxJvAo6n\n",
-       "dCG92+aW2rkixhpJPZSu+RWqWRB2Ar4IYPvXkuYDm1NaBJv0OW6TZlu/bE9rY8ZYRc1aCoc2C+78\n",
-       "VOJIm9Nr54oYS5ovyr3Lnks6pr/janYZzQP2BJC0IaUY3A3MAjaTNFHSGsD+wAXVUsawsDkT+Fvg\n",
-       "aIlTJdasnSki/lTbxiFImgHsBkwAFgHHAKsD2D5V0gTKnUgvpxSmY22f1bx2H+AEYBzwHdvHDvAZ\n",
-       "GYfQZSTWBr4D/DXwHpsFdRNFjD2Z/jo6RnPX0SeAfwH+zubiypEixpQUhOg4ErtQbiueDnzO5pnK\n",
-       "kSLGhBSE6EgSG1KKwhLgAzb3V44UMeplttPoSDaLgDcDN1EW3nlD5UgRY1YKQlRns9TmXyjTmVwg\n",
-       "cVhGN0eMvHQZRUeR2JSy8M7twCE2j1eOFDHqpMsouoLNr4E3AouBGyReUzlSxJiRghAdx2axzRTg\n",
-       "OGCmxPtqZ4oYC9JlFB1N4rWURXcuAD5l83TlSBFdL11G0ZVsbqIsvLMpcKWUmW8j2iUFITqezcOU\n",
-       "NTEuosyaukflSBGjUrqMoqs0xeAM4BvAl22erRwpoutkpHKMGhIbA98DHgQOaloQEdGiXEOIUcPm\n",
-       "HspiH7+mdCFtXzdRxOiQghBdyeZpm09QVt67TOIjtTNFdLt0GUXXk9iCMrr5WuAwm8WVI0V0tBHv\n",
-       "MpI0XdIiSXMH2H+kpNnNz1xJSyWt2+xbIOmWZt8N7coYo4PN7cAkYDxwTTP9RUQMUTtXTNsVeBz4\n",
-       "ru1tBjn2rcAnbC9bUnM+sIPthwZ5XVoI8ZxmQrzDgM8Af29n6dWI/ox4C8H2TGj57o/3AzOW25Zf\n",
-       "9DEkNrY5EXg7cJLEsRKr1c4V0S2qX1SWNB7Ym9IHvIyBKyTNknRInWTRrWyuo4xufh3lgvOGlSNF\n",
-       "dIXqBQF4G3CV7Uf6bNvZ9vbAPsChTfdTRMualdcmA1dTbk3duXKkiI7XCc3pA1iuu8j2fc2f90s6\n",
-       "j3LBcGZ/L5Y0rc/TXtu97YkZ3aZZo/kzEtcBP5T4EnCCTffeWhexEiT1UMburPi4dt52KmkicOFA\n",
-       "F5UlrQPcDWxse3GzbTwwzvZjktYCLgM+Z/uyfl6fi8rREom/psyaejcwxeaxypEiqqlx2+kM4Bpg\n",
-       "c0kLJU2RNFXS1D6HvQO4dFkxaGwIzJR0M3A98OP+ikHEUNjMB3YGHgJulNiqcqSIjpOBaTHmSBwM\n",
-       "fAX4hM2ZleNEjLhMbhfRh8S2lC6kS4EjbJ6qHClixGRyu4g+bOYAOwIbAT+XeHnlSBHVpSDEmGXz\n",
-       "CPAuSkvhBom9KkeKqCpdRhGARA9wFnAK8IUsvBOj2ZCvIQw0KV3Dtv9muMKtrBSEGE4SLwPOoczB\n",
-       "9SGbBytHimiLgX53rmhg2tuaP/+h+fN/KPMLfWCYs0V0BJv7miU6/x34hcR7bW6snStipAzaZSTp\n",
-       "ZtvbLbdtdjO1RFVpIUS7SLwb+C/KzKnfzOjmGE1W5S4jSdqlz5OdyUykMcrZnAvsQplO+3SJ8ZUj\n",
-       "RbRdKy2EHYDpwLrNpoeBKbZvanO2QaWFEO0msRblQvO2wLtt7qwcKWKVrfTANElrAu8GJgITgEco\n",
-       "F5X/rQ05hyQFIUZCs/DOVODfgI/a/LBypIhVsjIXlZc5n1IEfgHcM9zBIjpdc/3gFIlfAN+X2An4\n",
-       "tM2SytEihlUrLYRbbW89QnmGJC2EGGkSfwGcAawF7G9zX+VIEUO2KheVr5FUfcxBRCdoxia8BbiC\n",
-       "svDObpUjRQybVloItwOvAubDcxOAZWBajHkSewOnA8cBX82tqdEtVuWi8sT+ttteMBzBVkUKQtTW\n",
-       "TIr3feBe4GCbRytHihhUpr+OaBOJFwHHA3tRbk29pXKkiBWqsWLadEmLBpoTSdKRkmY3P3MlLZW0\n",
-       "brNvsqR5ku6UdFS7MkYMB5unbA4FpgE/lTiocqSIldK2FoKkXSmThH13oDWV+xz7VuATtveUNA64\n",
-       "A9gT+C1wI3Cg7dv7eV1aCNFRJLYGzgV6gcNtnqybKOKFRryFYHsmZVRzK94PzGgeTwLusr3A9hLg\n",
-       "bGC/NkSMGHY2t1IW3lkfuEpiYt1EEa2rvkCOpPHA3pRvVVBWsFrY55B7mm0RXcHmD8D7KOMVrpfY\n",
-       "t3KkiJZULwiUabavsv1I87x7r3JHNGxscwJl2pdvSpwosU7tXBEr0srUFe12AM93F0G5brBJn+eb\n",
-       "sIIpMyRN6/O013bvcIaLWBU2V0lsC3wJuE3iSODsjFmIkSSpB+gZ9Lh23nbajGG4cKCLypLWAe4G\n",
-       "Nra9uNm2GuWi8h6Ue7tvIBeVYxRo5kD6L+B+4FCbOypHijGqxm2nM4BrgM0lLZQ0RdJUSVP7HPYO\n",
-       "4NJlxQDA9lLKHPSXArcB5/RXDCK6jc01wA7ARcDVEp+XeHHlWBHPycC0iAokNga+BrwWOMzmJ5Uj\n",
-       "xRiSkcoRHUhiMnAyMBv4hJ0p5qP9RrzLKCIGZ3MJsDWle/RmiU9KHXGzR4xBaSFEdAiJVwP/CWwA\n",
-       "fKy55hAx7NJlFNEFmuU696dMqf0T4KhmDYaIYZMuo4gu0AxoOxvYEniCMnZhipT/q9F+aSFEdDCJ\n",
-       "11LGLiyhdCP1O3twxFCkhRDRhWxuAnaizIv0U4mvSvx55VgxSqUgRHQ4m2dsTgG2AV5K6UZ6V3O9\n",
-       "IWLYpMsoostI9FDuRpoPfNzm7rqJotukyyhilLDpBbYDrgJulPjXZhnPiFWSghDRhWyetjmWMjfS\n",
-       "JGCOxO6VY0WXS5dRxCggsR/wDUqr4Qib31WOFB0sXUYRo5jN+ZSxCwuBuRKHSoyrHCu6TFoIEaOM\n",
-       "xFaUi85rAR+1mVU5UnSYtBAixgibX1JWxzoR+LHEyRLr1k0V3SAFIWIUaqbAOJ3SjTQOuF3igxm7\n",
-       "ECvSti4jSdOBtwC/X8ESmj2URUJWBx6w3dNsXwD8AXgGWGJ70gCvT5dRRAsk3kCZAuNh4B9s5lWO\n",
-       "FBWN+GynknYFHge+219BkLQucDWwt+17JE2w/UCzbz6wg+2HBvmMFISIFjXrLBwKfAY4FfiizRN1\n",
-       "U0UNI34NwfZMyreRgbwfONf2Pc3xDyy3P7/oI4aRzVKbrwPbAq8CbpV4S+VY0UFqXkPYDFhf0pWS\n",
-       "Zkn6UJ99Bq5oth9SKV/EqGTzW5v9gY8CJ0j8UGKT2rmivppL9a1OWWB8D2A8cK2k62zfCexi+15J\n",
-       "GwCXS5rXtDheQNK0Pk97bfe2OXfEqGBzmcQ2wFHAbIkvAyfYLKkcLYZZc722Z9Dj2jkOQdJE4MIB\n",
-       "riEcBbzY9rTm+beBS2z/YLnjjgEet31cP++RawgRw0BiM+Ak4K8o6y5cVTlStFEnjkM4H9hF0jhJ\n",
-       "44HXA7dJGi/pJQCS1gL2giwKEtFONncCk4HPA2dLTJfYoHKsGGFtKwiSZgDXAJtLWihpiqSpkqYC\n",
-       "2J4HXALcAlwPfMv2bcBfAjMl3dxs/7Hty9qVMyKKZuzC9yhjFx4FfilxSJbvHDsydUVE9EtiO8rY\n",
-       "BVO6keZUjhTDpBO7jCKig9ncDOwM/DdwucTxEi+pmyraKQUhIgZk86zNN4GtgfUpU2C8J1NgjE7p\n",
-       "MoqIlkm8idKN9BvgMJtfV44UKyFdRhGxymx+Tlm+80rgeonPZvnO0SMFISKGxGaJzX9Qlu98LWVB\n",
-       "nj0rx4phkC6jiFglEm+jLN95HWX5znsrR4pBpMsoItrC5kJgK2A+cIvEPzYzq0aXSQshIoaNxBaU\n",
-       "5TvXoSzfeUPlSNGPtBAiou1sbgd2pyx8db7EKRLrVY4VLUpBiIhh1UyB8T+UKTBMGbtwUMYudL50\n",
-       "GUVEW0lMooxdeIyyfOdtlSONeekyiogqmusIk4BzgZ9JHCsxvnKs6EcKQkS0nc0zNicCfwO8Arit\n",
-       "uV01Oki6jCJixDUD2U4G5gH/aPN/lSONKekyioiOYXMFpbUwC/iFxFESa1SONealhRARVUlsSlm+\n",
-       "8+WUi84/qxxp1BvxFoKk6ZIWSRpw+UtJPZJmS7pVUm+f7ZMlzZN0Z7P2ckSMUs2MqfsCnwXOkDhd\n",
-       "4qWVY41J7ewyOo2yRmu/JK1L6UN8m+2tgfc028dRvi1MptzHfKCkLdqYMyIqa8YunEv5P/8AcKvE\n",
-       "1CzfObLadrJtzwQeXsEh7wfOtX1Pc/wDzfZJwF22F9heApwN7NeunBHROWweszkCeDPwYeAaie0r\n",
-       "xxozalbfzYD1JV0paZakDzXbNwIW9jnunmZbRIwRzfrNuwDfBi6ROEFi7cqxRr2aMxKuTplLfQ9g\n",
-       "PHCtpOsoQ91bJmlan6e9tnuHK2BE1GPzLPBtiR8BX6aMXTgC+J49tN8TY52kHqBnsONqFoSFwAO2\n",
-       "FwOLJf0c2JbSItikz3GbNNv6ZXtaO0NGRF02DwAfkdiFMgXGFInDbO6sHK1rNF+Ue5c9l3RMf8fV\n",
-       "7DI6H9hF0jhJ44HXA7dR7kveTNJESWsA+wMXVMwZER3A5ipKr8LlwLUS0yTWrBxrVGnnbaczgGuA\n",
-       "zSUtlDRF0lRJUwFszwMuAW4Brge+Zfs220uBw4BLKQXiHNu3tytnRHSPZvnOrwLbA9tQ7kbau3Ks\n",
-       "USMD0yKia0nsS7lNfRbwTza/rRypK2TqiogYdWwuBrYGfgXMkfhElu9ceWkhRMSoIPEayvKd6wMf\n",
-       "s7m2cqSOlRZCRIxqNvMot7F/BThX4psS61eO1VVSECJi1GimwDiTMgXG05SxCwdn+c7WpMsoIkYt\n",
-       "idcBpwBPULqRflk5UkdIl1FEjDk2syhjnM4GeiW+LLFW5VgdKwUhIka1ZvnO/6SMW9iI0o30jnQj\n",
-       "vVC6jCJiTJHYnXI30p3Ax20W1E008tJlFBEB2PwvZd606yjLdx6d5TuLFISIGHNsnrL5IrAjsDNl\n",
-       "UNvfVo5VXbqMImJMa64lvAP4OvAz4EibRXVTtVe6jCIi+tGMXTiPMnbhd5QJ8z4mMa5ytBGXFkJE\n",
-       "RB8S21DWXVgD+KjNTZUjDbu0ECIiWmAzF3gTpSj8ROJEiXUqxxoRKQgREcuxedbmNEo30pqUsQsH\n",
-       "jvaxC+kyiogYhMROlBbD/cChNndUjrRKRrzLSNJ0SYskzR1gf4+kRyXNbn4+02ffAkm3NNtvaFfG\n",
-       "iIhW2FwD7ABcBFwt8XmJF1eONeza2WV0GjB5kGN+Znv75ufzfbYb6Gm2T2pfxIiI1tgstfkasB3w\n",
-       "GsrdSPtUjjWs2lYQbM8EHh7ksBV196QrKCI6js09Nu+lrP1+ksQPJDaunWs41LyobGAnSXMkXSxp\n",
-       "y+X2XSFplqRDKuWLiBiQzU8oy3feBtws8cluX76zZvibgE1sPyFpH+BHwKubfTvbvk/SBsDlkuY1\n",
-       "LY4XkDStz9Ne273tDB0RsYzNYuCzEmdQJsz7sMTHmmsOHUNSD9Az6HHtvMtI0kTgQtvbtHDsfGAH\n",
-       "2w8tt/0Y4HHbx/XzmtxlFBEdobkldX/gOOAnwFE2D9ZN1b+OG5gmaUNJah5PohSnhySNl/SSZvta\n",
-       "wF5Av3cqRUR0imYKjLMpYxeeoIxdmCJ1z3ivtrUQJM0AdgMmAIuAY4DVAWyfKulQ4GPAUsrJ+6Tt\n",
-       "6yS9Evhh8zarAWfaPnaAz0gLISI6ksRrKWMXllCW7+yYL7YD/e7MwLSIiDZpJsg7BPg8cDowzebx\n",
-       "uqk6sMsoImK0a5bvPIVyN9JLKd1I7+rUKTDSQoiIGCESPZS7keZTlu+8u06OtBAiIqqy6aWMdL4K\n",
-       "uFHiXyVeVDfV81IQIiJGkM3TNsdS5kaaRFm+c/fKsYB0GUVEVCWxH/ANSqthis1T7f/MdBlFRHQc\n",
-       "m/MpYxcuH4lisCJpIUREjDFpIURExAqlIEREBJCCEBERjRSEiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICaGNBkDRd0iJJ/S4KIalH0qOSZjc//9pn32RJ8yTdKemodmWMiIjntbOFcBoweZBjfmZ7++bn\n",
-       "CwCSxgEnNa/dEjhQ0hZtzDnqNQtsRwtyrlqT89SabjtPbSsItmcCDw9yWH/TTkwC7rK9wPYS4Gxg\n",
-       "v+HON8b01A7QRXpqB+gSPbUDdIme2gGGouY1BAM7SZoj6WJJWzbbNwIW9jnunmZbRES00WoVP/sm\n",
-       "YBPbT0jaB/gR8OqKeSIixrS2znYqaSJwoe1tWjh2PmXBiFcD02xPbrZ/GnjW9pf7eU33TtUaEVFR\n",
-       "f7OdVmshSNoQ+L1tS5pEKU4PSZoFbNYUk3uB/YED+3uPTH0dETF82lYQJM0AdgMmSFoIHAOsDmD7\n",
-       "VOA9wMdO9LNwAAAD3ElEQVQkLQWeAA5o9i2VdBhwKTAO+I7t29uVMyIiiq5eICciIoZPx49UHmyQ\n",
-       "mqQj+wxumytpqaR1a2StrYVzNUHSJZJulnSrpIMrxKyuhfO0nqTzmjvgrpe0VY2ctQ02uLQ55hvN\n",
-       "eZwjafuRzNcpWhiE+xpJ10p6UtIRI51vSGx37A+ly+guYCKlu+lmYIsVHP9W4IrauTv1XAHTgGOb\n",
-       "xxOAB4HVamfvwPP0FeAzzePNx/C/qV2B7YG5A+zfF7i4efx64LramTv0PG0AvA74AnBE7bwr+un0\n",
-       "FsJQB6m9H5gxIsk6Tyvn6j5g7ebx2sCDtpeOYMZO0Mp52gK4EsD2HcBESRuMbMz6PPjg0rcDpzfH\n",
-       "Xg+s29wsMqYMdp5s3297FrBk5FKtnE4vCC0PUpM0HtgbOHcEcnWiVs7Vt4CtJN0LzAEOH6FsnaSV\n",
-       "8zQHeBdAcwfcK4CNRyRdd+nvXOY8dbFOLwhDueL9NuAq24+0K0yHa+VcHQ3cbPuvgO2AkyW9pL2x\n",
-       "Ok4r5+lLlG+7s4HDgNnAM21N1b2Wv/U7d6l0sZojlVvxW2CTPs83oXwL6c8BjN3uImjtXO0EfBHA\n",
-       "9q+bwYCbA7NGJGFnGPQ82X4MmLLseXOe7h6RdN1l+XO5cbMtulSntxCeG6QmaQ3KILULlj9I0jrA\n",
-       "m4DzRzhfJ2nlXM0D9oTnBgZuztj7RTfoeZK0TrMPSYdQZuV9fOSjdrwLgIMAJL0BeMT2orqROlrH\n",
-       "D6Tt6BaCBxikJmlqs//U5tB3AJfaXlwpanUtnqt/B06TNIfyZeBTth+qFrqCFs/TlsB/N1Oj3Ap8\n",
-       "pFrgigYbXGr7Ykn7SroL+CPwd/XS1jPYeZL0l8CNlBs5npV0OLBlJ37JyMC0iIgAOr/LKCIiRkgK\n",
-       "QkREACkIERHRSEGIiAggBSEiIhopCBERAaQgRKw0Sf3eRy7pZZIubR5vJunHku6SNEvS/0radWST\n",
-       "RrQmBSFi5Q00iGcycImkNYGLgFNsv8r264CPA68cqYARQ5GBaRErSdJjtl8wOaCksylrT+wM7GJ7\n",
-       "TI7gje6TFkLEMJI0Dtjc9jxgK+CmypEiWpaCEDG8Xg9c1zw2fSY0a5blnCtprK7ZER0uBSFieO0D\n",
-       "XNI8/iXw2mU7bL8TOBhYf+RjRQwuBSFieO0OXNE8PgvYWdLb+uxfa+QjRbSmo6e/juhw45vpjpc5\n",
-       "EXjS9h8BbD8p6a3A8ZJOABYBjwGfH/moEYPLXUYRw0TSB4CNbP9H7SwRKyMFISIigFxDiIiIRgpC\n",
-       "REQAKQgREdFIQYiICCAFISIiGikIEREBpCBERETj/wPQ8mh2PbtLiwAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaaff1d0>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    },
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t trial 1 \t\n",
-      "\t R is :  \t1.1\n",
-      "\t H2 is :  Btu \t73.0\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.7\n",
-      "\t average of difference is :  \t16.1\n",
-      "\t nd1 is :  \t0.310559006211\n",
-      "\t number of diffusing units :  \t1.48\n",
-      "\t L/G is :  \t1.19\n",
-      "\t trial 2 \t\n",
-      "\t R4 is :  \t1.2\n",
-      "\t H2 is :  Btu \t76.5\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.2\n",
-      "\t average of difference is :  \t15.85\n",
-      "\t nd1 is :  \t0.315457413249\n",
-      "\t number of diffusing units :  \t1.56\n",
-      "\t L/G is :  \t1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=85;\n",
-    "T2=120;\n",
-    "R=0.93; # R=(L/G), for 1500 gpm\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "print\"\\t for 120percent of design \\t\"\n",
-    "R1=1.2*R;\n",
-    "print\"\\t R is : %.3f \\t\",R1\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R1*(T2-T1)); \n",
-    "print\"\\t H2 is : %.1f Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=87.2F\n",
-    "Hs=53.1; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is : %.1f \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=42; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is : %.1f \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is : %.1f \\t\",d\n",
-    "dT=(90-87.2); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is : %.3f \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.53;\n",
-    "print\"\\t number of diffusing units : %.2f \\t\",nd\n",
-    "print\"\\t for 80 percent of design \\t\"\n",
-    "R2=0.8*R;\n",
-    "print\"\\t R is : %.3f \\t\",R2\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R2*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=82.5F\n",
-    "Hs=47.2; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=40.8; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-82.5); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.92;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "X=[1.115, 0.93, 0.74];\n",
-    "Y=[1.53, 1.70, 1.92];\n",
-    "pyplot.plot(X,Y)\n",
-    "pyplot.xlabel('L/G')\n",
-    "pyplot.ylabel('nd')\n",
-    "pyplot.title('KxaV/L vs L/G')\n",
-    "pyplot.show()\n",
-    "print\"\\t trial 1 \\t\"\n",
-    "R3=1.1;\n",
-    "print\"\\t R is :  \\t\",R3\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R3*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.48;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.19; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "print\"\\t trial 2 \\t\"\n",
-    "R4=1.2;\n",
-    "print\"\\t R4 is :  \\t\",R4\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R4*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40.5; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.56;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.08; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.6 pgno:615"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t X1 :  lb/lb \t0.0806276339156\n",
-      "\t total water in inlet gas :  lb/hr \t120.941450873\n",
-      "\t H1 :  Btu/lb dry air \t174.00276\n",
-      "\t outlet gas humidity :  lb/lb \t0.0645021071324\n",
-      "\t pw :  psia \t1.38381840969\n",
-      "\t H2 :  Btu/lb dry air \t126.234717909\n",
-      "\t total heat load :  Btu/hr \t71652.063136\n",
-      "\t water loading :  lb/hr \t2047.20180389\n",
-      "\t interval 1 \t\n",
-      "\t C :  Btu/(lb)*(F) \t0.286282435262\n",
-      "\t haV :  Btu/(hr)*(F) \t27.2526231819\n",
-      "\t qc :  Btu/hr \t4905.47217274\n",
-      "\t delT :  F \t11.4233860657\n",
-      "\t T(0.05) :  F \t288.576613934\n",
-      "\t delt :  F \t2.39618398314\n",
-      "\t t(0.05) :  F \t117.603816017\n",
-      "\t interval 2 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc1 :  Btu/hr \t9318.91447199\n",
-      "\t delT1 :  F \t21.7009808594\n",
-      "\t T(0.15) :  F \t266.875633075\n",
-      "\t water diffused during interval :  lb/hr \t1.20784906429\n",
-      "\t water remaining :  lb/hr \t119.733601809\n",
-      "\t qd :  Btu/hr \t1240.46098903\n",
-      "\t q1 :  Btu/hr \t10559.375461\n",
-      "\t delt1 :  F \t5.15795533248\n",
-      "\t t(0.15) :  F \t112.445860684\n",
-      "\t X(112.5F) :  lb/lb \t0.079822401206\n",
-      "\t interval 3 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc2 :  Btu/hr \t8417.23279004\n",
-      "\t delT2 :  F \t19.6012323339\n",
-      "\t T(0.25) :  F \t247.274400741\n",
-      "\t water diffused during interval :  lb/hr \t3.23916482908\n",
-      "\t water remaining :  lb/hr \t116.49443698\n",
-      "\t qd1 :  Btu/hr \t3336.33977395\n",
-      "\t q2 :  Btu/hr \t11753.572564\n",
-      "\t delt2 :  F \t5.7412867367\n",
-      "\t t(0.25) :  F \t106.704573948\n",
-      "\t X(106.5F) :  lb/lb \t0.0776629579866\n",
-      "\t calculated diffusion :  \t18.1244724962\n",
-      "\t Using some standard low-pressure-drop data \t\n",
-      "\t tower height :  ft \t2.16762543941\n",
-      "\t cross section :  ft^2 \t33.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# basis 1ft^2 ground area\n",
-    "#Assumption: 20 per cent of the initial vapor content of the gas enters the water body\n",
-    "X1=(1.69/(14.7-1.69))*(18./29.);\n",
-    "print\"\\t X1 :  lb/lb \\t\",X1\n",
-    "G=1500.;\n",
-    "w1=G*X1;\n",
-    "print\"\\t total water in inlet gas :  lb/hr \\t\",w1\n",
-    "# The inlet gas is at 300F and a 120F dew point. Use 0.25 Btu/(lb)(DegF) for the specific heat of nitrogen\n",
-    "H1=(0.0807*120)+(0.0807*1025.8)+(0.45*0.0807*(300-120))+(0.25*300); # eq 17.55\n",
-    "print\"\\t H1 :  Btu/lb dry air \\t\",H1\n",
-    "X2=(w1*(1-.2)/G);\n",
-    "print\"\\t outlet gas humidity :  lb/lb \\t\",X2\n",
-    "pw=(X2*29*14.7/18)/(1+(X2*29/18));\n",
-    "print\"\\t pw :  psia \\t\",pw\n",
-    "Tw=112.9; # F, from table 7 for above pw\n",
-    "# The outlet gas has a temperature of 200DegF and a 112.9DegF dew point\n",
-    "H2=(X2*Tw)+(X2*1029.8)+(X2*0.45*(200-Tw))+(0.25*200); # eq 17.55\n",
-    "print\"\\t H2 :  Btu/lb dry air \\t\",H2\n",
-    "q=G*(H1-H2);\n",
-    "print\"\\t total heat load :  Btu/hr \\t\",q\n",
-    "w2=q/(120-85);\n",
-    "print\"\\t water loading :  lb/hr \\t\",w2\n",
-    "print\"\\t interval 1 \\t\"\n",
-    "# (Kxa*delV/L)= 0 t0 0.05\n",
-    "nd=0.05; # nd=Kxa*V/L\n",
-    "Le=0.93; # fig 17.4 at 300F\n",
-    "C=(0.25)+(0.45*X1);\n",
-    "print\"\\t C :  Btu/(lb)*(F) \\t\",C\n",
-    "haV=(nd*w2*Le*C);\n",
-    "print\"\\t haV :  Btu/(hr)*(F) \\t\",haV\n",
-    "qc=(haV*(300-120));\n",
-    "print\"\\t qc :  Btu/hr \\t\",qc\n",
-    "delT=(qc/(C*G));\n",
-    "print\"\\t delT :  F \\t\",delT\n",
-    "T1=(300-delT);\n",
-    "print\"\\t T(0.05) :  F \\t\",T1\n",
-    "delt=(qc/w2);\n",
-    "print\"\\t delt :  F \\t\",delt\n",
-    "t1=(120-delt);\n",
-    "print\"\\t t(0.05) :  F \\t\",t1\n",
-    "print\"\\t interval 2 \\t\"\n",
-    "# (Kxa*delV/L)= 0.05 to 0.15\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc1=(haV1*(T1-t1));\n",
-    "print\"\\t qc1 :  Btu/hr \\t\",qc1\n",
-    "delT1=(qc1/(C*G));\n",
-    "print\"\\t delT1 :  F \\t\",delT1\n",
-    "T2=(T1-delT1);\n",
-    "print\"\\t T(0.15) :  F \\t\",T2\n",
-    "X3=0.0748; # at 117.6F\n",
-    "w3=(nd1*w2*(0.0807-X3));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w3\n",
-    "w4=(w1-w3);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w4\n",
-    "l1=1027; # Btu/lb, l1= lamda at 117.6F\n",
-    "qd=(w3*l1);\n",
-    "print\"\\t qd :  Btu/hr \\t\",qd\n",
-    "q1=(qd+qc1);\n",
-    "print\"\\t q1 :  Btu/hr \\t\",q1\n",
-    "delt1=(q1/w2);\n",
-    "print\"\\t delt1 :  F \\t\",delt1\n",
-    "t2=(t1-delt1);\n",
-    "print\"\\t t(0.15) :  F \\t\",t2\n",
-    "X4=0.0640; # at 112.5\n",
-    "X5=(w4/G);\n",
-    "print\"\\t X(112.5F) :  lb/lb \\t\",X5\n",
-    "print\"\\t interval 3 \\t\"\n",
-    "# (Kxa*delV/L)= 0.15 to 0.25\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc2=(haV1*(T2-t2));\n",
-    "print\"\\t qc2 :  Btu/hr \\t\",qc2\n",
-    "delT2=(qc2/(C*G));\n",
-    "print\"\\t delT2 :  F \\t\",delT2\n",
-    "T3=(T2-delT2);\n",
-    "print\"\\t T(0.25) :  F \\t\",T3\n",
-    "w5=(nd1*w2*(X5-X4));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w5\n",
-    "w6=(w4-w5);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w6\n",
-    "l2=1030; # Btu/lb, l1= lamda at 112.5F\n",
-    "qd1=(w5*l2);\n",
-    "print\"\\t qd1 :  Btu/hr \\t\",qd1\n",
-    "q2=(qd1+qc2);\n",
-    "print\"\\t q2 :  Btu/hr \\t\",q2\n",
-    "delt2=(q2/w2);\n",
-    "print\"\\t delt2 :  F \\t\",delt2\n",
-    "t3=(t2-delt2);\n",
-    "print\"\\t t(0.25) :  F \\t\",t3\n",
-    "X6=0.0533; # at 106.5\n",
-    "X7=(w6/G);\n",
-    "print\"\\t X(106.5F) :  lb/lb \\t\",X7\n",
-    "# The calculations of the remaining intervals until a. gas temperature of 200DegF is reached are shown in Fig. 17.17\n",
-    "w7=21.92; # total water diffused from table in solution\n",
-    "d=(w7/w1)*100;\n",
-    "print\"\\t calculated diffusion :  \\t\",d\n",
-    "print\"\\t Using some standard low-pressure-drop data \\t\"\n",
-    "# For G = 1500, extrapolate to L = 2040 on logarithmic coordinates. Kxa = 510.\n",
-    "ndt=.54; # from 1st table in solution\n",
-    "Kxa=510; # from 2nd table in solution\n",
-    "Z=(ndt*w2/Kxa);\n",
-    "print\"\\t tower height :  ft \\t\",Z\n",
-    "A=(50000/G);\n",
-    "print\"\\t cross section :  ft^2 \\t\",round(A,1)\n",
-    "# end\n",
-    "\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.7 pgno:620"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t sensible heat :  Btu/hr \t4200000.0\n",
-      "\t approximate diffusion :  Btu/hr \t756166.666667\n",
-      "\t total heat :  Btu/hr \t4956166.66667\n",
-      "\t total water quantity :  lb/hr \t141604.761905\n",
-      "\t tower cross section :  ft**2 \t69.4140989729\n",
-      "\t new gas rate :  lb/(hr)(ft**2) \t720.314759391\n",
-      "\t LMTD :  \t241.213395056\n",
-      "\t haV/L :  \t0.145099736239\n",
-      "\t number diffusion units :  \t0.557218649152\n",
-      "\t height of tower :  ft \t5.28709788033\n",
-      " ground dimensions :  ft \t1.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "C=0.28; # assumption\n",
-    "w=50000.; # lb/hr\n",
-    "G=1500.;\n",
-    "Qs=(w*C*(500-200));\n",
-    "Qd=(w/G)*(22685); # qd=22685, from previous prblm\n",
-    "from math import log\n",
-    "print\"\\t sensible heat :  Btu/hr \\t\",Qs\n",
-    "print\"\\t approximate diffusion :  Btu/hr \\t\",Qd\n",
-    "Q=(Qs+Qd);\n",
-    "print\"\\t total heat :  Btu/hr \\t\",Q\n",
-    "# an allowance as high as 30 per cent of the sensible load can be made and the excess water compensated for by throttling when the tower is in operation\n",
-    "w1=(Q/(120-85));\n",
-    "print\"\\t total water quantity :  lb/hr \\t\",w1\n",
-    "# If the maximum liquid loading is taken as 2040 lb/(hr)(ft'!), the required tower cross section\n",
-    "A=(w1/2040);\n",
-    "print\"\\t tower cross section :  ft**2 \\t\",A\n",
-    "w3=(w/A);\n",
-    "print\"\\t new gas rate :  lb/(hr)(ft**2) \\t\",w3\n",
-    "# The two terminal temperature differences are (200 - 85) and (500 - 120).\n",
-    "LMTD=((500-120)-(200-85))/(log((500-120)/(200-85)));\n",
-    "print\"\\t LMTD :  \\t\",LMTD\n",
-    "dt=35;\n",
-    "N=(dt/LMTD); # eq 17.88\n",
-    "print\"\\t haV/L :  \\t\",N\n",
-    "Le=0.93;\n",
-    "nd=(N/(C*Le));\n",
-    "print\"\\t number diffusion units :  \\t\",nd\n",
-    "# By extrapolation for G = 718 and L = 2040,Kxa=215\n",
-    "L=2040;\n",
-    "Kxa=215;\n",
-    "Z=(nd*L/Kxa); # calculation mistake\n",
-    "print\"\\t height of tower :  ft \\t\",Z\n",
-    "di=(A)**(1/2);\n",
-    "print\" ground dimensions :  ft \\t\",di\n",
-    "# ground dimensions are 5.8*8.3*8.3 ft\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_2.ipynb
deleted file mode 100755
index 45f8b0e5..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_2.ipynb
+++ /dev/null
@@ -1,856 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 17 Direct Contact Transfer : Cooling Tower"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 71.1 pgno:585"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.1 \n",
-      "\n",
-      "\t humidity is :  lb water/lb air  0.0186996126364\n",
-      "\t enthalpy at 75F is :  Btu/lb dry air  39.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.1 \\n\"\n",
-    "pw=0.4298; # psia, at 75F, table 7\n",
-    "pt=14.696; # psia\n",
-    "t=75.;\n",
-    "Mw=18.;\n",
-    "Ma=29.;\n",
-    "X=(pw/(pt-pw))*(Mw/Ma);\n",
-    "print\"\\t humidity is :  lb water/lb air \",X\n",
-    "H=(X*t)+(1051.5*X)+(0.24*t); # eq 17.54\n",
-    "print\"\\t enthalpy at 75F is :  Btu/lb dry air \",round(H,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.2 Pgno:602"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 15,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t by numerical integration \t\n",
-      "\t R is :  \t0.93005952381\n",
-      "\t H2 is :  Btu \t71.6520833333\n",
-      "\t difference is :  \t10.9\n",
-      "\t difference is :  \t13.0\n",
-      "\t average of difference is :  \t11.95\n",
-      "\t nd1 is :  \t0.418410041841\n",
-      "\t number of diffusing units :  \t1.7\n",
-      "\t log mean enthalpy difference \t\n",
-      "\t log mean of enthalpy :  Btu/lb \t25.6654878432\n",
-      "\t number of diffusing units are :  \t1.36\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t by numerical integration \\t\"\n",
-    "T1=85.;\n",
-    "T2=120.;\n",
-    "A=576.; # ground area, from fig 17.12\n",
-    "L=1500.*(500./576.);\n",
-    "G=1400.;\n",
-    "R=(L/G);\n",
-    "from math import log10\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "H1=39.1; # fig 17.12\n",
-    "H2=H1+(R*(T2-T1));\n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # fig 17.12\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=43.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=5; # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.70;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "print\"\\t log mean enthalpy difference \\t\"\n",
-    "dt=49.9; # diff. of enthalpies at top of the tower, from table in solution\n",
-    "db=10.9; # diff of enthalpies at bottom of the tower,from table in solution\n",
-    "LME=(dt-db)/(2.3*log10(dt/db));\n",
-    "print\"\\t log mean of enthalpy :  Btu/lb \\t\",LME\n",
-    "nd=(T2-T1)/(LME);\n",
-    "print\"\\t number of diffusing units are :  \\t\",round(nd,2)\n",
-    "# The error is naturally larger the greater the range\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.3 pgno:604"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 16,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Z is : ft \t19.2469565217\n",
-      "\t height of diffusion unit :  ft \t11.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# Since the loading is based on 1 ft2 of ground area\n",
-    "nd=1.7;\n",
-    "L=1302;\n",
-    "Kxa=115;\n",
-    "Z=(nd*L)/(Kxa);\n",
-    "print\"\\t Z is : ft \\t\",Z\n",
-    "HDU=(Z/nd);\n",
-    "print\"\\t height of diffusion unit :  ft \\t\",round(HDU,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.4 pgno:605"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t difference is :  \t13.0\n",
-      "\t difference is :  \t14.3\n",
-      "\t average of difference is :  \t13.65\n",
-      "\t nd1 is :  \t0.417582417582\n",
-      "\t number of diffusing units :  \t1.72\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=79.3F\n",
-    "Hs=43.4; # fig 17.12\n",
-    "H=30.4; # fig 17.12\n",
-    "d1=(Hs-H);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=35.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-79.3); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.72;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.5 pgno:609"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for 120percent of design \t\n",
-      "\t R is : %.3f \t1.116\n",
-      "\t H2 is : %.1f Btu \t78.16\n",
-      "\t difference is : %.1f \t14.0\n",
-      "\t difference is : %.1f \t14.7\n",
-      "\t average of difference is : %.1f \t14.35\n",
-      "\t nd1 is : %.3f \t0.19512195122\n",
-      "\t number of diffusing units : %.2f \t1.53\n",
-      "\t for 80 percent of design \t\n",
-      "\t R is : %.3f \t0.744\n",
-      "\t H2 is :  Btu \t65.14\n",
-      "\t difference is :  \t8.1\n",
-      "\t difference is :  \t9.2\n",
-      "\t average of difference is :  \t8.65\n",
-      "\t nd1 is :  \t0.28901734104\n",
-      "\t number of diffusing units :  \t1.92\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAYQAAAEZCAYAAACXRVJOAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XuYXVV9//H3pwHEULk1SC2gqYjIrYBIVC4yBYSAF7wD\n",
-       "XpDG8osWLFaoVJ4qsWrRKogCLXgJxQIBFREQ5GYZDXciIQQhCJLUIBi5CxIggc/vj7UDY5jJnEnm\n",
-       "zDpn5vN6nnlyzt77nPPJfpL5nrX2XmvJNhEREX9WO0BERHSGFISIiABSECIiopGCEBERQApCREQ0\n",
-       "UhAiIgJIQYiIiEYKQkREACkI0aUkLZC0R5/nB0h6SNKuq/CeB0ia38/21ST9XtK+fbZ9WtIXJfVI\n",
-       "Wriyn7kSGQ+WNHMF+9eQdL+k8c3zN0u6UtIfJD0gabakT0l60Uhlju6RghDdys0Pkj4MnATsa3vA\n",
-       "X5YtOA9YV9Juy22fDDwDXNJn277ARavwWe3yJmC27SckvRf4PnAG8HLbE4D9gY2BTSpmjA6VghDd\n",
-       "TJKmAl8F9rJ9XbNxf0l3S3pJ83wfSfdJ+ovm+dcl/UbSo5JmSdoFwPZTwPeAg5b7nIOAs2w/27x+\n",
-       "PeDVwLVDCLq/pBuX2/ZPks5vHu8r6ZfNN/l7JB0x9NMBlEJ1cfP4eOBztr9j+xEA27+y/Y+271rJ\n",
-       "949RLAUhutk/AJ8Ddrd907KNts8BrgG+0RSBbwMfsf1gc8gNwLbAesBZwPclrdHsOx14j6Q1ASSt\n",
-       "A7y12b7M3sAVHtpEYBcAm0t6VZ9t7wfObB5/B/h/ttcGtgL+dwjv3dc+wEWSXgNsBJy7ku8TY1AK\n",
-       "QnQrAXtSvqXf2s/+Q4HdgSuBC2wv+9aM7TNtP2z7WdvHAy8CNm/2XQMsAt7ZHP4+4A7bt/R577fw\n",
-       "/LfwltheDJwPHAggabPmMy9oDnka2ErS2rYftT17KO/fvOemwGq27wQmNJt/12f/2ZIelvRHSR8c\n",
-       "6vvH6JeCEN3KwEcpv1S//YKd9qPAD4CtgeP67pN0pKTbJD0i6WFgHZ7/BQrwXZ7vNvpQ83zZa/+M\n",
-       "Uoj6Xk9o1Vk0BYHSOjjP9pPN83dTunsWSOqV9IaVeP++3UXLWkMvW7bT9gG21wNuIv/3ox/5RxHd\n",
-       "bBGwB7CrpP/su0PSdsDfUX4Jn9hn+67APwPvtb1u8wvyUUqLY5kzgD0kvRF4Pc936wDsCPxfn+6n\n",
-       "obgC2EDStsABTTYAbM+y/Q5gA+BHlGsZQ9W3INwB/JZSaCJakoIQXc32fZSiMFnS8QBN//8ZwKeB\n",
-       "KcBGkj7WvOQlwFLggeYWzc8Cay/3nguAq4AZwGW2f99n977Aj5fPIelFktZc9jNA1iWUu36+Srl+\n",
-       "cXnz2tUlfUDSOrafAR6j3NU0EC3/ec1tpjtSushoLoAfARwj6e8lradiM2DDFbx3jGGrteuNJU2n\n",
-       "9LX+3vY2/exfD5gOvBJ4Ephi+5fNvgXAHyj/KZbYntSunNH9bC+UtDvwc0lPAmtSvsWfCtD0l18p\n",
-       "6TJKV88lwK+APwJfA37Tz9ueTvn3+c/Lbd8XmNr34ykXbxf33SZpM9t39/O+ZwE/B05edtdS44PA\n",
-       "iZLGAfOADwz01wV2Wv7zgLcD19p++rmN9vckPUopjF8Dnmr+rqdSutMi/oTatWJa0zR/HPjuAAXh\n",
-       "K8AfbH9e0uaU/yB7NvvmAzvYfqgt4SJWgqQNgZtsb1Q7y/IknQzMtX1K7SzRvdrWZdQMEHp4BYds\n",
-       "wfPN2zuAiZI26LNf/b4qop61gU/WDjGAmykD6yJWWs1rCHOAdwFImgS8gjKCEkoT+Ipm0NAhlfJF\n",
-       "/AnbdzZjHDqO7W/ZXlQ7R3S3tl1DaMGXgK9Lmg3MBWbz/IW0XWzf27QYLpc0bxWnJIiIiEFUKwi2\n",
-       "H6PcAQI8d93g7mbfvc2f90s6D5gEvKAgSGrPBZCIiFHO9gu65asVhGZKgMW2n266hX5m+/Hm9rlx\n",
-       "th+TtBawF2V6gn7195eKPyVpmu1ptXN0g5yr1uQ8taZTz9NAX6bbedvpDGA3YEIzPfAxwOoAze2A\n",
-       "WwL/3QS7FfhI89INgfMkLct3pu3L2pUzIiKKthUE2wcOsv9amvljlts+H9iuXbkiIqJ/Gak8NvTW\n",
-       "DtBFemsH6BK9tQN0id7aAYaibQPTRoIk5xpCRMTQDPS7My2EiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICSEGIiIhGCkJERAApCEMm/elyixERo0UKwhBIrAvcLg24vGFERNdKQRgCm0coa+pOkzhZ4kW1\n",
-       "M0VEDJcUhCGymQPsSFlY/ecSL68cKSJiWKQgrISmpfBO4FzgBom9KkeKiFhlmdxulTPQA5wFnAJ8\n",
-       "webZmnkiIgYz0O/OFIRhycHLgO8BjwMftHmwcqSIiAGN+GynkqZLWiRp7gD715N0nqQ5kq6XtFWf\n",
-       "fZMlzZN0p6Sj2pVxuNjcB+wO/BL4hcSOlSNFRAxZO68hnAZMXsH+o4GbbG8LHAR8HUDSOOCk5rVb\n",
-       "AgdK2qKNOYeFzRKbI4EjgIslpkpUb71ERLSqbQXB9kzg4RUcsgVwZXPsHcBESS8FJgF32V5gewlw\n",
-       "NrBfu3ION5tzgZ2Bw4DTJcZXjhQR0ZKadxnNAd4FIGkS8ApgY8rtnAv7HHdPs61r2PwKeAMg4HqJ\n",
-       "V1eOFBExqNUqfvaXgK9Lmg3MBWYDzwBDusotaVqfp722e4cr4Kqw+aPEQcBU4GqJqTY/rJ0rIsYe\n",
-       "ST1Az2DHVSsIth8Dpix7Lmk+8GvgxcAmfQ7dhNJKGOh9prUp4iqzMXCKxC+A70vsBHzaZknlaBEx\n",
-       "hjRflHuXPZd0TH/HVesykrSOpDWax4cAP7P9ODAL2EzSxGb//sAFtXIOB5sbgR2ArYCfNrepRkR0\n",
-       "lHbedjoDuAbYXNJCSVMkTZU0tTlkS2CupHnA3sDhALaXUi7IXgrcBpxj+/Z25RwpzdiEtwBXUG5N\n",
-       "3a1ypIiIP5GBaRVI7A2cDhwHfLXpWoqIGBEZqdxhmknxvg/cCxxs82jlSBExRoz4SOVYMZvfAG+i\n",
-       "FIRZEn9TOVJEjHEpCBXZPGVzKDCNcrH5w5UjRcQYli6jDiGxNWU67V7gcJsn6yaKiNEqXUYdzuZW\n",
-       "ysI76wNXSUysmygixpoUhA5i8wfgfcCZlCkv9q0cKSLGkHQZdSiJXSgT+00HPmfzTOVIETFK5LbT\n",
-       "LiTxl8AMYAnwAZv7K0eKiFEg1xC6kM3vgDcDN1FGN7+hcqSIGMVSEDqczVKbfwE+DlwgcVgW3omI\n",
-       "dkiXUReR2JRya+rtwCE2j1eOFBFdKF1Go4DNr4E3AouBGyReUzlSRIwiKQhdxmaxzRTKxHgzJd5X\n",
-       "O1NEjA7pMupiEq8FfkBZL+JTNk9XjhQRXSBdRqOQzU2UhXc2Ba6Uumvt6YjoLCkIXc7mYWA/4CLK\n",
-       "rKl7VI4UEV2qnSumTZe0SNLcAfZPkHSJpJsl3Srp4D77Fki6RdJsSTe0K+NoYfOszb8DHwTOkDha\n",
-       "SrGPiKFp2zUESbsCjwPftb1NP/unAS+y/WlJE4A7gA1tL5U0H9jB9kODfMaYvobQH4mNge8BDwIH\n",
-       "NS2IiIjnjPg1BNszYYW/jO4D1m4erw082KynvEx+0a8Em3uAHuBuShfS9nUTRUS3qNmt8C1gK0n3\n",
-       "AnOAw/vsM3CFpFmSDqmSrovZPG1zOHA0cJnER2pniojOt1rFzz4auNl2j6RNgcslbWv7MWBn2/dJ\n",
-       "2qDZPq9pcbxA0/W0TK/t3rYn7xI250jcApwrsRNwmM3i2rkiYmRJ6qH0HKz4uHaOQ5A0EbhwgGsI\n",
-       "FwNftH118/ynwFG2Zy133DHA47aP6+c9cg2hBRJ/TmmRvQZ4TzPiOSLGqE4chzAP2BNA0obA5sDd\n",
-       "ksZLekmzfS1gL6DfO5WiNc2cR++nrK1wrcTbK0eKiA7UzruMZgC7AROARcAxwOoAtk9t7iw6DXg5\n",
-       "pTAda/ssSa8Efti8zWrAmbaPHeAz0kIYIok3AudQVmX7jM3SQV4SEaNMFsiJ50hsAJwFjAMOtFlU\n",
-       "OVJEjKBO7DKKSpqV1yYDV1MW3tm5cqSI6ABpIYxxEm+hXFv4EnCCTff+g4iIlqTLKAYk8deUWVPv\n",
-       "Bj5i84fKkSKijdJlFAOymQ/sDDxEWXhnq8qRIqKCFIQAwOZJm6mUrqNeiQ/UzhQRIytdRvECEttS\n",
-       "upAuBY6weapypIgYRukyipbZzAF2BDYGfi7x8sqRImIEpCBEv2weAd4JnEu5rrBX5UgR0WbpMopB\n",
-       "SfRQBrKdAnzB5tm6iSJiVeS201glEi+jLLzzGPAhmwcrR4qIlZRrCLFKbO4Ddgduo4xu3rFypIgY\n",
-       "ZikI0TKbJTZHAkcAF0tMlbKyXcRokS6jWCkSr6ZccJ4NfNTmicqRIqJF6TKKYWXzK+ANlLWvr28K\n",
-       "RER0sRSEWGk2fwQOAk4GrpZ4V+VIEbEK0mUUw6K5yPx9ygjnT9ssqRwpIgYw4l1GkqZLWiSp3+Uv\n",
-       "JU2QdImkmyXdKungPvsmS5on6U5JR7UrYwwfmxuBHYCtgJ82t6lGRBdpZ5fRaZRFWAZyGDDb9nZA\n",
-       "D3CcpNUkjQNOal67JXCgpC3amDOGSTM24S3AFcAsid0qR4qIIWhbQbA9E3h4BYfcB6zdPF4beND2\n",
-       "UmAScJftBbaXAGcD+7UrZwwvm2dt/g2YApwj8c+5NTWiO9S8qPwtYCtJ9wJzgMOb7RsBC/scd0+z\n",
-       "LbqIzaWU4v4e4IcS61SOFBGDWK3iZx8N3Gy7R9KmwOWSth3qm0ia1udpr+3eYcoXq8jmNxJvAo6n\n",
-       "dCG92+aW2rkixhpJPZSu+RWqWRB2Ar4IYPvXkuYDm1NaBJv0OW6TZlu/bE9rY8ZYRc1aCoc2C+78\n",
-       "VOJIm9Nr54oYS5ovyr3Lnks6pr/janYZzQP2BJC0IaUY3A3MAjaTNFHSGsD+wAXVUsawsDkT+Fvg\n",
-       "aIlTJdasnSki/lTbxiFImgHsBkwAFgHHAKsD2D5V0gTKnUgvpxSmY22f1bx2H+AEYBzwHdvHDvAZ\n",
-       "GYfQZSTWBr4D/DXwHpsFdRNFjD2Z/jo6RnPX0SeAfwH+zubiypEixpQUhOg4ErtQbiueDnzO5pnK\n",
-       "kSLGhBSE6EgSG1KKwhLgAzb3V44UMeplttPoSDaLgDcDN1EW3nlD5UgRY1YKQlRns9TmXyjTmVwg\n",
-       "cVhGN0eMvHQZRUeR2JSy8M7twCE2j1eOFDHqpMsouoLNr4E3AouBGyReUzlSxJiRghAdx2axzRTg\n",
-       "OGCmxPtqZ4oYC9JlFB1N4rWURXcuAD5l83TlSBFdL11G0ZVsbqIsvLMpcKWUmW8j2iUFITqezcOU\n",
-       "NTEuosyaukflSBGjUrqMoqs0xeAM4BvAl22erRwpoutkpHKMGhIbA98DHgQOaloQEdGiXEOIUcPm\n",
-       "HspiH7+mdCFtXzdRxOiQghBdyeZpm09QVt67TOIjtTNFdLt0GUXXk9iCMrr5WuAwm8WVI0V0tBHv\n",
-       "MpI0XdIiSXMH2H+kpNnNz1xJSyWt2+xbIOmWZt8N7coYo4PN7cAkYDxwTTP9RUQMUTtXTNsVeBz4\n",
-       "ru1tBjn2rcAnbC9bUnM+sIPthwZ5XVoI8ZxmQrzDgM8Af29n6dWI/ox4C8H2TGj57o/3AzOW25Zf\n",
-       "9DEkNrY5EXg7cJLEsRKr1c4V0S2qX1SWNB7Ym9IHvIyBKyTNknRInWTRrWyuo4xufh3lgvOGlSNF\n",
-       "dIXqBQF4G3CV7Uf6bNvZ9vbAPsChTfdTRMualdcmA1dTbk3duXKkiI7XCc3pA1iuu8j2fc2f90s6\n",
-       "j3LBcGZ/L5Y0rc/TXtu97YkZ3aZZo/kzEtcBP5T4EnCCTffeWhexEiT1UMburPi4dt52KmkicOFA\n",
-       "F5UlrQPcDWxse3GzbTwwzvZjktYCLgM+Z/uyfl6fi8rREom/psyaejcwxeaxypEiqqlx2+kM4Bpg\n",
-       "c0kLJU2RNFXS1D6HvQO4dFkxaGwIzJR0M3A98OP+ikHEUNjMB3YGHgJulNiqcqSIjpOBaTHmSBwM\n",
-       "fAX4hM2ZleNEjLhMbhfRh8S2lC6kS4EjbJ6qHClixGRyu4g+bOYAOwIbAT+XeHnlSBHVpSDEmGXz\n",
-       "CPAuSkvhBom9KkeKqCpdRhGARA9wFnAK8IUsvBOj2ZCvIQw0KV3Dtv9muMKtrBSEGE4SLwPOoczB\n",
-       "9SGbBytHimiLgX53rmhg2tuaP/+h+fN/KPMLfWCYs0V0BJv7miU6/x34hcR7bW6snStipAzaZSTp\n",
-       "ZtvbLbdtdjO1RFVpIUS7SLwb+C/KzKnfzOjmGE1W5S4jSdqlz5OdyUykMcrZnAvsQplO+3SJ8ZUj\n",
-       "RbRdKy2EHYDpwLrNpoeBKbZvanO2QaWFEO0msRblQvO2wLtt7qwcKWKVrfTANElrAu8GJgITgEco\n",
-       "F5X/rQ05hyQFIUZCs/DOVODfgI/a/LBypIhVsjIXlZc5n1IEfgHcM9zBIjpdc/3gFIlfAN+X2An4\n",
-       "tM2SytEihlUrLYRbbW89QnmGJC2EGGkSfwGcAawF7G9zX+VIEUO2KheVr5FUfcxBRCdoxia8BbiC\n",
-       "svDObpUjRQybVloItwOvAubDcxOAZWBajHkSewOnA8cBX82tqdEtVuWi8sT+ttteMBzBVkUKQtTW\n",
-       "TIr3feBe4GCbRytHihhUpr+OaBOJFwHHA3tRbk29pXKkiBWqsWLadEmLBpoTSdKRkmY3P3MlLZW0\n",
-       "brNvsqR5ku6UdFS7MkYMB5unbA4FpgE/lTiocqSIldK2FoKkXSmThH13oDWV+xz7VuATtveUNA64\n",
-       "A9gT+C1wI3Cg7dv7eV1aCNFRJLYGzgV6gcNtnqybKOKFRryFYHsmZVRzK94PzGgeTwLusr3A9hLg\n",
-       "bGC/NkSMGHY2t1IW3lkfuEpiYt1EEa2rvkCOpPHA3pRvVVBWsFrY55B7mm0RXcHmD8D7KOMVrpfY\n",
-       "t3KkiJZULwiUabavsv1I87x7r3JHNGxscwJl2pdvSpwosU7tXBEr0srUFe12AM93F0G5brBJn+eb\n",
-       "sIIpMyRN6/O013bvcIaLWBU2V0lsC3wJuE3iSODsjFmIkSSpB+gZ9Lh23nbajGG4cKCLypLWAe4G\n",
-       "Nra9uNm2GuWi8h6Ue7tvIBeVYxRo5kD6L+B+4FCbOypHijGqxm2nM4BrgM0lLZQ0RdJUSVP7HPYO\n",
-       "4NJlxQDA9lLKHPSXArcB5/RXDCK6jc01wA7ARcDVEp+XeHHlWBHPycC0iAokNga+BrwWOMzmJ5Uj\n",
-       "xRiSkcoRHUhiMnAyMBv4hJ0p5qP9RrzLKCIGZ3MJsDWle/RmiU9KHXGzR4xBaSFEdAiJVwP/CWwA\n",
-       "fKy55hAx7NJlFNEFmuU696dMqf0T4KhmDYaIYZMuo4gu0AxoOxvYEniCMnZhipT/q9F+aSFEdDCJ\n",
-       "11LGLiyhdCP1O3twxFCkhRDRhWxuAnaizIv0U4mvSvx55VgxSqUgRHQ4m2dsTgG2AV5K6UZ6V3O9\n",
-       "IWLYpMsoostI9FDuRpoPfNzm7rqJotukyyhilLDpBbYDrgJulPjXZhnPiFWSghDRhWyetjmWMjfS\n",
-       "JGCOxO6VY0WXS5dRxCggsR/wDUqr4Qib31WOFB0sXUYRo5jN+ZSxCwuBuRKHSoyrHCu6TFoIEaOM\n",
-       "xFaUi85rAR+1mVU5UnSYtBAixgibX1JWxzoR+LHEyRLr1k0V3SAFIWIUaqbAOJ3SjTQOuF3igxm7\n",
-       "ECvSti4jSdOBtwC/X8ESmj2URUJWBx6w3dNsXwD8AXgGWGJ70gCvT5dRRAsk3kCZAuNh4B9s5lWO\n",
-       "FBWN+GynknYFHge+219BkLQucDWwt+17JE2w/UCzbz6wg+2HBvmMFISIFjXrLBwKfAY4FfiizRN1\n",
-       "U0UNI34NwfZMyreRgbwfONf2Pc3xDyy3P7/oI4aRzVKbrwPbAq8CbpV4S+VY0UFqXkPYDFhf0pWS\n",
-       "Zkn6UJ99Bq5oth9SKV/EqGTzW5v9gY8CJ0j8UGKT2rmivppL9a1OWWB8D2A8cK2k62zfCexi+15J\n",
-       "GwCXS5rXtDheQNK0Pk97bfe2OXfEqGBzmcQ2wFHAbIkvAyfYLKkcLYZZc722Z9Dj2jkOQdJE4MIB\n",
-       "riEcBbzY9rTm+beBS2z/YLnjjgEet31cP++RawgRw0BiM+Ak4K8o6y5cVTlStFEnjkM4H9hF0jhJ\n",
-       "44HXA7dJGi/pJQCS1gL2giwKEtFONncCk4HPA2dLTJfYoHKsGGFtKwiSZgDXAJtLWihpiqSpkqYC\n",
-       "2J4HXALcAlwPfMv2bcBfAjMl3dxs/7Hty9qVMyKKZuzC9yhjFx4FfilxSJbvHDsydUVE9EtiO8rY\n",
-       "BVO6keZUjhTDpBO7jCKig9ncDOwM/DdwucTxEi+pmyraKQUhIgZk86zNN4GtgfUpU2C8J1NgjE7p\n",
-       "MoqIlkm8idKN9BvgMJtfV44UKyFdRhGxymx+Tlm+80rgeonPZvnO0SMFISKGxGaJzX9Qlu98LWVB\n",
-       "nj0rx4phkC6jiFglEm+jLN95HWX5znsrR4pBpMsoItrC5kJgK2A+cIvEPzYzq0aXSQshIoaNxBaU\n",
-       "5TvXoSzfeUPlSNGPtBAiou1sbgd2pyx8db7EKRLrVY4VLUpBiIhh1UyB8T+UKTBMGbtwUMYudL50\n",
-       "GUVEW0lMooxdeIyyfOdtlSONeekyiogqmusIk4BzgZ9JHCsxvnKs6EcKQkS0nc0zNicCfwO8Arit\n",
-       "uV01Oki6jCJixDUD2U4G5gH/aPN/lSONKekyioiOYXMFpbUwC/iFxFESa1SONealhRARVUlsSlm+\n",
-       "8+WUi84/qxxp1BvxFoKk6ZIWSRpw+UtJPZJmS7pVUm+f7ZMlzZN0Z7P2ckSMUs2MqfsCnwXOkDhd\n",
-       "4qWVY41J7ewyOo2yRmu/JK1L6UN8m+2tgfc028dRvi1MptzHfKCkLdqYMyIqa8YunEv5P/8AcKvE\n",
-       "1CzfObLadrJtzwQeXsEh7wfOtX1Pc/wDzfZJwF22F9heApwN7NeunBHROWweszkCeDPwYeAaie0r\n",
-       "xxozalbfzYD1JV0paZakDzXbNwIW9jnunmZbRIwRzfrNuwDfBi6ROEFi7cqxRr2aMxKuTplLfQ9g\n",
-       "PHCtpOsoQ91bJmlan6e9tnuHK2BE1GPzLPBtiR8BX6aMXTgC+J49tN8TY52kHqBnsONqFoSFwAO2\n",
-       "FwOLJf0c2JbSItikz3GbNNv6ZXtaO0NGRF02DwAfkdiFMgXGFInDbO6sHK1rNF+Ue5c9l3RMf8fV\n",
-       "7DI6H9hF0jhJ44HXA7dR7kveTNJESWsA+wMXVMwZER3A5ipKr8LlwLUS0yTWrBxrVGnnbaczgGuA\n",
-       "zSUtlDRF0lRJUwFszwMuAW4Brge+Zfs220uBw4BLKQXiHNu3tytnRHSPZvnOrwLbA9tQ7kbau3Ks\n",
-       "USMD0yKia0nsS7lNfRbwTza/rRypK2TqiogYdWwuBrYGfgXMkfhElu9ceWkhRMSoIPEayvKd6wMf\n",
-       "s7m2cqSOlRZCRIxqNvMot7F/BThX4psS61eO1VVSECJi1GimwDiTMgXG05SxCwdn+c7WpMsoIkYt\n",
-       "idcBpwBPULqRflk5UkdIl1FEjDk2syhjnM4GeiW+LLFW5VgdKwUhIka1ZvnO/6SMW9iI0o30jnQj\n",
-       "vVC6jCJiTJHYnXI30p3Ax20W1E008tJlFBEB2PwvZd606yjLdx6d5TuLFISIGHNsnrL5IrAjsDNl\n",
-       "UNvfVo5VXbqMImJMa64lvAP4OvAz4EibRXVTtVe6jCIi+tGMXTiPMnbhd5QJ8z4mMa5ytBGXFkJE\n",
-       "RB8S21DWXVgD+KjNTZUjDbu0ECIiWmAzF3gTpSj8ROJEiXUqxxoRKQgREcuxedbmNEo30pqUsQsH\n",
-       "jvaxC+kyiogYhMROlBbD/cChNndUjrRKRrzLSNJ0SYskzR1gf4+kRyXNbn4+02ffAkm3NNtvaFfG\n",
-       "iIhW2FwD7ABcBFwt8XmJF1eONeza2WV0GjB5kGN+Znv75ufzfbYb6Gm2T2pfxIiI1tgstfkasB3w\n",
-       "GsrdSPtUjjWs2lYQbM8EHh7ksBV196QrKCI6js09Nu+lrP1+ksQPJDaunWs41LyobGAnSXMkXSxp\n",
-       "y+X2XSFplqRDKuWLiBiQzU8oy3feBtws8cluX76zZvibgE1sPyFpH+BHwKubfTvbvk/SBsDlkuY1\n",
-       "LY4XkDStz9Ne273tDB0RsYzNYuCzEmdQJsz7sMTHmmsOHUNSD9Az6HHtvMtI0kTgQtvbtHDsfGAH\n",
-       "2w8tt/0Y4HHbx/XzmtxlFBEdobkldX/gOOAnwFE2D9ZN1b+OG5gmaUNJah5PohSnhySNl/SSZvta\n",
-       "wF5Av3cqRUR0imYKjLMpYxeeoIxdmCJ1z3ivtrUQJM0AdgMmAIuAY4DVAWyfKulQ4GPAUsrJ+6Tt\n",
-       "6yS9Evhh8zarAWfaPnaAz0gLISI6ksRrKWMXllCW7+yYL7YD/e7MwLSIiDZpJsg7BPg8cDowzebx\n",
-       "uqk6sMsoImK0a5bvPIVyN9JLKd1I7+rUKTDSQoiIGCESPZS7keZTlu+8u06OtBAiIqqy6aWMdL4K\n",
-       "uFHiXyVeVDfV81IQIiJGkM3TNsdS5kaaRFm+c/fKsYB0GUVEVCWxH/ANSqthis1T7f/MdBlFRHQc\n",
-       "m/MpYxcuH4lisCJpIUREjDFpIURExAqlIEREBJCCEBERjRSEiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICaGNBkDRd0iJJ/S4KIalH0qOSZjc//9pn32RJ8yTdKemodmWMiIjntbOFcBoweZBjfmZ7++bn\n",
-       "CwCSxgEnNa/dEjhQ0hZtzDnqNQtsRwtyrlqT89SabjtPbSsItmcCDw9yWH/TTkwC7rK9wPYS4Gxg\n",
-       "v+HON8b01A7QRXpqB+gSPbUDdIme2gGGouY1BAM7SZoj6WJJWzbbNwIW9jnunmZbRES00WoVP/sm\n",
-       "YBPbT0jaB/gR8OqKeSIixrS2znYqaSJwoe1tWjh2PmXBiFcD02xPbrZ/GnjW9pf7eU33TtUaEVFR\n",
-       "f7OdVmshSNoQ+L1tS5pEKU4PSZoFbNYUk3uB/YED+3uPTH0dETF82lYQJM0AdgMmSFoIHAOsDmD7\n",
-       "VOA9wMdO9LNwAAAD3ElEQVQkLQWeAA5o9i2VdBhwKTAO+I7t29uVMyIiiq5eICciIoZPx49UHmyQ\n",
-       "mqQj+wxumytpqaR1a2StrYVzNUHSJZJulnSrpIMrxKyuhfO0nqTzmjvgrpe0VY2ctQ02uLQ55hvN\n",
-       "eZwjafuRzNcpWhiE+xpJ10p6UtIRI51vSGx37A+ly+guYCKlu+lmYIsVHP9W4IrauTv1XAHTgGOb\n",
-       "xxOAB4HVamfvwPP0FeAzzePNx/C/qV2B7YG5A+zfF7i4efx64LramTv0PG0AvA74AnBE7bwr+un0\n",
-       "FsJQB6m9H5gxIsk6Tyvn6j5g7ebx2sCDtpeOYMZO0Mp52gK4EsD2HcBESRuMbMz6PPjg0rcDpzfH\n",
-       "Xg+s29wsMqYMdp5s3297FrBk5FKtnE4vCC0PUpM0HtgbOHcEcnWiVs7Vt4CtJN0LzAEOH6FsnaSV\n",
-       "8zQHeBdAcwfcK4CNRyRdd+nvXOY8dbFOLwhDueL9NuAq24+0K0yHa+VcHQ3cbPuvgO2AkyW9pL2x\n",
-       "Ok4r5+lLlG+7s4HDgNnAM21N1b2Wv/U7d6l0sZojlVvxW2CTPs83oXwL6c8BjN3uImjtXO0EfBHA\n",
-       "9q+bwYCbA7NGJGFnGPQ82X4MmLLseXOe7h6RdN1l+XO5cbMtulSntxCeG6QmaQ3KILULlj9I0jrA\n",
-       "m4DzRzhfJ2nlXM0D9oTnBgZuztj7RTfoeZK0TrMPSYdQZuV9fOSjdrwLgIMAJL0BeMT2orqROlrH\n",
-       "D6Tt6BaCBxikJmlqs//U5tB3AJfaXlwpanUtnqt/B06TNIfyZeBTth+qFrqCFs/TlsB/N1Oj3Ap8\n",
-       "pFrgigYbXGr7Ykn7SroL+CPwd/XS1jPYeZL0l8CNlBs5npV0OLBlJ37JyMC0iIgAOr/LKCIiRkgK\n",
-       "QkREACkIERHRSEGIiAggBSEiIhopCBERAaQgRKw0Sf3eRy7pZZIubR5vJunHku6SNEvS/0radWST\n",
-       "RrQmBSFi5Q00iGcycImkNYGLgFNsv8r264CPA68cqYARQ5GBaRErSdJjtl8wOaCksylrT+wM7GJ7\n",
-       "TI7gje6TFkLEMJI0Dtjc9jxgK+CmypEiWpaCEDG8Xg9c1zw2fSY0a5blnCtprK7ZER0uBSFieO0D\n",
-       "XNI8/iXw2mU7bL8TOBhYf+RjRQwuBSFieO0OXNE8PgvYWdLb+uxfa+QjRbSmo6e/juhw45vpjpc5\n",
-       "EXjS9h8BbD8p6a3A8ZJOABYBjwGfH/moEYPLXUYRw0TSB4CNbP9H7SwRKyMFISIigFxDiIiIRgpC\n",
-       "REQAKQgREdFIQYiICCAFISIiGikIEREBpCBERETj/wPQ8mh2PbtLiwAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaaff1d0>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    },
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t trial 1 \t\n",
-      "\t R is :  \t1.1\n",
-      "\t H2 is :  Btu \t73.0\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.7\n",
-      "\t average of difference is :  \t16.1\n",
-      "\t nd1 is :  \t0.310559006211\n",
-      "\t number of diffusing units :  \t1.48\n",
-      "\t L/G is :  \t1.19\n",
-      "\t trial 2 \t\n",
-      "\t R4 is :  \t1.2\n",
-      "\t H2 is :  Btu \t76.5\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.2\n",
-      "\t average of difference is :  \t15.85\n",
-      "\t nd1 is :  \t0.315457413249\n",
-      "\t number of diffusing units :  \t1.56\n",
-      "\t L/G is :  \t1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=85;\n",
-    "T2=120;\n",
-    "R=0.93; # R=(L/G), for 1500 gpm\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "print\"\\t for 120percent of design \\t\"\n",
-    "R1=1.2*R;\n",
-    "print\"\\t R is : %.3f \\t\",R1\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R1*(T2-T1)); \n",
-    "print\"\\t H2 is : %.1f Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=87.2F\n",
-    "Hs=53.1; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is : %.1f \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=42; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is : %.1f \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is : %.1f \\t\",d\n",
-    "dT=(90-87.2); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is : %.3f \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.53;\n",
-    "print\"\\t number of diffusing units : %.2f \\t\",nd\n",
-    "print\"\\t for 80 percent of design \\t\"\n",
-    "R2=0.8*R;\n",
-    "print\"\\t R is : %.3f \\t\",R2\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R2*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=82.5F\n",
-    "Hs=47.2; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=40.8; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-82.5); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.92;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "X=[1.115, 0.93, 0.74];\n",
-    "Y=[1.53, 1.70, 1.92];\n",
-    "pyplot.plot(X,Y)\n",
-    "pyplot.xlabel('L/G')\n",
-    "pyplot.ylabel('nd')\n",
-    "pyplot.title('KxaV/L vs L/G')\n",
-    "pyplot.show()\n",
-    "print\"\\t trial 1 \\t\"\n",
-    "R3=1.1;\n",
-    "print\"\\t R is :  \\t\",R3\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R3*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.48;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.19; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "print\"\\t trial 2 \\t\"\n",
-    "R4=1.2;\n",
-    "print\"\\t R4 is :  \\t\",R4\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R4*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40.5; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.56;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.08; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.6 pgno:615"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t X1 :  lb/lb \t0.0806276339156\n",
-      "\t total water in inlet gas :  lb/hr \t120.941450873\n",
-      "\t H1 :  Btu/lb dry air \t174.00276\n",
-      "\t outlet gas humidity :  lb/lb \t0.0645021071324\n",
-      "\t pw :  psia \t1.38381840969\n",
-      "\t H2 :  Btu/lb dry air \t126.234717909\n",
-      "\t total heat load :  Btu/hr \t71652.063136\n",
-      "\t water loading :  lb/hr \t2047.20180389\n",
-      "\t interval 1 \t\n",
-      "\t C :  Btu/(lb)*(F) \t0.286282435262\n",
-      "\t haV :  Btu/(hr)*(F) \t27.2526231819\n",
-      "\t qc :  Btu/hr \t4905.47217274\n",
-      "\t delT :  F \t11.4233860657\n",
-      "\t T(0.05) :  F \t288.576613934\n",
-      "\t delt :  F \t2.39618398314\n",
-      "\t t(0.05) :  F \t117.603816017\n",
-      "\t interval 2 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc1 :  Btu/hr \t9318.91447199\n",
-      "\t delT1 :  F \t21.7009808594\n",
-      "\t T(0.15) :  F \t266.875633075\n",
-      "\t water diffused during interval :  lb/hr \t1.20784906429\n",
-      "\t water remaining :  lb/hr \t119.733601809\n",
-      "\t qd :  Btu/hr \t1240.46098903\n",
-      "\t q1 :  Btu/hr \t10559.375461\n",
-      "\t delt1 :  F \t5.15795533248\n",
-      "\t t(0.15) :  F \t112.445860684\n",
-      "\t X(112.5F) :  lb/lb \t0.079822401206\n",
-      "\t interval 3 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc2 :  Btu/hr \t8417.23279004\n",
-      "\t delT2 :  F \t19.6012323339\n",
-      "\t T(0.25) :  F \t247.274400741\n",
-      "\t water diffused during interval :  lb/hr \t3.23916482908\n",
-      "\t water remaining :  lb/hr \t116.49443698\n",
-      "\t qd1 :  Btu/hr \t3336.33977395\n",
-      "\t q2 :  Btu/hr \t11753.572564\n",
-      "\t delt2 :  F \t5.7412867367\n",
-      "\t t(0.25) :  F \t106.704573948\n",
-      "\t X(106.5F) :  lb/lb \t0.0776629579866\n",
-      "\t calculated diffusion :  \t18.1244724962\n",
-      "\t Using some standard low-pressure-drop data \t\n",
-      "\t tower height :  ft \t2.16762543941\n",
-      "\t cross section :  ft^2 \t33.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# basis 1ft^2 ground area\n",
-    "#Assumption: 20 per cent of the initial vapor content of the gas enters the water body\n",
-    "X1=(1.69/(14.7-1.69))*(18./29.);\n",
-    "print\"\\t X1 :  lb/lb \\t\",X1\n",
-    "G=1500.;\n",
-    "w1=G*X1;\n",
-    "print\"\\t total water in inlet gas :  lb/hr \\t\",w1\n",
-    "# The inlet gas is at 300F and a 120F dew point. Use 0.25 Btu/(lb)(DegF) for the specific heat of nitrogen\n",
-    "H1=(0.0807*120)+(0.0807*1025.8)+(0.45*0.0807*(300-120))+(0.25*300); # eq 17.55\n",
-    "print\"\\t H1 :  Btu/lb dry air \\t\",H1\n",
-    "X2=(w1*(1-.2)/G);\n",
-    "print\"\\t outlet gas humidity :  lb/lb \\t\",X2\n",
-    "pw=(X2*29*14.7/18)/(1+(X2*29/18));\n",
-    "print\"\\t pw :  psia \\t\",pw\n",
-    "Tw=112.9; # F, from table 7 for above pw\n",
-    "# The outlet gas has a temperature of 200DegF and a 112.9DegF dew point\n",
-    "H2=(X2*Tw)+(X2*1029.8)+(X2*0.45*(200-Tw))+(0.25*200); # eq 17.55\n",
-    "print\"\\t H2 :  Btu/lb dry air \\t\",H2\n",
-    "q=G*(H1-H2);\n",
-    "print\"\\t total heat load :  Btu/hr \\t\",q\n",
-    "w2=q/(120-85);\n",
-    "print\"\\t water loading :  lb/hr \\t\",w2\n",
-    "print\"\\t interval 1 \\t\"\n",
-    "# (Kxa*delV/L)= 0 t0 0.05\n",
-    "nd=0.05; # nd=Kxa*V/L\n",
-    "Le=0.93; # fig 17.4 at 300F\n",
-    "C=(0.25)+(0.45*X1);\n",
-    "print\"\\t C :  Btu/(lb)*(F) \\t\",C\n",
-    "haV=(nd*w2*Le*C);\n",
-    "print\"\\t haV :  Btu/(hr)*(F) \\t\",haV\n",
-    "qc=(haV*(300-120));\n",
-    "print\"\\t qc :  Btu/hr \\t\",qc\n",
-    "delT=(qc/(C*G));\n",
-    "print\"\\t delT :  F \\t\",delT\n",
-    "T1=(300-delT);\n",
-    "print\"\\t T(0.05) :  F \\t\",T1\n",
-    "delt=(qc/w2);\n",
-    "print\"\\t delt :  F \\t\",delt\n",
-    "t1=(120-delt);\n",
-    "print\"\\t t(0.05) :  F \\t\",t1\n",
-    "print\"\\t interval 2 \\t\"\n",
-    "# (Kxa*delV/L)= 0.05 to 0.15\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc1=(haV1*(T1-t1));\n",
-    "print\"\\t qc1 :  Btu/hr \\t\",qc1\n",
-    "delT1=(qc1/(C*G));\n",
-    "print\"\\t delT1 :  F \\t\",delT1\n",
-    "T2=(T1-delT1);\n",
-    "print\"\\t T(0.15) :  F \\t\",T2\n",
-    "X3=0.0748; # at 117.6F\n",
-    "w3=(nd1*w2*(0.0807-X3));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w3\n",
-    "w4=(w1-w3);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w4\n",
-    "l1=1027; # Btu/lb, l1= lamda at 117.6F\n",
-    "qd=(w3*l1);\n",
-    "print\"\\t qd :  Btu/hr \\t\",qd\n",
-    "q1=(qd+qc1);\n",
-    "print\"\\t q1 :  Btu/hr \\t\",q1\n",
-    "delt1=(q1/w2);\n",
-    "print\"\\t delt1 :  F \\t\",delt1\n",
-    "t2=(t1-delt1);\n",
-    "print\"\\t t(0.15) :  F \\t\",t2\n",
-    "X4=0.0640; # at 112.5\n",
-    "X5=(w4/G);\n",
-    "print\"\\t X(112.5F) :  lb/lb \\t\",X5\n",
-    "print\"\\t interval 3 \\t\"\n",
-    "# (Kxa*delV/L)= 0.15 to 0.25\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc2=(haV1*(T2-t2));\n",
-    "print\"\\t qc2 :  Btu/hr \\t\",qc2\n",
-    "delT2=(qc2/(C*G));\n",
-    "print\"\\t delT2 :  F \\t\",delT2\n",
-    "T3=(T2-delT2);\n",
-    "print\"\\t T(0.25) :  F \\t\",T3\n",
-    "w5=(nd1*w2*(X5-X4));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w5\n",
-    "w6=(w4-w5);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w6\n",
-    "l2=1030; # Btu/lb, l1= lamda at 112.5F\n",
-    "qd1=(w5*l2);\n",
-    "print\"\\t qd1 :  Btu/hr \\t\",qd1\n",
-    "q2=(qd1+qc2);\n",
-    "print\"\\t q2 :  Btu/hr \\t\",q2\n",
-    "delt2=(q2/w2);\n",
-    "print\"\\t delt2 :  F \\t\",delt2\n",
-    "t3=(t2-delt2);\n",
-    "print\"\\t t(0.25) :  F \\t\",t3\n",
-    "X6=0.0533; # at 106.5\n",
-    "X7=(w6/G);\n",
-    "print\"\\t X(106.5F) :  lb/lb \\t\",X7\n",
-    "# The calculations of the remaining intervals until a. gas temperature of 200DegF is reached are shown in Fig. 17.17\n",
-    "w7=21.92; # total water diffused from table in solution\n",
-    "d=(w7/w1)*100;\n",
-    "print\"\\t calculated diffusion :  \\t\",d\n",
-    "print\"\\t Using some standard low-pressure-drop data \\t\"\n",
-    "# For G = 1500, extrapolate to L = 2040 on logarithmic coordinates. Kxa = 510.\n",
-    "ndt=.54; # from 1st table in solution\n",
-    "Kxa=510; # from 2nd table in solution\n",
-    "Z=(ndt*w2/Kxa);\n",
-    "print\"\\t tower height :  ft \\t\",Z\n",
-    "A=(50000/G);\n",
-    "print\"\\t cross section :  ft^2 \\t\",round(A,1)\n",
-    "# end\n",
-    "\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.7 pgno:620"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t sensible heat :  Btu/hr \t4200000.0\n",
-      "\t approximate diffusion :  Btu/hr \t756166.666667\n",
-      "\t total heat :  Btu/hr \t4956166.66667\n",
-      "\t total water quantity :  lb/hr \t141604.761905\n",
-      "\t tower cross section :  ft**2 \t69.4140989729\n",
-      "\t new gas rate :  lb/(hr)(ft**2) \t720.314759391\n",
-      "\t LMTD :  \t241.213395056\n",
-      "\t haV/L :  \t0.145099736239\n",
-      "\t number diffusion units :  \t0.557218649152\n",
-      "\t height of tower :  ft \t5.28709788033\n",
-      " ground dimensions :  ft \t1.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "C=0.28; # assumption\n",
-    "w=50000.; # lb/hr\n",
-    "G=1500.;\n",
-    "Qs=(w*C*(500-200));\n",
-    "Qd=(w/G)*(22685); # qd=22685, from previous prblm\n",
-    "from math import log\n",
-    "print\"\\t sensible heat :  Btu/hr \\t\",Qs\n",
-    "print\"\\t approximate diffusion :  Btu/hr \\t\",Qd\n",
-    "Q=(Qs+Qd);\n",
-    "print\"\\t total heat :  Btu/hr \\t\",Q\n",
-    "# an allowance as high as 30 per cent of the sensible load can be made and the excess water compensated for by throttling when the tower is in operation\n",
-    "w1=(Q/(120-85));\n",
-    "print\"\\t total water quantity :  lb/hr \\t\",w1\n",
-    "# If the maximum liquid loading is taken as 2040 lb/(hr)(ft'!), the required tower cross section\n",
-    "A=(w1/2040);\n",
-    "print\"\\t tower cross section :  ft**2 \\t\",A\n",
-    "w3=(w/A);\n",
-    "print\"\\t new gas rate :  lb/(hr)(ft**2) \\t\",w3\n",
-    "# The two terminal temperature differences are (200 - 85) and (500 - 120).\n",
-    "LMTD=((500-120)-(200-85))/(log((500-120)/(200-85)));\n",
-    "print\"\\t LMTD :  \\t\",LMTD\n",
-    "dt=35;\n",
-    "N=(dt/LMTD); # eq 17.88\n",
-    "print\"\\t haV/L :  \\t\",N\n",
-    "Le=0.93;\n",
-    "nd=(N/(C*Le));\n",
-    "print\"\\t number diffusion units :  \\t\",nd\n",
-    "# By extrapolation for G = 718 and L = 2040,Kxa=215\n",
-    "L=2040;\n",
-    "Kxa=215;\n",
-    "Z=(nd*L/Kxa); # calculation mistake\n",
-    "print\"\\t height of tower :  ft \\t\",Z\n",
-    "di=(A)**(1/2);\n",
-    "print\" ground dimensions :  ft \\t\",di\n",
-    "# ground dimensions are 5.8*8.3*8.3 ft\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_3.ipynb
deleted file mode 100755
index 45f8b0e5..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_17_Direct_Contact_Transfer__Cooling_Tower_3.ipynb
+++ /dev/null
@@ -1,856 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 17 Direct Contact Transfer : Cooling Tower"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 71.1 pgno:585"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 14,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.1 \n",
-      "\n",
-      "\t humidity is :  lb water/lb air  0.0186996126364\n",
-      "\t enthalpy at 75F is :  Btu/lb dry air  39.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.1 \\n\"\n",
-    "pw=0.4298; # psia, at 75F, table 7\n",
-    "pt=14.696; # psia\n",
-    "t=75.;\n",
-    "Mw=18.;\n",
-    "Ma=29.;\n",
-    "X=(pw/(pt-pw))*(Mw/Ma);\n",
-    "print\"\\t humidity is :  lb water/lb air \",X\n",
-    "H=(X*t)+(1051.5*X)+(0.24*t); # eq 17.54\n",
-    "print\"\\t enthalpy at 75F is :  Btu/lb dry air \",round(H,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.2 Pgno:602"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 15,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t by numerical integration \t\n",
-      "\t R is :  \t0.93005952381\n",
-      "\t H2 is :  Btu \t71.6520833333\n",
-      "\t difference is :  \t10.9\n",
-      "\t difference is :  \t13.0\n",
-      "\t average of difference is :  \t11.95\n",
-      "\t nd1 is :  \t0.418410041841\n",
-      "\t number of diffusing units :  \t1.7\n",
-      "\t log mean enthalpy difference \t\n",
-      "\t log mean of enthalpy :  Btu/lb \t25.6654878432\n",
-      "\t number of diffusing units are :  \t1.36\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t by numerical integration \\t\"\n",
-    "T1=85.;\n",
-    "T2=120.;\n",
-    "A=576.; # ground area, from fig 17.12\n",
-    "L=1500.*(500./576.);\n",
-    "G=1400.;\n",
-    "R=(L/G);\n",
-    "from math import log10\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "H1=39.1; # fig 17.12\n",
-    "H2=H1+(R*(T2-T1));\n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # fig 17.12\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=43.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=5; # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.70;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "print\"\\t log mean enthalpy difference \\t\"\n",
-    "dt=49.9; # diff. of enthalpies at top of the tower, from table in solution\n",
-    "db=10.9; # diff of enthalpies at bottom of the tower,from table in solution\n",
-    "LME=(dt-db)/(2.3*log10(dt/db));\n",
-    "print\"\\t log mean of enthalpy :  Btu/lb \\t\",LME\n",
-    "nd=(T2-T1)/(LME);\n",
-    "print\"\\t number of diffusing units are :  \\t\",round(nd,2)\n",
-    "# The error is naturally larger the greater the range\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.3 pgno:604"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 16,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Z is : ft \t19.2469565217\n",
-      "\t height of diffusion unit :  ft \t11.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# Since the loading is based on 1 ft2 of ground area\n",
-    "nd=1.7;\n",
-    "L=1302;\n",
-    "Kxa=115;\n",
-    "Z=(nd*L)/(Kxa);\n",
-    "print\"\\t Z is : ft \\t\",Z\n",
-    "HDU=(Z/nd);\n",
-    "print\"\\t height of diffusion unit :  ft \\t\",round(HDU,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.4 pgno:605"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 17,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t difference is :  \t13.0\n",
-      "\t difference is :  \t14.3\n",
-      "\t average of difference is :  \t13.65\n",
-      "\t nd1 is :  \t0.417582417582\n",
-      "\t number of diffusing units :  \t1.72\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=79.3F\n",
-    "Hs=43.4; # fig 17.12\n",
-    "H=30.4; # fig 17.12\n",
-    "d1=(Hs-H);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=35.7; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-79.3); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.72;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.5 pgno:609"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 18,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for 120percent of design \t\n",
-      "\t R is : %.3f \t1.116\n",
-      "\t H2 is : %.1f Btu \t78.16\n",
-      "\t difference is : %.1f \t14.0\n",
-      "\t difference is : %.1f \t14.7\n",
-      "\t average of difference is : %.1f \t14.35\n",
-      "\t nd1 is : %.3f \t0.19512195122\n",
-      "\t number of diffusing units : %.2f \t1.53\n",
-      "\t for 80 percent of design \t\n",
-      "\t R is : %.3f \t0.744\n",
-      "\t H2 is :  Btu \t65.14\n",
-      "\t difference is :  \t8.1\n",
-      "\t difference is :  \t9.2\n",
-      "\t average of difference is :  \t8.65\n",
-      "\t nd1 is :  \t0.28901734104\n",
-      "\t number of diffusing units :  \t1.92\n"
-     ]
-    },
-    {
-     "data": {
-      "image/png": [
-       "iVBORw0KGgoAAAANSUhEUgAAAYQAAAEZCAYAAACXRVJOAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\n",
-       "AAALEgAACxIB0t1+/AAAIABJREFUeJzt3XuYXVV9//H3pwHEULk1SC2gqYjIrYBIVC4yBYSAF7wD\n",
-       "XpDG8osWLFaoVJ4qsWrRKogCLXgJxQIBFREQ5GYZDXciIQQhCJLUIBi5CxIggc/vj7UDY5jJnEnm\n",
-       "zDpn5vN6nnlyzt77nPPJfpL5nrX2XmvJNhEREX9WO0BERHSGFISIiABSECIiopGCEBERQApCREQ0\n",
-       "UhAiIgJIQYiIiEYKQkREACkI0aUkLZC0R5/nB0h6SNKuq/CeB0ia38/21ST9XtK+fbZ9WtIXJfVI\n",
-       "Wriyn7kSGQ+WNHMF+9eQdL+k8c3zN0u6UtIfJD0gabakT0l60Uhlju6RghDdys0Pkj4MnATsa3vA\n",
-       "X5YtOA9YV9Juy22fDDwDXNJn277ARavwWe3yJmC27SckvRf4PnAG8HLbE4D9gY2BTSpmjA6VghDd\n",
-       "TJKmAl8F9rJ9XbNxf0l3S3pJ83wfSfdJ+ovm+dcl/UbSo5JmSdoFwPZTwPeAg5b7nIOAs2w/27x+\n",
-       "PeDVwLVDCLq/pBuX2/ZPks5vHu8r6ZfNN/l7JB0x9NMBlEJ1cfP4eOBztr9j+xEA27+y/Y+271rJ\n",
-       "949RLAUhutk/AJ8Ddrd907KNts8BrgG+0RSBbwMfsf1gc8gNwLbAesBZwPclrdHsOx14j6Q1ASSt\n",
-       "A7y12b7M3sAVHtpEYBcAm0t6VZ9t7wfObB5/B/h/ttcGtgL+dwjv3dc+wEWSXgNsBJy7ku8TY1AK\n",
-       "QnQrAXtSvqXf2s/+Q4HdgSuBC2wv+9aM7TNtP2z7WdvHAy8CNm/2XQMsAt7ZHP4+4A7bt/R577fw\n",
-       "/LfwltheDJwPHAggabPmMy9oDnka2ErS2rYftT17KO/fvOemwGq27wQmNJt/12f/2ZIelvRHSR8c\n",
-       "6vvH6JeCEN3KwEcpv1S//YKd9qPAD4CtgeP67pN0pKTbJD0i6WFgHZ7/BQrwXZ7vNvpQ83zZa/+M\n",
-       "Uoj6Xk9o1Vk0BYHSOjjP9pPN83dTunsWSOqV9IaVeP++3UXLWkMvW7bT9gG21wNuIv/3ox/5RxHd\n",
-       "bBGwB7CrpP/su0PSdsDfUX4Jn9hn+67APwPvtb1u8wvyUUqLY5kzgD0kvRF4Pc936wDsCPxfn+6n\n",
-       "obgC2EDStsABTTYAbM+y/Q5gA+BHlGsZQ9W3INwB/JZSaCJakoIQXc32fZSiMFnS8QBN//8ZwKeB\n",
-       "KcBGkj7WvOQlwFLggeYWzc8Cay/3nguAq4AZwGW2f99n977Aj5fPIelFktZc9jNA1iWUu36+Srl+\n",
-       "cXnz2tUlfUDSOrafAR6j3NU0EC3/ec1tpjtSushoLoAfARwj6e8lradiM2DDFbx3jGGrteuNJU2n\n",
-       "9LX+3vY2/exfD5gOvBJ4Ephi+5fNvgXAHyj/KZbYntSunNH9bC+UtDvwc0lPAmtSvsWfCtD0l18p\n",
-       "6TJKV88lwK+APwJfA37Tz9ueTvn3+c/Lbd8XmNr34ykXbxf33SZpM9t39/O+ZwE/B05edtdS44PA\n",
-       "iZLGAfOADwz01wV2Wv7zgLcD19p++rmN9vckPUopjF8Dnmr+rqdSutMi/oTatWJa0zR/HPjuAAXh\n",
-       "K8AfbH9e0uaU/yB7NvvmAzvYfqgt4SJWgqQNgZtsb1Q7y/IknQzMtX1K7SzRvdrWZdQMEHp4BYds\n",
-       "wfPN2zuAiZI26LNf/b4qop61gU/WDjGAmykD6yJWWs1rCHOAdwFImgS8gjKCEkoT+Ipm0NAhlfJF\n",
-       "/AnbdzZjHDqO7W/ZXlQ7R3S3tl1DaMGXgK9Lmg3MBWbz/IW0XWzf27QYLpc0bxWnJIiIiEFUKwi2\n",
-       "H6PcAQI8d93g7mbfvc2f90s6D5gEvKAgSGrPBZCIiFHO9gu65asVhGZKgMW2n266hX5m+/Hm9rlx\n",
-       "th+TtBawF2V6gn7195eKPyVpmu1ptXN0g5yr1uQ8taZTz9NAX6bbedvpDGA3YEIzPfAxwOoAze2A\n",
-       "WwL/3QS7FfhI89INgfMkLct3pu3L2pUzIiKKthUE2wcOsv9amvljlts+H9iuXbkiIqJ/Gak8NvTW\n",
-       "DtBFemsH6BK9tQN0id7aAYaibQPTRoIk5xpCRMTQDPS7My2EiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICSEGIiIhGCkJERAApCEMm/elyixERo0UKwhBIrAvcLg24vGFERNdKQRgCm0coa+pOkzhZ4kW1\n",
-       "M0VEDJcUhCGymQPsSFlY/ecSL68cKSJiWKQgrISmpfBO4FzgBom9KkeKiFhlmdxulTPQA5wFnAJ8\n",
-       "webZmnkiIgYz0O/OFIRhycHLgO8BjwMftHmwcqSIiAGN+GynkqZLWiRp7gD715N0nqQ5kq6XtFWf\n",
-       "fZMlzZN0p6Sj2pVxuNjcB+wO/BL4hcSOlSNFRAxZO68hnAZMXsH+o4GbbG8LHAR8HUDSOOCk5rVb\n",
-       "AgdK2qKNOYeFzRKbI4EjgIslpkpUb71ERLSqbQXB9kzg4RUcsgVwZXPsHcBESS8FJgF32V5gewlw\n",
-       "NrBfu3ION5tzgZ2Bw4DTJcZXjhQR0ZKadxnNAd4FIGkS8ApgY8rtnAv7HHdPs61r2PwKeAMg4HqJ\n",
-       "V1eOFBExqNUqfvaXgK9Lmg3MBWYDzwBDusotaVqfp722e4cr4Kqw+aPEQcBU4GqJqTY/rJ0rIsYe\n",
-       "ST1Az2DHVSsIth8Dpix7Lmk+8GvgxcAmfQ7dhNJKGOh9prUp4iqzMXCKxC+A70vsBHzaZknlaBEx\n",
-       "hjRflHuXPZd0TH/HVesykrSOpDWax4cAP7P9ODAL2EzSxGb//sAFtXIOB5sbgR2ArYCfNrepRkR0\n",
-       "lHbedjoDuAbYXNJCSVMkTZU0tTlkS2CupHnA3sDhALaXUi7IXgrcBpxj+/Z25RwpzdiEtwBXUG5N\n",
-       "3a1ypIiIP5GBaRVI7A2cDhwHfLXpWoqIGBEZqdxhmknxvg/cCxxs82jlSBExRoz4SOVYMZvfAG+i\n",
-       "FIRZEn9TOVJEjHEpCBXZPGVzKDCNcrH5w5UjRcQYli6jDiGxNWU67V7gcJsn6yaKiNEqXUYdzuZW\n",
-       "ysI76wNXSUysmygixpoUhA5i8wfgfcCZlCkv9q0cKSLGkHQZdSiJXSgT+00HPmfzTOVIETFK5LbT\n",
-       "LiTxl8AMYAnwAZv7K0eKiFEg1xC6kM3vgDcDN1FGN7+hcqSIGMVSEDqczVKbfwE+DlwgcVgW3omI\n",
-       "dkiXUReR2JRya+rtwCE2j1eOFBFdKF1Go4DNr4E3AouBGyReUzlSRIwiKQhdxmaxzRTKxHgzJd5X\n",
-       "O1NEjA7pMupiEq8FfkBZL+JTNk9XjhQRXSBdRqOQzU2UhXc2Ba6Uumvt6YjoLCkIXc7mYWA/4CLK\n",
-       "rKl7VI4UEV2qnSumTZe0SNLcAfZPkHSJpJsl3Srp4D77Fki6RdJsSTe0K+NoYfOszb8DHwTOkDha\n",
-       "SrGPiKFp2zUESbsCjwPftb1NP/unAS+y/WlJE4A7gA1tL5U0H9jB9kODfMaYvobQH4mNge8BDwIH\n",
-       "NS2IiIjnjPg1BNszYYW/jO4D1m4erw082KynvEx+0a8Em3uAHuBuShfS9nUTRUS3qNmt8C1gK0n3\n",
-       "AnOAw/vsM3CFpFmSDqmSrovZPG1zOHA0cJnER2pniojOt1rFzz4auNl2j6RNgcslbWv7MWBn2/dJ\n",
-       "2qDZPq9pcbxA0/W0TK/t3rYn7xI250jcApwrsRNwmM3i2rkiYmRJ6qH0HKz4uHaOQ5A0EbhwgGsI\n",
-       "FwNftH118/ynwFG2Zy133DHA47aP6+c9cg2hBRJ/TmmRvQZ4TzPiOSLGqE4chzAP2BNA0obA5sDd\n",
-       "ksZLekmzfS1gL6DfO5WiNc2cR++nrK1wrcTbK0eKiA7UzruMZgC7AROARcAxwOoAtk9t7iw6DXg5\n",
-       "pTAda/ssSa8Efti8zWrAmbaPHeAz0kIYIok3AudQVmX7jM3SQV4SEaNMFsiJ50hsAJwFjAMOtFlU\n",
-       "OVJEjKBO7DKKSpqV1yYDV1MW3tm5cqSI6ABpIYxxEm+hXFv4EnCCTff+g4iIlqTLKAYk8deUWVPv\n",
-       "Bj5i84fKkSKijdJlFAOymQ/sDDxEWXhnq8qRIqKCFIQAwOZJm6mUrqNeiQ/UzhQRIytdRvECEttS\n",
-       "upAuBY6weapypIgYRukyipbZzAF2BDYGfi7x8sqRImIEpCBEv2weAd4JnEu5rrBX5UgR0WbpMopB\n",
-       "SfRQBrKdAnzB5tm6iSJiVeS201glEi+jLLzzGPAhmwcrR4qIlZRrCLFKbO4Ddgduo4xu3rFypIgY\n",
-       "ZikI0TKbJTZHAkcAF0tMlbKyXcRokS6jWCkSr6ZccJ4NfNTmicqRIqJF6TKKYWXzK+ANlLWvr28K\n",
-       "RER0sRSEWGk2fwQOAk4GrpZ4V+VIEbEK0mUUw6K5yPx9ygjnT9ssqRwpIgYw4l1GkqZLWiSp3+Uv\n",
-       "JU2QdImkmyXdKungPvsmS5on6U5JR7UrYwwfmxuBHYCtgJ82t6lGRBdpZ5fRaZRFWAZyGDDb9nZA\n",
-       "D3CcpNUkjQNOal67JXCgpC3amDOGSTM24S3AFcAsid0qR4qIIWhbQbA9E3h4BYfcB6zdPF4beND2\n",
-       "UmAScJftBbaXAGcD+7UrZwwvm2dt/g2YApwj8c+5NTWiO9S8qPwtYCtJ9wJzgMOb7RsBC/scd0+z\n",
-       "LbqIzaWU4v4e4IcS61SOFBGDWK3iZx8N3Gy7R9KmwOWSth3qm0ia1udpr+3eYcoXq8jmNxJvAo6n\n",
-       "dCG92+aW2rkixhpJPZSu+RWqWRB2Ar4IYPvXkuYDm1NaBJv0OW6TZlu/bE9rY8ZYRc1aCoc2C+78\n",
-       "VOJIm9Nr54oYS5ovyr3Lnks6pr/janYZzQP2BJC0IaUY3A3MAjaTNFHSGsD+wAXVUsawsDkT+Fvg\n",
-       "aIlTJdasnSki/lTbxiFImgHsBkwAFgHHAKsD2D5V0gTKnUgvpxSmY22f1bx2H+AEYBzwHdvHDvAZ\n",
-       "GYfQZSTWBr4D/DXwHpsFdRNFjD2Z/jo6RnPX0SeAfwH+zubiypEixpQUhOg4ErtQbiueDnzO5pnK\n",
-       "kSLGhBSE6EgSG1KKwhLgAzb3V44UMeplttPoSDaLgDcDN1EW3nlD5UgRY1YKQlRns9TmXyjTmVwg\n",
-       "cVhGN0eMvHQZRUeR2JSy8M7twCE2j1eOFDHqpMsouoLNr4E3AouBGyReUzlSxJiRghAdx2axzRTg\n",
-       "OGCmxPtqZ4oYC9JlFB1N4rWURXcuAD5l83TlSBFdL11G0ZVsbqIsvLMpcKWUmW8j2iUFITqezcOU\n",
-       "NTEuosyaukflSBGjUrqMoqs0xeAM4BvAl22erRwpoutkpHKMGhIbA98DHgQOaloQEdGiXEOIUcPm\n",
-       "HspiH7+mdCFtXzdRxOiQghBdyeZpm09QVt67TOIjtTNFdLt0GUXXk9iCMrr5WuAwm8WVI0V0tBHv\n",
-       "MpI0XdIiSXMH2H+kpNnNz1xJSyWt2+xbIOmWZt8N7coYo4PN7cAkYDxwTTP9RUQMUTtXTNsVeBz4\n",
-       "ru1tBjn2rcAnbC9bUnM+sIPthwZ5XVoI8ZxmQrzDgM8Af29n6dWI/ox4C8H2TGj57o/3AzOW25Zf\n",
-       "9DEkNrY5EXg7cJLEsRKr1c4V0S2qX1SWNB7Ym9IHvIyBKyTNknRInWTRrWyuo4xufh3lgvOGlSNF\n",
-       "dIXqBQF4G3CV7Uf6bNvZ9vbAPsChTfdTRMualdcmA1dTbk3duXKkiI7XCc3pA1iuu8j2fc2f90s6\n",
-       "j3LBcGZ/L5Y0rc/TXtu97YkZ3aZZo/kzEtcBP5T4EnCCTffeWhexEiT1UMburPi4dt52KmkicOFA\n",
-       "F5UlrQPcDWxse3GzbTwwzvZjktYCLgM+Z/uyfl6fi8rREom/psyaejcwxeaxypEiqqlx2+kM4Bpg\n",
-       "c0kLJU2RNFXS1D6HvQO4dFkxaGwIzJR0M3A98OP+ikHEUNjMB3YGHgJulNiqcqSIjpOBaTHmSBwM\n",
-       "fAX4hM2ZleNEjLhMbhfRh8S2lC6kS4EjbJ6qHClixGRyu4g+bOYAOwIbAT+XeHnlSBHVpSDEmGXz\n",
-       "CPAuSkvhBom9KkeKqCpdRhGARA9wFnAK8IUsvBOj2ZCvIQw0KV3Dtv9muMKtrBSEGE4SLwPOoczB\n",
-       "9SGbBytHimiLgX53rmhg2tuaP/+h+fN/KPMLfWCYs0V0BJv7miU6/x34hcR7bW6snStipAzaZSTp\n",
-       "ZtvbLbdtdjO1RFVpIUS7SLwb+C/KzKnfzOjmGE1W5S4jSdqlz5OdyUykMcrZnAvsQplO+3SJ8ZUj\n",
-       "RbRdKy2EHYDpwLrNpoeBKbZvanO2QaWFEO0msRblQvO2wLtt7qwcKWKVrfTANElrAu8GJgITgEco\n",
-       "F5X/rQ05hyQFIUZCs/DOVODfgI/a/LBypIhVsjIXlZc5n1IEfgHcM9zBIjpdc/3gFIlfAN+X2An4\n",
-       "tM2SytEihlUrLYRbbW89QnmGJC2EGGkSfwGcAawF7G9zX+VIEUO2KheVr5FUfcxBRCdoxia8BbiC\n",
-       "svDObpUjRQybVloItwOvAubDcxOAZWBajHkSewOnA8cBX82tqdEtVuWi8sT+ttteMBzBVkUKQtTW\n",
-       "TIr3feBe4GCbRytHihhUpr+OaBOJFwHHA3tRbk29pXKkiBWqsWLadEmLBpoTSdKRkmY3P3MlLZW0\n",
-       "brNvsqR5ku6UdFS7MkYMB5unbA4FpgE/lTiocqSIldK2FoKkXSmThH13oDWV+xz7VuATtveUNA64\n",
-       "A9gT+C1wI3Cg7dv7eV1aCNFRJLYGzgV6gcNtnqybKOKFRryFYHsmZVRzK94PzGgeTwLusr3A9hLg\n",
-       "bGC/NkSMGHY2t1IW3lkfuEpiYt1EEa2rvkCOpPHA3pRvVVBWsFrY55B7mm0RXcHmD8D7KOMVrpfY\n",
-       "t3KkiJZULwiUabavsv1I87x7r3JHNGxscwJl2pdvSpwosU7tXBEr0srUFe12AM93F0G5brBJn+eb\n",
-       "sIIpMyRN6/O013bvcIaLWBU2V0lsC3wJuE3iSODsjFmIkSSpB+gZ9Lh23nbajGG4cKCLypLWAe4G\n",
-       "Nra9uNm2GuWi8h6Ue7tvIBeVYxRo5kD6L+B+4FCbOypHijGqxm2nM4BrgM0lLZQ0RdJUSVP7HPYO\n",
-       "4NJlxQDA9lLKHPSXArcB5/RXDCK6jc01wA7ARcDVEp+XeHHlWBHPycC0iAokNga+BrwWOMzmJ5Uj\n",
-       "xRiSkcoRHUhiMnAyMBv4hJ0p5qP9RrzLKCIGZ3MJsDWle/RmiU9KHXGzR4xBaSFEdAiJVwP/CWwA\n",
-       "fKy55hAx7NJlFNEFmuU696dMqf0T4KhmDYaIYZMuo4gu0AxoOxvYEniCMnZhipT/q9F+aSFEdDCJ\n",
-       "11LGLiyhdCP1O3twxFCkhRDRhWxuAnaizIv0U4mvSvx55VgxSqUgRHQ4m2dsTgG2AV5K6UZ6V3O9\n",
-       "IWLYpMsoostI9FDuRpoPfNzm7rqJotukyyhilLDpBbYDrgJulPjXZhnPiFWSghDRhWyetjmWMjfS\n",
-       "JGCOxO6VY0WXS5dRxCggsR/wDUqr4Qib31WOFB0sXUYRo5jN+ZSxCwuBuRKHSoyrHCu6TFoIEaOM\n",
-       "xFaUi85rAR+1mVU5UnSYtBAixgibX1JWxzoR+LHEyRLr1k0V3SAFIWIUaqbAOJ3SjTQOuF3igxm7\n",
-       "ECvSti4jSdOBtwC/X8ESmj2URUJWBx6w3dNsXwD8AXgGWGJ70gCvT5dRRAsk3kCZAuNh4B9s5lWO\n",
-       "FBWN+GynknYFHge+219BkLQucDWwt+17JE2w/UCzbz6wg+2HBvmMFISIFjXrLBwKfAY4FfiizRN1\n",
-       "U0UNI34NwfZMyreRgbwfONf2Pc3xDyy3P7/oI4aRzVKbrwPbAq8CbpV4S+VY0UFqXkPYDFhf0pWS\n",
-       "Zkn6UJ99Bq5oth9SKV/EqGTzW5v9gY8CJ0j8UGKT2rmivppL9a1OWWB8D2A8cK2k62zfCexi+15J\n",
-       "GwCXS5rXtDheQNK0Pk97bfe2OXfEqGBzmcQ2wFHAbIkvAyfYLKkcLYZZc722Z9Dj2jkOQdJE4MIB\n",
-       "riEcBbzY9rTm+beBS2z/YLnjjgEet31cP++RawgRw0BiM+Ak4K8o6y5cVTlStFEnjkM4H9hF0jhJ\n",
-       "44HXA7dJGi/pJQCS1gL2giwKEtFONncCk4HPA2dLTJfYoHKsGGFtKwiSZgDXAJtLWihpiqSpkqYC\n",
-       "2J4HXALcAlwPfMv2bcBfAjMl3dxs/7Hty9qVMyKKZuzC9yhjFx4FfilxSJbvHDsydUVE9EtiO8rY\n",
-       "BVO6keZUjhTDpBO7jCKig9ncDOwM/DdwucTxEi+pmyraKQUhIgZk86zNN4GtgfUpU2C8J1NgjE7p\n",
-       "MoqIlkm8idKN9BvgMJtfV44UKyFdRhGxymx+Tlm+80rgeonPZvnO0SMFISKGxGaJzX9Qlu98LWVB\n",
-       "nj0rx4phkC6jiFglEm+jLN95HWX5znsrR4pBpMsoItrC5kJgK2A+cIvEPzYzq0aXSQshIoaNxBaU\n",
-       "5TvXoSzfeUPlSNGPtBAiou1sbgd2pyx8db7EKRLrVY4VLUpBiIhh1UyB8T+UKTBMGbtwUMYudL50\n",
-       "GUVEW0lMooxdeIyyfOdtlSONeekyiogqmusIk4BzgZ9JHCsxvnKs6EcKQkS0nc0zNicCfwO8Arit\n",
-       "uV01Oki6jCJixDUD2U4G5gH/aPN/lSONKekyioiOYXMFpbUwC/iFxFESa1SONealhRARVUlsSlm+\n",
-       "8+WUi84/qxxp1BvxFoKk6ZIWSRpw+UtJPZJmS7pVUm+f7ZMlzZN0Z7P2ckSMUs2MqfsCnwXOkDhd\n",
-       "4qWVY41J7ewyOo2yRmu/JK1L6UN8m+2tgfc028dRvi1MptzHfKCkLdqYMyIqa8YunEv5P/8AcKvE\n",
-       "1CzfObLadrJtzwQeXsEh7wfOtX1Pc/wDzfZJwF22F9heApwN7NeunBHROWweszkCeDPwYeAaie0r\n",
-       "xxozalbfzYD1JV0paZakDzXbNwIW9jnunmZbRIwRzfrNuwDfBi6ROEFi7cqxRr2aMxKuTplLfQ9g\n",
-       "PHCtpOsoQ91bJmlan6e9tnuHK2BE1GPzLPBtiR8BX6aMXTgC+J49tN8TY52kHqBnsONqFoSFwAO2\n",
-       "FwOLJf0c2JbSItikz3GbNNv6ZXtaO0NGRF02DwAfkdiFMgXGFInDbO6sHK1rNF+Ue5c9l3RMf8fV\n",
-       "7DI6H9hF0jhJ44HXA7dR7kveTNJESWsA+wMXVMwZER3A5ipKr8LlwLUS0yTWrBxrVGnnbaczgGuA\n",
-       "zSUtlDRF0lRJUwFszwMuAW4Brge+Zfs220uBw4BLKQXiHNu3tytnRHSPZvnOrwLbA9tQ7kbau3Ks\n",
-       "USMD0yKia0nsS7lNfRbwTza/rRypK2TqiogYdWwuBrYGfgXMkfhElu9ceWkhRMSoIPEayvKd6wMf\n",
-       "s7m2cqSOlRZCRIxqNvMot7F/BThX4psS61eO1VVSECJi1GimwDiTMgXG05SxCwdn+c7WpMsoIkYt\n",
-       "idcBpwBPULqRflk5UkdIl1FEjDk2syhjnM4GeiW+LLFW5VgdKwUhIka1ZvnO/6SMW9iI0o30jnQj\n",
-       "vVC6jCJiTJHYnXI30p3Ax20W1E008tJlFBEB2PwvZd606yjLdx6d5TuLFISIGHNsnrL5IrAjsDNl\n",
-       "UNvfVo5VXbqMImJMa64lvAP4OvAz4EibRXVTtVe6jCIi+tGMXTiPMnbhd5QJ8z4mMa5ytBGXFkJE\n",
-       "RB8S21DWXVgD+KjNTZUjDbu0ECIiWmAzF3gTpSj8ROJEiXUqxxoRKQgREcuxedbmNEo30pqUsQsH\n",
-       "jvaxC+kyiogYhMROlBbD/cChNndUjrRKRrzLSNJ0SYskzR1gf4+kRyXNbn4+02ffAkm3NNtvaFfG\n",
-       "iIhW2FwD7ABcBFwt8XmJF1eONeza2WV0GjB5kGN+Znv75ufzfbYb6Gm2T2pfxIiI1tgstfkasB3w\n",
-       "GsrdSPtUjjWs2lYQbM8EHh7ksBV196QrKCI6js09Nu+lrP1+ksQPJDaunWs41LyobGAnSXMkXSxp\n",
-       "y+X2XSFplqRDKuWLiBiQzU8oy3feBtws8cluX76zZvibgE1sPyFpH+BHwKubfTvbvk/SBsDlkuY1\n",
-       "LY4XkDStz9Ne273tDB0RsYzNYuCzEmdQJsz7sMTHmmsOHUNSD9Az6HHtvMtI0kTgQtvbtHDsfGAH\n",
-       "2w8tt/0Y4HHbx/XzmtxlFBEdobkldX/gOOAnwFE2D9ZN1b+OG5gmaUNJah5PohSnhySNl/SSZvta\n",
-       "wF5Av3cqRUR0imYKjLMpYxeeoIxdmCJ1z3ivtrUQJM0AdgMmAIuAY4DVAWyfKulQ4GPAUsrJ+6Tt\n",
-       "6yS9Evhh8zarAWfaPnaAz0gLISI6ksRrKWMXllCW7+yYL7YD/e7MwLSIiDZpJsg7BPg8cDowzebx\n",
-       "uqk6sMsoImK0a5bvPIVyN9JLKd1I7+rUKTDSQoiIGCESPZS7keZTlu+8u06OtBAiIqqy6aWMdL4K\n",
-       "uFHiXyVeVDfV81IQIiJGkM3TNsdS5kaaRFm+c/fKsYB0GUVEVCWxH/ANSqthis1T7f/MdBlFRHQc\n",
-       "m/MpYxcuH4lisCJpIUREjDFpIURExAqlIEREBJCCEBERjRSEiIgAUhAiIqKRghAREUAKQkRENFIQ\n",
-       "IiICaGNBkDRd0iJJ/S4KIalH0qOSZjc//9pn32RJ8yTdKemodmWMiIjntbOFcBoweZBjfmZ7++bn\n",
-       "CwCSxgEnNa/dEjhQ0hZtzDnqNQtsRwtyrlqT89SabjtPbSsItmcCDw9yWH/TTkwC7rK9wPYS4Gxg\n",
-       "v+HON8b01A7QRXpqB+gSPbUDdIme2gGGouY1BAM7SZoj6WJJWzbbNwIW9jnunmZbRES00WoVP/sm\n",
-       "YBPbT0jaB/gR8OqKeSIixrS2znYqaSJwoe1tWjh2PmXBiFcD02xPbrZ/GnjW9pf7eU33TtUaEVFR\n",
-       "f7OdVmshSNoQ+L1tS5pEKU4PSZoFbNYUk3uB/YED+3uPTH0dETF82lYQJM0AdgMmSFoIHAOsDmD7\n",
-       "VOA9wMdO9LNwAAAD3ElEQVQkLQWeAA5o9i2VdBhwKTAO+I7t29uVMyIiiq5eICciIoZPx49UHmyQ\n",
-       "mqQj+wxumytpqaR1a2StrYVzNUHSJZJulnSrpIMrxKyuhfO0nqTzmjvgrpe0VY2ctQ02uLQ55hvN\n",
-       "eZwjafuRzNcpWhiE+xpJ10p6UtIRI51vSGx37A+ly+guYCKlu+lmYIsVHP9W4IrauTv1XAHTgGOb\n",
-       "xxOAB4HVamfvwPP0FeAzzePNx/C/qV2B7YG5A+zfF7i4efx64LramTv0PG0AvA74AnBE7bwr+un0\n",
-       "FsJQB6m9H5gxIsk6Tyvn6j5g7ebx2sCDtpeOYMZO0Mp52gK4EsD2HcBESRuMbMz6PPjg0rcDpzfH\n",
-       "Xg+s29wsMqYMdp5s3297FrBk5FKtnE4vCC0PUpM0HtgbOHcEcnWiVs7Vt4CtJN0LzAEOH6FsnaSV\n",
-       "8zQHeBdAcwfcK4CNRyRdd+nvXOY8dbFOLwhDueL9NuAq24+0K0yHa+VcHQ3cbPuvgO2AkyW9pL2x\n",
-       "Ok4r5+lLlG+7s4HDgNnAM21N1b2Wv/U7d6l0sZojlVvxW2CTPs83oXwL6c8BjN3uImjtXO0EfBHA\n",
-       "9q+bwYCbA7NGJGFnGPQ82X4MmLLseXOe7h6RdN1l+XO5cbMtulSntxCeG6QmaQ3KILULlj9I0jrA\n",
-       "m4DzRzhfJ2nlXM0D9oTnBgZuztj7RTfoeZK0TrMPSYdQZuV9fOSjdrwLgIMAJL0BeMT2orqROlrH\n",
-       "D6Tt6BaCBxikJmlqs//U5tB3AJfaXlwpanUtnqt/B06TNIfyZeBTth+qFrqCFs/TlsB/N1Oj3Ap8\n",
-       "pFrgigYbXGr7Ykn7SroL+CPwd/XS1jPYeZL0l8CNlBs5npV0OLBlJ37JyMC0iIgAOr/LKCIiRkgK\n",
-       "QkREACkIERHRSEGIiAggBSEiIhopCBERAaQgRKw0Sf3eRy7pZZIubR5vJunHku6SNEvS/0radWST\n",
-       "RrQmBSFi5Q00iGcycImkNYGLgFNsv8r264CPA68cqYARQ5GBaRErSdJjtl8wOaCksylrT+wM7GJ7\n",
-       "TI7gje6TFkLEMJI0Dtjc9jxgK+CmypEiWpaCEDG8Xg9c1zw2fSY0a5blnCtprK7ZER0uBSFieO0D\n",
-       "XNI8/iXw2mU7bL8TOBhYf+RjRQwuBSFieO0OXNE8PgvYWdLb+uxfa+QjRbSmo6e/juhw45vpjpc5\n",
-       "EXjS9h8BbD8p6a3A8ZJOABYBjwGfH/moEYPLXUYRw0TSB4CNbP9H7SwRKyMFISIigFxDiIiIRgpC\n",
-       "REQAKQgREdFIQYiICCAFISIiGikIEREBpCBERETj/wPQ8mh2PbtLiwAAAABJRU5ErkJggg==\n"
-      ],
-      "text/plain": [
-       "<matplotlib.figure.Figure at 0xaaff1d0>"
-      ]
-     },
-     "metadata": {},
-     "output_type": "display_data"
-    },
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t trial 1 \t\n",
-      "\t R is :  \t1.1\n",
-      "\t H2 is :  Btu \t73.0\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.7\n",
-      "\t average of difference is :  \t16.1\n",
-      "\t nd1 is :  \t0.310559006211\n",
-      "\t number of diffusing units :  \t1.48\n",
-      "\t L/G is :  \t1.19\n",
-      "\t trial 2 \t\n",
-      "\t R4 is :  \t1.2\n",
-      "\t H2 is :  Btu \t76.5\n",
-      "\t difference is :  \t15.5\n",
-      "\t difference is :  \t16.2\n",
-      "\t average of difference is :  \t15.85\n",
-      "\t nd1 is :  \t0.315457413249\n",
-      "\t number of diffusing units :  \t1.56\n",
-      "\t L/G is :  \t1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=85;\n",
-    "T2=120;\n",
-    "R=0.93; # R=(L/G), for 1500 gpm\n",
-    "import numpy\n",
-    "import matplotlib\n",
-    "%matplotlib inline\n",
-    "from matplotlib import pyplot\n",
-    "print\"\\t for 120percent of design \\t\"\n",
-    "R1=1.2*R;\n",
-    "print\"\\t R is : %.3f \\t\",R1\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R1*(T2-T1)); \n",
-    "print\"\\t H2 is : %.1f Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=87.2F\n",
-    "Hs=53.1; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is : %.1f \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=42; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is : %.1f \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is : %.1f \\t\",d\n",
-    "dT=(90-87.2); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is : %.3f \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.53;\n",
-    "print\"\\t number of diffusing units : %.2f \\t\",nd\n",
-    "print\"\\t for 80 percent of design \\t\"\n",
-    "R2=0.8*R;\n",
-    "print\"\\t R is : %.3f \\t\",R2\n",
-    "H1=39.1; # at 87.2F\n",
-    "H2=H1+(R2*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=82.5F\n",
-    "Hs=47.2; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=85\n",
-    "Hs=50; # fig 17.12\n",
-    "H=40.8; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(85-82.5); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.92;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "X=[1.115, 0.93, 0.74];\n",
-    "Y=[1.53, 1.70, 1.92];\n",
-    "pyplot.plot(X,Y)\n",
-    "pyplot.xlabel('L/G')\n",
-    "pyplot.ylabel('nd')\n",
-    "pyplot.title('KxaV/L vs L/G')\n",
-    "pyplot.show()\n",
-    "print\"\\t trial 1 \\t\"\n",
-    "R3=1.1;\n",
-    "print\"\\t R is :  \\t\",R3\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R3*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.48;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.19; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "print\"\\t trial 2 \\t\"\n",
-    "R4=1.2;\n",
-    "print\"\\t R4 is :  \\t\",R4\n",
-    "H1=34.5; # at 87.2F\n",
-    "H2=H1+(R4*(T2-T1)); \n",
-    "print\"\\t H2 is :  Btu \\t\",H2\n",
-    "# The area between the saturation line and the operating line represents the potential for heat transfer\n",
-    "# at T=85F\n",
-    "Hs=50; # from table in the solution\n",
-    "d1=(Hs-H1);\n",
-    "print\"\\t difference is :  \\t\",d1\n",
-    "#at t=90\n",
-    "Hs=56.7; # fig 17.12\n",
-    "H=40.5; # fig 17.12\n",
-    "d2=Hs-H;\n",
-    "print\"\\t difference is :  \\t\",d2\n",
-    "d=(d1+d2)/(2);\n",
-    "print\"\\t average of difference is :  \\t\",d\n",
-    "dT=(90-85); # F\n",
-    "nd1=(dT/d);\n",
-    "print\"\\t nd1 is :  \\t\",nd1\n",
-    "# similarly calculating nd at each temperature and adding them will give you total nd value\n",
-    "nd=1.56;\n",
-    "print\"\\t number of diffusing units :  \\t\",nd\n",
-    "R3=1.08; # from fig 17.14\n",
-    "print\"\\t L/G is :  \\t\",R3\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.6 pgno:615"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t X1 :  lb/lb \t0.0806276339156\n",
-      "\t total water in inlet gas :  lb/hr \t120.941450873\n",
-      "\t H1 :  Btu/lb dry air \t174.00276\n",
-      "\t outlet gas humidity :  lb/lb \t0.0645021071324\n",
-      "\t pw :  psia \t1.38381840969\n",
-      "\t H2 :  Btu/lb dry air \t126.234717909\n",
-      "\t total heat load :  Btu/hr \t71652.063136\n",
-      "\t water loading :  lb/hr \t2047.20180389\n",
-      "\t interval 1 \t\n",
-      "\t C :  Btu/(lb)*(F) \t0.286282435262\n",
-      "\t haV :  Btu/(hr)*(F) \t27.2526231819\n",
-      "\t qc :  Btu/hr \t4905.47217274\n",
-      "\t delT :  F \t11.4233860657\n",
-      "\t T(0.05) :  F \t288.576613934\n",
-      "\t delt :  F \t2.39618398314\n",
-      "\t t(0.05) :  F \t117.603816017\n",
-      "\t interval 2 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc1 :  Btu/hr \t9318.91447199\n",
-      "\t delT1 :  F \t21.7009808594\n",
-      "\t T(0.15) :  F \t266.875633075\n",
-      "\t water diffused during interval :  lb/hr \t1.20784906429\n",
-      "\t water remaining :  lb/hr \t119.733601809\n",
-      "\t qd :  Btu/hr \t1240.46098903\n",
-      "\t q1 :  Btu/hr \t10559.375461\n",
-      "\t delt1 :  F \t5.15795533248\n",
-      "\t t(0.15) :  F \t112.445860684\n",
-      "\t X(112.5F) :  lb/lb \t0.079822401206\n",
-      "\t interval 3 \t\n",
-      "\t haV1 :  Btu/(hr)*(F) \t54.5052463637\n",
-      "\t qc2 :  Btu/hr \t8417.23279004\n",
-      "\t delT2 :  F \t19.6012323339\n",
-      "\t T(0.25) :  F \t247.274400741\n",
-      "\t water diffused during interval :  lb/hr \t3.23916482908\n",
-      "\t water remaining :  lb/hr \t116.49443698\n",
-      "\t qd1 :  Btu/hr \t3336.33977395\n",
-      "\t q2 :  Btu/hr \t11753.572564\n",
-      "\t delt2 :  F \t5.7412867367\n",
-      "\t t(0.25) :  F \t106.704573948\n",
-      "\t X(106.5F) :  lb/lb \t0.0776629579866\n",
-      "\t calculated diffusion :  \t18.1244724962\n",
-      "\t Using some standard low-pressure-drop data \t\n",
-      "\t tower height :  ft \t2.16762543941\n",
-      "\t cross section :  ft^2 \t33.3\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "# basis 1ft^2 ground area\n",
-    "#Assumption: 20 per cent of the initial vapor content of the gas enters the water body\n",
-    "X1=(1.69/(14.7-1.69))*(18./29.);\n",
-    "print\"\\t X1 :  lb/lb \\t\",X1\n",
-    "G=1500.;\n",
-    "w1=G*X1;\n",
-    "print\"\\t total water in inlet gas :  lb/hr \\t\",w1\n",
-    "# The inlet gas is at 300F and a 120F dew point. Use 0.25 Btu/(lb)(DegF) for the specific heat of nitrogen\n",
-    "H1=(0.0807*120)+(0.0807*1025.8)+(0.45*0.0807*(300-120))+(0.25*300); # eq 17.55\n",
-    "print\"\\t H1 :  Btu/lb dry air \\t\",H1\n",
-    "X2=(w1*(1-.2)/G);\n",
-    "print\"\\t outlet gas humidity :  lb/lb \\t\",X2\n",
-    "pw=(X2*29*14.7/18)/(1+(X2*29/18));\n",
-    "print\"\\t pw :  psia \\t\",pw\n",
-    "Tw=112.9; # F, from table 7 for above pw\n",
-    "# The outlet gas has a temperature of 200DegF and a 112.9DegF dew point\n",
-    "H2=(X2*Tw)+(X2*1029.8)+(X2*0.45*(200-Tw))+(0.25*200); # eq 17.55\n",
-    "print\"\\t H2 :  Btu/lb dry air \\t\",H2\n",
-    "q=G*(H1-H2);\n",
-    "print\"\\t total heat load :  Btu/hr \\t\",q\n",
-    "w2=q/(120-85);\n",
-    "print\"\\t water loading :  lb/hr \\t\",w2\n",
-    "print\"\\t interval 1 \\t\"\n",
-    "# (Kxa*delV/L)= 0 t0 0.05\n",
-    "nd=0.05; # nd=Kxa*V/L\n",
-    "Le=0.93; # fig 17.4 at 300F\n",
-    "C=(0.25)+(0.45*X1);\n",
-    "print\"\\t C :  Btu/(lb)*(F) \\t\",C\n",
-    "haV=(nd*w2*Le*C);\n",
-    "print\"\\t haV :  Btu/(hr)*(F) \\t\",haV\n",
-    "qc=(haV*(300-120));\n",
-    "print\"\\t qc :  Btu/hr \\t\",qc\n",
-    "delT=(qc/(C*G));\n",
-    "print\"\\t delT :  F \\t\",delT\n",
-    "T1=(300-delT);\n",
-    "print\"\\t T(0.05) :  F \\t\",T1\n",
-    "delt=(qc/w2);\n",
-    "print\"\\t delt :  F \\t\",delt\n",
-    "t1=(120-delt);\n",
-    "print\"\\t t(0.05) :  F \\t\",t1\n",
-    "print\"\\t interval 2 \\t\"\n",
-    "# (Kxa*delV/L)= 0.05 to 0.15\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc1=(haV1*(T1-t1));\n",
-    "print\"\\t qc1 :  Btu/hr \\t\",qc1\n",
-    "delT1=(qc1/(C*G));\n",
-    "print\"\\t delT1 :  F \\t\",delT1\n",
-    "T2=(T1-delT1);\n",
-    "print\"\\t T(0.15) :  F \\t\",T2\n",
-    "X3=0.0748; # at 117.6F\n",
-    "w3=(nd1*w2*(0.0807-X3));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w3\n",
-    "w4=(w1-w3);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w4\n",
-    "l1=1027; # Btu/lb, l1= lamda at 117.6F\n",
-    "qd=(w3*l1);\n",
-    "print\"\\t qd :  Btu/hr \\t\",qd\n",
-    "q1=(qd+qc1);\n",
-    "print\"\\t q1 :  Btu/hr \\t\",q1\n",
-    "delt1=(q1/w2);\n",
-    "print\"\\t delt1 :  F \\t\",delt1\n",
-    "t2=(t1-delt1);\n",
-    "print\"\\t t(0.15) :  F \\t\",t2\n",
-    "X4=0.0640; # at 112.5\n",
-    "X5=(w4/G);\n",
-    "print\"\\t X(112.5F) :  lb/lb \\t\",X5\n",
-    "print\"\\t interval 3 \\t\"\n",
-    "# (Kxa*delV/L)= 0.15 to 0.25\n",
-    "nd1=0.1;\n",
-    "haV1=(nd1*w2*Le*C);\n",
-    "print\"\\t haV1 :  Btu/(hr)*(F) \\t\",haV1\n",
-    "qc2=(haV1*(T2-t2));\n",
-    "print\"\\t qc2 :  Btu/hr \\t\",qc2\n",
-    "delT2=(qc2/(C*G));\n",
-    "print\"\\t delT2 :  F \\t\",delT2\n",
-    "T3=(T2-delT2);\n",
-    "print\"\\t T(0.25) :  F \\t\",T3\n",
-    "w5=(nd1*w2*(X5-X4));\n",
-    "print\"\\t water diffused during interval :  lb/hr \\t\",w5\n",
-    "w6=(w4-w5);\n",
-    "print\"\\t water remaining :  lb/hr \\t\",w6\n",
-    "l2=1030; # Btu/lb, l1= lamda at 112.5F\n",
-    "qd1=(w5*l2);\n",
-    "print\"\\t qd1 :  Btu/hr \\t\",qd1\n",
-    "q2=(qd1+qc2);\n",
-    "print\"\\t q2 :  Btu/hr \\t\",q2\n",
-    "delt2=(q2/w2);\n",
-    "print\"\\t delt2 :  F \\t\",delt2\n",
-    "t3=(t2-delt2);\n",
-    "print\"\\t t(0.25) :  F \\t\",t3\n",
-    "X6=0.0533; # at 106.5\n",
-    "X7=(w6/G);\n",
-    "print\"\\t X(106.5F) :  lb/lb \\t\",X7\n",
-    "# The calculations of the remaining intervals until a. gas temperature of 200DegF is reached are shown in Fig. 17.17\n",
-    "w7=21.92; # total water diffused from table in solution\n",
-    "d=(w7/w1)*100;\n",
-    "print\"\\t calculated diffusion :  \\t\",d\n",
-    "print\"\\t Using some standard low-pressure-drop data \\t\"\n",
-    "# For G = 1500, extrapolate to L = 2040 on logarithmic coordinates. Kxa = 510.\n",
-    "ndt=.54; # from 1st table in solution\n",
-    "Kxa=510; # from 2nd table in solution\n",
-    "Z=(ndt*w2/Kxa);\n",
-    "print\"\\t tower height :  ft \\t\",Z\n",
-    "A=(50000/G);\n",
-    "print\"\\t cross section :  ft^2 \\t\",round(A,1)\n",
-    "# end\n",
-    "\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 17.7 pgno:620"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 17.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t sensible heat :  Btu/hr \t4200000.0\n",
-      "\t approximate diffusion :  Btu/hr \t756166.666667\n",
-      "\t total heat :  Btu/hr \t4956166.66667\n",
-      "\t total water quantity :  lb/hr \t141604.761905\n",
-      "\t tower cross section :  ft**2 \t69.4140989729\n",
-      "\t new gas rate :  lb/(hr)(ft**2) \t720.314759391\n",
-      "\t LMTD :  \t241.213395056\n",
-      "\t haV/L :  \t0.145099736239\n",
-      "\t number diffusion units :  \t0.557218649152\n",
-      "\t height of tower :  ft \t5.28709788033\n",
-      " ground dimensions :  ft \t1.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 17.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "C=0.28; # assumption\n",
-    "w=50000.; # lb/hr\n",
-    "G=1500.;\n",
-    "Qs=(w*C*(500-200));\n",
-    "Qd=(w/G)*(22685); # qd=22685, from previous prblm\n",
-    "from math import log\n",
-    "print\"\\t sensible heat :  Btu/hr \\t\",Qs\n",
-    "print\"\\t approximate diffusion :  Btu/hr \\t\",Qd\n",
-    "Q=(Qs+Qd);\n",
-    "print\"\\t total heat :  Btu/hr \\t\",Q\n",
-    "# an allowance as high as 30 per cent of the sensible load can be made and the excess water compensated for by throttling when the tower is in operation\n",
-    "w1=(Q/(120-85));\n",
-    "print\"\\t total water quantity :  lb/hr \\t\",w1\n",
-    "# If the maximum liquid loading is taken as 2040 lb/(hr)(ft'!), the required tower cross section\n",
-    "A=(w1/2040);\n",
-    "print\"\\t tower cross section :  ft**2 \\t\",A\n",
-    "w3=(w/A);\n",
-    "print\"\\t new gas rate :  lb/(hr)(ft**2) \\t\",w3\n",
-    "# The two terminal temperature differences are (200 - 85) and (500 - 120).\n",
-    "LMTD=((500-120)-(200-85))/(log((500-120)/(200-85)));\n",
-    "print\"\\t LMTD :  \\t\",LMTD\n",
-    "dt=35;\n",
-    "N=(dt/LMTD); # eq 17.88\n",
-    "print\"\\t haV/L :  \\t\",N\n",
-    "Le=0.93;\n",
-    "nd=(N/(C*Le));\n",
-    "print\"\\t number diffusion units :  \\t\",nd\n",
-    "# By extrapolation for G = 718 and L = 2040,Kxa=215\n",
-    "L=2040;\n",
-    "Kxa=215;\n",
-    "Z=(nd*L/Kxa); # calculation mistake\n",
-    "print\"\\t height of tower :  ft \\t\",Z\n",
-    "di=(A)**(1/2);\n",
-    "print\" ground dimensions :  ft \\t\",di\n",
-    "# ground dimensions are 5.8*8.3*8.3 ft\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes.ipynb
deleted file mode 100755
index cddac489..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes.ipynb
+++ /dev/null
@@ -1,634 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 18 Batch and Unsteady State Processes"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 18.1 pgno:635"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.1 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t weight of benzene is : lb \t54978.0\n",
-      "\t Q1 is : Btu/(hr)*(F) \t19200.0\n",
-      "\t Q2 is : Btu/(hr)*(F) \t6000.0\n",
-      "\t Ks is : \t0.101097824987\n",
-      "\t Z is : \t1.09861228867\n",
-      "\t theta is : hr \t5.20557650697\n",
-      "\t for b \t\n",
-      "\t R is : \t3.2\n",
-      "\t KT is : \t2.83393630769\n",
-      "\t S is : \t0.31793720236\n",
-      "\t theta1 is : hr \t5.67664533895\n",
-      "\t for c \t\n",
-      "\t K8 is : \t1.68342992361\n",
-      "\t S1 is : \t0.492221932725\n",
-      "\t theta2 is : hr \t5.35456617078\n",
-      "\t for d \t\n",
-      "\t K9 is : \t9.89140963346\n",
-      "\t S2 is : \t0.290071168513\n",
-      "\t t1 is : F \t187.021350554\n",
-      "\t t2 is : F \t248.800316267\n",
-      "\t t3 is : F \t292.658985206\n",
-      "\t t4 is : F \t323.795518797\n",
-      "\t fractional circulation is : \t0.23\n",
-      "\t total fractional circulation : \t3.23\n",
-      "\t theta3 is : \t4.44\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.1 \\t\"\n",
-    "# specific gravity of benzene is 0.88\n",
-    "# specific heat of benzene is 0.48 Btu/(lb)*(F)\n",
-    "U=50;\n",
-    "A=400;\n",
-    "T1=400;\n",
-    "t1=100;\n",
-    "t2=300;\n",
-    "c=0.48;\n",
-    "w=40000;\n",
-    "C=0.60;\n",
-    "W=10000;\n",
-    "from math import e\n",
-    "from math import log\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "M=(7500*8.33*0.88);\n",
-    "print\"\\t weight of benzene is : lb \\t\",M\n",
-    "Q1=(w*c);\n",
-    "print\"\\t Q1 is : Btu/(hr)*(F) \\t\",Q1\n",
-    "Q2=(W*C);\n",
-    "print\"\\t Q2 is : Btu/(hr)*(F) \\t\",Q2\n",
-    "Ks=((e)**(U*A*((1/Q1)-(1/Q2)))); # eq 18.16\n",
-    "print\"\\t Ks is : \\t\",Ks\n",
-    "Z=log((T1-t1)/(T1-t2));\n",
-    "print\"\\t Z is : \\t\",Z\n",
-    "theta=((M*(Z)*(Ks*6000-(19200)))/((Ks-1)*40000*6000));\n",
-    "print\"\\t theta is : hr \\t\",theta\n",
-    "print\"\\t for b \\t\"\n",
-    "R=(Q1/Q2);\n",
-    "print\"\\t R is : \\t\",R\n",
-    "KT=((e)**(U*(A/Q1)*(1+R**2)**(1/2)));\n",
-    "print\"\\t KT is : \\t\",KT\n",
-    "S=((2*(KT-1))/((KT*(R+1+(1+R**2)**(1/2)))-(R+1-(1+R**2)**(1/2)))); # eq 18.24\n",
-    "print\"\\t S is : \\t\",S\n",
-    "theta1=((M*Z)/(0.266*40000)); # eq 18.25\n",
-    "print\"\\t theta1 is : hr \\t\",theta1\n",
-    "print\"\\t for c \\t\"\n",
-    "U1=100;\n",
-    "A1=200;\n",
-    "K8=((e)**(U*(A/(2*Q1))*(1+R**2)**(1/2))); # eq 18.32\n",
-    "S1=((2*(K8-1)*(1+((1-0.266)*(1-(3.2*0.266)))**(1/2)))/(((K8-1)*(3.2+1))+((K8+1)*(1+3.2**2)**(1/2)))); # eq 18.31\n",
-    "print\"\\t K8 is : \\t\",K8\n",
-    "print\"\\t S1 is : \\t\",S1\n",
-    "theta2=((M*Z)/(0.282*40000)); # eq 18.25\n",
-    "print\"\\t theta2 is : hr \\t\",theta2\n",
-    "print\"\\t for d \\t\"\n",
-    "K9=((e)**(U*(A/(Q1))*(R-1)));\n",
-    "S2=((K9-1)/((K9*R)-1)); # eq 18.36\n",
-    "print\"\\t K9 is : \\t\",K9\n",
-    "print\"\\t S2 is : \\t\",S2\n",
-    "t=100;\n",
-    "t1=t+(S2*(T1-t)); # 18.37\n",
-    "print\"\\t t1 is : F \\t\",t1\n",
-    "t2=t1+(S2*(T1-t1));\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "t3=t2+(S2*(T1-t2));\n",
-    "print\"\\t t3 is : F \\t\",t3\n",
-    "t4=t3+(S2*(T1-t3));\n",
-    "print\"\\t t4 is : F \\t\",t4\n",
-    "x=0.23;\n",
-    "print\"\\t fractional circulation is : \\t\",x\n",
-    "N=3+x;\n",
-    "print\"\\t total fractional circulation : \\t\",N\n",
-    "theta3=(N*(M/w));\n",
-    "print\"\\t theta3 is : \\t\",round(theta3,2)\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 18.2 pgno:643"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.2 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X is : \t0.1665\n",
-      "\t t si : F \t872.2\n",
-      "\t q is : Btu/(hr)*(ft**2) \t21600.0\n",
-      "\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \t75200.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.2 \\t\"\n",
-    "tav=500.; # F\n",
-    "Ts=1000.; \n",
-    "t0=100.;\n",
-    "c=0.12; # Btu/(lb)*(F)\n",
-    "k=24; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=488; # lb/ft**3\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "x=0.333; # ft\n",
-    "theta=4;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X=(x/(2*(alpha*theta)**(1/2)));\n",
-    "print\"\\t X is : \\t\",X\n",
-    "Y=0.142; # Y=f1(X) from fig 18.7 \n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t si : F \\t\",t\n",
-    "q=((k*(Ts-t0))/(3.14*alpha*theta)**(1/2)); # q=(Q/A),from eq 18.47\n",
-    "print\"\\t q is : Btu/(hr)*(ft**2) \\t\",q\n",
-    "q1=(2*k*(Ts-t0)*(theta/(3.14*alpha))**(1/2))+32000; # q=(Q1/A). eq 18.49\n",
-    "print\"\\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \\t\",q1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.3 pgno:646"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.3 \n",
-      "\n",
-      "\t X is :   0.0\n",
-      "\t t si :  F 861.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.3 \\n\"\n",
-    "Ts=1000; \n",
-    "t0=100;\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=15/60;\n",
-    "l=1; # ft\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "print\"\\t X is :  \",X\n",
-    "Y=0.155; # Y=f3*(X)from fig 18.9 when L=infinity\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.52\n",
-    "print\"\\t t si :  F\",round(t)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.4 pgno:648"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.4 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \t6.870372355\n",
-      "\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.3\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t7.170372355\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t3.55\n",
-      "\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \t5.3601861775\n",
-      "\t X is :  \t9.07776\n",
-      "\t Y is :  \t0.0827189224923\n",
-      "\t t is :  F \t502.6\n",
-      "\t for b \t\n",
-      "\t temperature of center plane is :  F \t512.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.4 \\t\"\n",
-    "T1=1100.; # F\n",
-    "T2=70.; # F\n",
-    "t1=T1+460; # R\n",
-    "t2=T2+460; # R\n",
-    "k=27; # from appendix\n",
-    "c=0.14; # from appendix\n",
-    "row=490; # from appendix\n",
-    "alpha=0.394;\n",
-    "theta=4.;\n",
-    "l=10./12.; # ft\n",
-    "x=0.173*10**(-8); # stefan constant\n",
-    "e=0.7; # emmisivity\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "# Assume the temperature is 500DegF after 4 hr. The coefficient from plate to air is the sum of the radiation and convection coefficients\n",
-    "hri=(e*x*(t1**4-t2**4))/(T1-T2);\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hri # eq 4.32\n",
-    "hci=(0.3*(T1-T2)**(1/4)); # eq 10.10\n",
-    "print\"\\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hci\n",
-    "hti=hri+hci;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hti\n",
-    "# For the 4-hr coefficient at 500DegF\n",
-    "hr=2.2; # Btu/(hr)*(ft**2)*(F)\n",
-    "hc=1.35; # Btu/(hr)*(ft**2)*(F)\n",
-    "ht=hr+hc;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ht\n",
-    "h=(hti+ht)/2;\n",
-    "print\"\\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",h\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Y=(h*l)/(2*k);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Y is :  \\t\",Y\n",
-    "Z=0.42; # Z=f3(X,Y), from fig 18.10\n",
-    "t=T2+((T1-T2)*Z); # eq 18.53\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "print\"\\t for b \\t\"\n",
-    "Z1=0.43; # Z=f4(X,Y), from fig 18.11\n",
-    "t1=T2+((T1-T2)*Z1); # eq 18.53\n",
-    "print\"\\t temperature of center plane is :  F \\t\",t1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.5 pgno:651"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.5 \t\n",
-      "\t X is :  \t1.0125\n",
-      "\t Z is :  \t1.5\n",
-      "\t t is :  F \t338.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.5 \\t\"\n",
-    "Ts=400.;\n",
-    "t0=200.;\n",
-    "k=25.; # from appendix\n",
-    "c=0.12; # from appendix\n",
-    "row=490.; # from appendix\n",
-    "alpha=0.45; # alpha=(k/(c*row))\n",
-    "theta=15./60.;\n",
-    "l=8./12.; # ft\n",
-    "h=50;\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Z=(2*k)/(h*l);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "Y=0.31; # Y=(Ts-t)/(Ts-t0), from fig 18.13\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.6 pgno:656"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.6 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X1 is :  \t0.0827733333333\n",
-      "\t Z1 is :  \t0.19512195122\n",
-      "\t X2 is :  \t0.331093333333\n",
-      "\t Z2 is :  \t0.390243902439\n",
-      "\t X3 is :  \t1.0727424\n",
-      "\t Z3 is :  \t0.70243902439\n",
-      "\t at centre (2*x/l) is zero \t\n",
-      "\t at surface (2*x/l) is one \t\n",
-      "\t center of brick \t\n",
-      "\t t1 is :  F \t227.3085\n",
-      "\t corner of brick \t\n",
-      "\t t2 is :  F \t294.6890125\n",
-      "\t center of 9 by 4.5in face \t\n",
-      "\t t3 is :  F \t258.58275\n",
-      "\t center of 9 by 2.5in face \t\n",
-      "\t t4 is :  F \t271.89262\n",
-      "\t center of 4.5 by 2.5in face \t\n",
-      "\t t5 is :  F \t275.893125\n",
-      "\t middle of long edge \t\n",
-      "\t t6 is :  F \t284.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.6 \\t\"\n",
-    "Ts=300.; \n",
-    "t0=70.;\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "k=0.3; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=103.; # lb/ft**3\n",
-    "alpha=0.01164; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=1.;\n",
-    "lx=9./12.;\n",
-    "ly=4.5/12.;\n",
-    "lz=2.5/12.;\n",
-    "h=4.1;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X1=(4*alpha*theta)/(lx**2);\n",
-    "Z1=(2*k)/(h*lx);\n",
-    "print\"\\t X1 is :  \\t\",X1\n",
-    "print\"\\t Z1 is :  \\t\",Z1\n",
-    "X2=(4*alpha*theta)/(ly**2);\n",
-    "Z2=(2*k)/(h*ly);\n",
-    "print\"\\t X2 is :  \\t\",X2\n",
-    "print\"\\t Z2 is :  \\t\",Z2\n",
-    "X3=(4*alpha*theta)/(lz**2);\n",
-    "Z3=(2*k)/(h*lz);\n",
-    "print\"\\t X3 is :  \\t\",X3\n",
-    "print\"\\t Z3 is :  \\t\",Z3\n",
-    "print\"\\t at centre (2*x/l) is zero \\t\"\n",
-    "Yx=0.98; # fig 18.12\n",
-    "Yy=0.75; # fig 18.12\n",
-    "Yz=0.43; # fig 18.12\n",
-    "print\"\\t at surface (2*x/l) is one \\t\"\n",
-    "Yx1=0.325; # fig 18.12\n",
-    "Yy1=0.29; # fig 18.12\n",
-    "Yz1=0.245; # fig 18.12\n",
-    "print\"\\t center of brick \\t\"\n",
-    "t1=Ts-(Yx*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t1 is :  F \\t\",t1\n",
-    "print\"\\t corner of brick \\t\"\n",
-    "t2=Ts-(Yx1*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t center of 9 by 4.5in face \\t\"\n",
-    "t3=Ts-(Yx*Yy*Yz1*(Ts-t0));\n",
-    "print\"\\t t3 is :  F \\t\",t3\n",
-    "print\"\\t center of 9 by 2.5in face \\t\"\n",
-    "t4=Ts-(Yx*Yy1*Yz*(Ts-t0));\n",
-    "print\"\\t t4 is :  F \\t\",t4\n",
-    "print\"\\t center of 4.5 by 2.5in face \\t\"\n",
-    "t5=Ts-(Yx1*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t5 is :  F \\t\",t5\n",
-    "print\"\\t middle of long edge \\t\"\n",
-    "t6=Ts-(Yx*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t6 is :  F \\t\",round(t6)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.7 pgno:659"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t deltheta is : hr \t0.03486125\n",
-      "\t number of steps required :  \t9.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.7 \\t\"\n",
-    "t=20.; # min\n",
-    "alpha=0.40; # ft**2/hr\n",
-    "delx=0.167; # ft\n",
-    "# From the conditions of Eq. (18.61) take time increments such that alpha(deltheta/delx**2)=1/2\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "deltheta=(delx**2/(2*alpha));\n",
-    "print\"\\t deltheta is : hr \\t\",deltheta\n",
-    "N=(t/(deltheta*60));\n",
-    "print\"\\t number of steps required :  \\t\",round(N,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.8 pgno:662"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.8 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t temperature lag 6in below the surface \t\n",
-      "\t theta is :  hr \t6.45\n",
-      "\t amplitude \t\n",
-      "\t deltom is :  F \t30.0\n",
-      "\t delt is :  F \t5.8\n",
-      "\t temperature deviation after 2 hr \t\n",
-      "\t deltx is :  F \t2.9\n",
-      "\t heat flow during the half period \t\n",
-      "\t heat flow is :  Btu/(hr)*(ft**2) \t326.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.8 \\t\"\n",
-    "k=0.3;\n",
-    "row=103.;\n",
-    "c=0.25;\n",
-    "alpha=0.01164;\n",
-    "f=1./24.;\n",
-    "t1=120.;\n",
-    "t2=60.;\n",
-    "from math import e\n",
-    "from math import cos\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t temperature lag 6in below the surface \\t\"\n",
-    "x=6./12.;\n",
-    "theta=6.45#(x/2.)*(1/(3.14*f*alpha))**(1/2); # eq 18.65\n",
-    "print\"\\t theta is :  hr \\t\",theta\n",
-    "print\"\\t amplitude \\t\"\n",
-    "deltom=(t1-t2)/2;\n",
-    "print\"\\t deltom is :  F \\t\",deltom\n",
-    "delt=5.8#(deltom)*(2.71)**(-x*(3.14*f/alpha)**(1/2)); # eq 18.67\n",
-    "print\"\\t delt is :  F \\t\",delt # calculation mistake in book\n",
-    "print\"\\t temperature deviation after 2 hr \\t\"\n",
-    "theta1=2; # hr\n",
-    "deltx=delt/2#(deltom)*((e)**(-x*(3.14*f/alpha)**(1/2)))*cos((2*3.14*f*theta1)-(x*(3.14*f/alpha)**(1/2))); # eq 18.69\n",
-    "print\"\\t deltx is :  F \\t\",deltx\n",
-    "print\"\\t heat flow during the half period \\t\"\n",
-    "q=(k*deltom*(2/(3.14*f*alpha))**(1/2))*36.2; # eq 18.70\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft**2) \\t\",round(q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.9 pgno:670"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.9 \t\n",
-      "\t h is : \t79.0241510219\n",
-      "\t X is : \t20.8736476395\n",
-      "\t Y is : \t0.266666666667\n",
-      "\t x is : ft \t4.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.9 \\t\"\n",
-    "G=60.; # lb/(hr)*(ft**2)\n",
-    "De=1./12.; # ft\n",
-    "theta=6; # hr\n",
-    "cs=41.3; # Btu/(ft**3)*(F)\n",
-    "c=0.0191; # Btu/(ft**3)*(F)\n",
-    "f=0.45; # void fraction\n",
-    "T=90.;\n",
-    "T1=200;\n",
-    "t0=50;\n",
-    "h=(0.79*(G/De)**0.7); # eq 18.90\n",
-    "print\"\\t h is : \\t\",h\n",
-    "X=(h*theta/(cs*(1-f)));\n",
-    "Y=(T-t0)/(T1-t0);\n",
-    "print\"\\t X is : \\t\",X\n",
-    "print\"\\t Y is : \\t\",Y\n",
-    "row=0.0807; # lb/(ft**3) air\n",
-    "Z=24.5; # Z=(h*x*row/(c*G)), by comparing X an Y in fig 18.21\n",
-    "x=24.5*(c*G/(h*row));\n",
-    "print\"\\t x is : ft \\t\",round(x,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_1.ipynb
deleted file mode 100755
index 583cdf29..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_1.ipynb
+++ /dev/null
@@ -1,616 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 18 Batch and Unsteady State Processes"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 18.1 pgno:635"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.1 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t weight of benzene is : lb \t54978.0\n",
-      "\t Q1 is : Btu/(hr)*(F) \t19200.0\n",
-      "\t Q2 is : Btu/(hr)*(F) \t6000.0\n",
-      "\t Ks is : \t0.101097824987\n",
-      "\t Z is : \t1.09861228867\n",
-      "\t theta is : hr \t5.20557650697\n",
-      "\t for b \t\n",
-      "\t R is : \t3.2\n",
-      "\t KT is : \t2.83393630769\n",
-      "\t S is : \t0.31793720236\n",
-      "\t theta1 is : hr \t5.67664533895\n",
-      "\t for c \t\n",
-      "\t K8 is : \t1.68342992361\n",
-      "\t S1 is : \t0.492221932725\n",
-      "\t theta2 is : hr \t5.35456617078\n",
-      "\t for d \t\n",
-      "\t K9 is : \t9.89140963346\n",
-      "\t S2 is : \t0.290071168513\n",
-      "\t t1 is : F \t187.021350554\n",
-      "\t t2 is : F \t248.800316267\n",
-      "\t t3 is : F \t292.658985206\n",
-      "\t t4 is : F \t323.795518797\n",
-      "\t fractional circulation is : \t0.23\n",
-      "\t total fractional circulation : \t3.23\n",
-      "\t theta3 is : \t4.44\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.1 \\t\"\n",
-    "# specific gravity of benzene is 0.88\n",
-    "# specific heat of benzene is 0.48 Btu/(lb)*(F)\n",
-    "U=50;\n",
-    "A=400;\n",
-    "T1=400;\n",
-    "t1=100;\n",
-    "t2=300;\n",
-    "c=0.48;\n",
-    "w=40000;\n",
-    "C=0.60;\n",
-    "W=10000;\n",
-    "from math import e\n",
-    "from math import log\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "M=(7500*8.33*0.88);\n",
-    "print\"\\t weight of benzene is : lb \\t\",M\n",
-    "Q1=(w*c);\n",
-    "print\"\\t Q1 is : Btu/(hr)*(F) \\t\",Q1\n",
-    "Q2=(W*C);\n",
-    "print\"\\t Q2 is : Btu/(hr)*(F) \\t\",Q2\n",
-    "Ks=((e)**(U*A*((1/Q1)-(1/Q2)))); # eq 18.16\n",
-    "print\"\\t Ks is : \\t\",Ks\n",
-    "Z=log((T1-t1)/(T1-t2));\n",
-    "print\"\\t Z is : \\t\",Z\n",
-    "theta=((M*(Z)*(Ks*6000-(19200)))/((Ks-1)*40000*6000));\n",
-    "print\"\\t theta is : hr \\t\",theta\n",
-    "print\"\\t for b \\t\"\n",
-    "R=(Q1/Q2);\n",
-    "print\"\\t R is : \\t\",R\n",
-    "KT=((e)**(U*(A/Q1)*(1+R**2)**(1/2)));\n",
-    "print\"\\t KT is : \\t\",KT\n",
-    "S=((2*(KT-1))/((KT*(R+1+(1+R**2)**(1/2)))-(R+1-(1+R**2)**(1/2)))); # eq 18.24\n",
-    "print\"\\t S is : \\t\",S\n",
-    "theta1=((M*Z)/(0.266*40000)); # eq 18.25\n",
-    "print\"\\t theta1 is : hr \\t\",theta1\n",
-    "print\"\\t for c \\t\"\n",
-    "U1=100;\n",
-    "A1=200;\n",
-    "K8=((e)**(U*(A/(2*Q1))*(1+R**2)**(1/2))); # eq 18.32\n",
-    "S1=((2*(K8-1)*(1+((1-0.266)*(1-(3.2*0.266)))**(1/2)))/(((K8-1)*(3.2+1))+((K8+1)*(1+3.2**2)**(1/2)))); # eq 18.31\n",
-    "print\"\\t K8 is : \\t\",K8\n",
-    "print\"\\t S1 is : \\t\",S1\n",
-    "theta2=((M*Z)/(0.282*40000)); # eq 18.25\n",
-    "print\"\\t theta2 is : hr \\t\",theta2\n",
-    "print\"\\t for d \\t\"\n",
-    "K9=((e)**(U*(A/(Q1))*(R-1)));\n",
-    "S2=((K9-1)/((K9*R)-1)); # eq 18.36\n",
-    "print\"\\t K9 is : \\t\",K9\n",
-    "print\"\\t S2 is : \\t\",S2\n",
-    "t=100;\n",
-    "t1=t+(S2*(T1-t)); # 18.37\n",
-    "print\"\\t t1 is : F \\t\",t1\n",
-    "t2=t1+(S2*(T1-t1));\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "t3=t2+(S2*(T1-t2));\n",
-    "print\"\\t t3 is : F \\t\",t3\n",
-    "t4=t3+(S2*(T1-t3));\n",
-    "print\"\\t t4 is : F \\t\",t4\n",
-    "x=0.23;\n",
-    "print\"\\t fractional circulation is : \\t\",x\n",
-    "N=3+x;\n",
-    "print\"\\t total fractional circulation : \\t\",N\n",
-    "theta3=(N*(M/w));\n",
-    "print\"\\t theta3 is : \\t\",round(theta3,2)\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 18.2 pgno:643"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.2 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X is : \t0.1665\n",
-      "\t t si : F \t872.2\n",
-      "\t q is : Btu/(hr)*(ft**2) \t21600.0\n",
-      "\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \t75200.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.2 \\t\"\n",
-    "tav=500.; # F\n",
-    "Ts=1000.; \n",
-    "t0=100.;\n",
-    "c=0.12; # Btu/(lb)*(F)\n",
-    "k=24; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=488; # lb/ft**3\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "x=0.333; # ft\n",
-    "theta=4;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X=(x/(2*(alpha*theta)**(1/2)));\n",
-    "print\"\\t X is : \\t\",X\n",
-    "Y=0.142; # Y=f1(X) from fig 18.7 \n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t si : F \\t\",t\n",
-    "q=((k*(Ts-t0))/(3.14*alpha*theta)**(1/2)); # q=(Q/A),from eq 18.47\n",
-    "print\"\\t q is : Btu/(hr)*(ft**2) \\t\",q\n",
-    "q1=(2*k*(Ts-t0)*(theta/(3.14*alpha))**(1/2))+32000; # q=(Q1/A). eq 18.49\n",
-    "print\"\\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \\t\",q1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.3 pgno:646"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.3 \n",
-      "\n",
-      "\t X is :   0.0\n",
-      "\t t si :  F 861.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.3 \\n\"\n",
-    "Ts=1000; \n",
-    "t0=100;\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=15/60;\n",
-    "l=1; # ft\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "print\"\\t X is :  \",X\n",
-    "Y=0.155; # Y=f3*(X)from fig 18.9 when L=infinity\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.52\n",
-    "print\"\\t t si :  F\",round(t)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.4 pgno:648"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.4 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \t6.870372355\n",
-      "\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.3\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t7.170372355\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t3.55\n",
-      "\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \t5.3601861775\n",
-      "\t X is :  \t9.07776\n",
-      "\t Y is :  \t0.0827189224923\n",
-      "\t t is :  F \t502.6\n",
-      "\t for b \t\n",
-      "\t temperature of center plane is :  F \t512.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.4 \\t\"\n",
-    "T1=1100.; # F\n",
-    "T2=70.; # F\n",
-    "t1=T1+460; # R\n",
-    "t2=T2+460; # R\n",
-    "k=27; # from appendix\n",
-    "c=0.14; # from appendix\n",
-    "row=490; # from appendix\n",
-    "alpha=0.394;\n",
-    "theta=4.;\n",
-    "l=10./12.; # ft\n",
-    "x=0.173*10**(-8); # stefan constant\n",
-    "e=0.7; # emmisivity\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "# Assume the temperature is 500DegF after 4 hr. The coefficient from plate to air is the sum of the radiation and convection coefficients\n",
-    "hri=(e*x*(t1**4-t2**4))/(T1-T2);\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hri # eq 4.32\n",
-    "hci=(0.3*(T1-T2)**(1/4)); # eq 10.10\n",
-    "print\"\\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hci\n",
-    "hti=hri+hci;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hti\n",
-    "# For the 4-hr coefficient at 500DegF\n",
-    "hr=2.2; # Btu/(hr)*(ft**2)*(F)\n",
-    "hc=1.35; # Btu/(hr)*(ft**2)*(F)\n",
-    "ht=hr+hc;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ht\n",
-    "h=(hti+ht)/2;\n",
-    "print\"\\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",h\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Y=(h*l)/(2*k);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Y is :  \\t\",Y\n",
-    "Z=0.42; # Z=f3(X,Y), from fig 18.10\n",
-    "t=T2+((T1-T2)*Z); # eq 18.53\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "print\"\\t for b \\t\"\n",
-    "Z1=0.43; # Z=f4(X,Y), from fig 18.11\n",
-    "t1=T2+((T1-T2)*Z1); # eq 18.53\n",
-    "print\"\\t temperature of center plane is :  F \\t\",t1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.5 pgno:651"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.5 \t\n",
-      "\t X is :  \t1.0125\n",
-      "\t Z is :  \t1.5\n",
-      "\t t is :  F \t338.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.5 \\t\"\n",
-    "Ts=400.;\n",
-    "t0=200.;\n",
-    "k=25.; # from appendix\n",
-    "c=0.12; # from appendix\n",
-    "row=490.; # from appendix\n",
-    "alpha=0.45; # alpha=(k/(c*row))\n",
-    "theta=15./60.;\n",
-    "l=8./12.; # ft\n",
-    "h=50;\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Z=(2*k)/(h*l);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "Y=0.31; # Y=(Ts-t)/(Ts-t0), from fig 18.13\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.6 pgno:656"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.6 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X1 is :  \t0.0827733333333\n",
-      "\t Z1 is :  \t0.19512195122\n",
-      "\t X2 is :  \t0.331093333333\n",
-      "\t Z2 is :  \t0.390243902439\n",
-      "\t X3 is :  \t1.0727424\n",
-      "\t Z3 is :  \t0.70243902439\n",
-      "\t at centre (2*x/l) is zero \t\n",
-      "\t at surface (2*x/l) is one \t\n",
-      "\t center of brick \t\n",
-      "\t t1 is :  F \t227.3085\n",
-      "\t corner of brick \t\n",
-      "\t t2 is :  F \t294.6890125\n",
-      "\t center of 9 by 4.5in face \t\n",
-      "\t t3 is :  F \t258.58275\n",
-      "\t center of 9 by 2.5in face \t\n",
-      "\t t4 is :  F \t271.89262\n",
-      "\t center of 4.5 by 2.5in face \t\n",
-      "\t t5 is :  F \t275.893125\n",
-      "\t middle of long edge \t\n",
-      "\t t6 is :  F \t284.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.6 \\t\"\n",
-    "Ts=300.; \n",
-    "t0=70.;\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "k=0.3; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=103.; # lb/ft**3\n",
-    "alpha=0.01164; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=1.;\n",
-    "lx=9./12.;\n",
-    "ly=4.5/12.;\n",
-    "lz=2.5/12.;\n",
-    "h=4.1;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X1=(4*alpha*theta)/(lx**2);\n",
-    "Z1=(2*k)/(h*lx);\n",
-    "print\"\\t X1 is :  \\t\",X1\n",
-    "print\"\\t Z1 is :  \\t\",Z1\n",
-    "X2=(4*alpha*theta)/(ly**2);\n",
-    "Z2=(2*k)/(h*ly);\n",
-    "print\"\\t X2 is :  \\t\",X2\n",
-    "print\"\\t Z2 is :  \\t\",Z2\n",
-    "X3=(4*alpha*theta)/(lz**2);\n",
-    "Z3=(2*k)/(h*lz);\n",
-    "print\"\\t X3 is :  \\t\",X3\n",
-    "print\"\\t Z3 is :  \\t\",Z3\n",
-    "print\"\\t at centre (2*x/l) is zero \\t\"\n",
-    "Yx=0.98; # fig 18.12\n",
-    "Yy=0.75; # fig 18.12\n",
-    "Yz=0.43; # fig 18.12\n",
-    "print\"\\t at surface (2*x/l) is one \\t\"\n",
-    "Yx1=0.325; # fig 18.12\n",
-    "Yy1=0.29; # fig 18.12\n",
-    "Yz1=0.245; # fig 18.12\n",
-    "print\"\\t center of brick \\t\"\n",
-    "t1=Ts-(Yx*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t1 is :  F \\t\",t1\n",
-    "print\"\\t corner of brick \\t\"\n",
-    "t2=Ts-(Yx1*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t center of 9 by 4.5in face \\t\"\n",
-    "t3=Ts-(Yx*Yy*Yz1*(Ts-t0));\n",
-    "print\"\\t t3 is :  F \\t\",t3\n",
-    "print\"\\t center of 9 by 2.5in face \\t\"\n",
-    "t4=Ts-(Yx*Yy1*Yz*(Ts-t0));\n",
-    "print\"\\t t4 is :  F \\t\",t4\n",
-    "print\"\\t center of 4.5 by 2.5in face \\t\"\n",
-    "t5=Ts-(Yx1*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t5 is :  F \\t\",t5\n",
-    "print\"\\t middle of long edge \\t\"\n",
-    "t6=Ts-(Yx*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t6 is :  F \\t\",round(t6)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.7 pgno:659"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t deltheta is : hr \t0.03486125\n",
-      "\t number of steps required :  \t9.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.7 \\t\"\n",
-    "t=20.; # min\n",
-    "alpha=0.40; # ft**2/hr\n",
-    "delx=0.167; # ft\n",
-    "# From the conditions of Eq. (18.61) take time increments such that alpha(deltheta/delx**2)=1/2\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "deltheta=(delx**2/(2*alpha));\n",
-    "print\"\\t deltheta is : hr \\t\",deltheta\n",
-    "N=(t/(deltheta*60));\n",
-    "print\"\\t number of steps required :  \\t\",round(N,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.8 pgno:662"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.8 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t temperature lag 6in below the surface \t\n",
-      "\t theta is :  hr \t6.45\n",
-      "\t amplitude \t\n",
-      "\t deltom is :  F \t30.0\n",
-      "\t delt is :  F \t5.8\n",
-      "\t temperature deviation after 2 hr \t\n",
-      "\t deltx is :  F \t2.9\n",
-      "\t heat flow during the half period \t\n",
-      "\t heat flow is :  Btu/(hr)*(ft**2) \t326.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.8 \\t\"\n",
-    "k=0.3;\n",
-    "row=103.;\n",
-    "c=0.25;\n",
-    "alpha=0.01164;\n",
-    "f=1./24.;\n",
-    "t1=120.;\n",
-    "t2=60.;\n",
-    "from math import e\n",
-    "from math import cos\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t temperature lag 6in below the surface \\t\"\n",
-    "x=6./12.;\n",
-    "theta=6.45#(x/2.)*(1/(3.14*f*alpha))**(1/2); # eq 18.65\n",
-    "print\"\\t theta is :  hr \\t\",theta\n",
-    "print\"\\t amplitude \\t\"\n",
-    "deltom=(t1-t2)/2;\n",
-    "print\"\\t deltom is :  F \\t\",deltom\n",
-    "delt=5.8#(deltom)*(2.71)**(-x*(3.14*f/alpha)**(1/2)); # eq 18.67\n",
-    "print\"\\t delt is :  F \\t\",delt # calculation mistake in book\n",
-    "print\"\\t temperature deviation after 2 hr \\t\"\n",
-    "theta1=2; # hr\n",
-    "deltx=delt/2#(deltom)*((e)**(-x*(3.14*f/alpha)**(1/2)))*cos((2*3.14*f*theta1)-(x*(3.14*f/alpha)**(1/2))); # eq 18.69\n",
-    "print\"\\t deltx is :  F \\t\",deltx\n",
-    "print\"\\t heat flow during the half period \\t\"\n",
-    "q=(k*deltom*(2/(3.14*f*alpha))**(1/2))*36.2; # eq 18.70\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft**2) \\t\",round(q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.9 pgno:670"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.9 \t\n",
-      "\t h is : \t79.0241510219\n",
-      "\t X is : \t20.8736476395\n",
-      "\t Y is : \t0.266666666667\n",
-      "\t x is : ft \t4.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.9 \\t\"\n",
-    "G=60.; # lb/(hr)*(ft**2)\n",
-    "De=1./12.; # ft\n",
-    "theta=6; # hr\n",
-    "cs=41.3; # Btu/(ft**3)*(F)\n",
-    "c=0.0191; # Btu/(ft**3)*(F)\n",
-    "f=0.45; # void fraction\n",
-    "T=90.;\n",
-    "T1=200;\n",
-    "t0=50;\n",
-    "h=(0.79*(G/De)**0.7); # eq 18.90\n",
-    "print\"\\t h is : \\t\",h\n",
-    "X=(h*theta/(cs*(1-f)));\n",
-    "Y=(T-t0)/(T1-t0);\n",
-    "print\"\\t X is : \\t\",X\n",
-    "print\"\\t Y is : \\t\",Y\n",
-    "row=0.0807; # lb/(ft**3) air\n",
-    "Z=24.5; # Z=(h*x*row/(c*G)), by comparing X an Y in fig 18.21\n",
-    "x=24.5*(c*G/(h*row));\n",
-    "print\"\\t x is : ft \\t\",round(x,1)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_2.ipynb
deleted file mode 100755
index 09fa8a9f..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_2.ipynb
+++ /dev/null
@@ -1,616 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 18 Batch and Unsteady State Processes"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.1 pgno:635"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.1 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t weight of benzene is : lb \t54978.0\n",
-      "\t Q1 is : Btu/(hr)*(F) \t19200.0\n",
-      "\t Q2 is : Btu/(hr)*(F) \t6000.0\n",
-      "\t Ks is : \t0.101097824987\n",
-      "\t Z is : \t1.09861228867\n",
-      "\t theta is : hr \t5.20557650697\n",
-      "\t for b \t\n",
-      "\t R is : \t3.2\n",
-      "\t KT is : \t2.83393630769\n",
-      "\t S is : \t0.31793720236\n",
-      "\t theta1 is : hr \t5.67664533895\n",
-      "\t for c \t\n",
-      "\t K8 is : \t1.68342992361\n",
-      "\t S1 is : \t0.492221932725\n",
-      "\t theta2 is : hr \t5.35456617078\n",
-      "\t for d \t\n",
-      "\t K9 is : \t9.89140963346\n",
-      "\t S2 is : \t0.290071168513\n",
-      "\t t1 is : F \t187.021350554\n",
-      "\t t2 is : F \t248.800316267\n",
-      "\t t3 is : F \t292.658985206\n",
-      "\t t4 is : F \t323.795518797\n",
-      "\t fractional circulation is : \t0.23\n",
-      "\t total fractional circulation : \t3.23\n",
-      "\t theta3 is : \t4.44\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.1 \\t\"\n",
-    "# specific gravity of benzene is 0.88\n",
-    "# specific heat of benzene is 0.48 Btu/(lb)*(F)\n",
-    "U=50;\n",
-    "A=400;\n",
-    "T1=400;\n",
-    "t1=100;\n",
-    "t2=300;\n",
-    "c=0.48;\n",
-    "w=40000;\n",
-    "C=0.60;\n",
-    "W=10000;\n",
-    "from math import e\n",
-    "from math import log\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "M=(7500*8.33*0.88);\n",
-    "print\"\\t weight of benzene is : lb \\t\",M\n",
-    "Q1=(w*c);\n",
-    "print\"\\t Q1 is : Btu/(hr)*(F) \\t\",Q1\n",
-    "Q2=(W*C);\n",
-    "print\"\\t Q2 is : Btu/(hr)*(F) \\t\",Q2\n",
-    "Ks=((e)**(U*A*((1/Q1)-(1/Q2)))); # eq 18.16\n",
-    "print\"\\t Ks is : \\t\",Ks\n",
-    "Z=log((T1-t1)/(T1-t2));\n",
-    "print\"\\t Z is : \\t\",Z\n",
-    "theta=((M*(Z)*(Ks*6000-(19200)))/((Ks-1)*40000*6000));\n",
-    "print\"\\t theta is : hr \\t\",theta\n",
-    "print\"\\t for b \\t\"\n",
-    "R=(Q1/Q2);\n",
-    "print\"\\t R is : \\t\",R\n",
-    "KT=((e)**(U*(A/Q1)*(1+R**2)**(1/2)));\n",
-    "print\"\\t KT is : \\t\",KT\n",
-    "S=((2*(KT-1))/((KT*(R+1+(1+R**2)**(1/2)))-(R+1-(1+R**2)**(1/2)))); # eq 18.24\n",
-    "print\"\\t S is : \\t\",S\n",
-    "theta1=((M*Z)/(0.266*40000)); # eq 18.25\n",
-    "print\"\\t theta1 is : hr \\t\",theta1\n",
-    "print\"\\t for c \\t\"\n",
-    "U1=100;\n",
-    "A1=200;\n",
-    "K8=((e)**(U*(A/(2*Q1))*(1+R**2)**(1/2))); # eq 18.32\n",
-    "S1=((2*(K8-1)*(1+((1-0.266)*(1-(3.2*0.266)))**(1/2)))/(((K8-1)*(3.2+1))+((K8+1)*(1+3.2**2)**(1/2)))); # eq 18.31\n",
-    "print\"\\t K8 is : \\t\",K8\n",
-    "print\"\\t S1 is : \\t\",S1\n",
-    "theta2=((M*Z)/(0.282*40000)); # eq 18.25\n",
-    "print\"\\t theta2 is : hr \\t\",theta2\n",
-    "print\"\\t for d \\t\"\n",
-    "K9=((e)**(U*(A/(Q1))*(R-1)));\n",
-    "S2=((K9-1)/((K9*R)-1)); # eq 18.36\n",
-    "print\"\\t K9 is : \\t\",K9\n",
-    "print\"\\t S2 is : \\t\",S2\n",
-    "t=100;\n",
-    "t1=t+(S2*(T1-t)); # 18.37\n",
-    "print\"\\t t1 is : F \\t\",t1\n",
-    "t2=t1+(S2*(T1-t1));\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "t3=t2+(S2*(T1-t2));\n",
-    "print\"\\t t3 is : F \\t\",t3\n",
-    "t4=t3+(S2*(T1-t3));\n",
-    "print\"\\t t4 is : F \\t\",t4\n",
-    "x=0.23;\n",
-    "print\"\\t fractional circulation is : \\t\",x\n",
-    "N=3+x;\n",
-    "print\"\\t total fractional circulation : \\t\",N\n",
-    "theta3=(N*(M/w));\n",
-    "print\"\\t theta3 is : \\t\",round(theta3,2)\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 18.2 pgno:643"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.2 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X is : \t0.1665\n",
-      "\t t si : F \t872.2\n",
-      "\t q is : Btu/(hr)*(ft**2) \t21600.0\n",
-      "\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \t75200.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.2 \\t\"\n",
-    "tav=500.; # F\n",
-    "Ts=1000.; \n",
-    "t0=100.;\n",
-    "c=0.12; # Btu/(lb)*(F)\n",
-    "k=24; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=488; # lb/ft**3\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "x=0.333; # ft\n",
-    "theta=4;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X=(x/(2*(alpha*theta)**(1/2)));\n",
-    "print\"\\t X is : \\t\",X\n",
-    "Y=0.142; # Y=f1(X) from fig 18.7 \n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t si : F \\t\",t\n",
-    "q=((k*(Ts-t0))/(3.14*alpha*theta)**(1/2)); # q=(Q/A),from eq 18.47\n",
-    "print\"\\t q is : Btu/(hr)*(ft**2) \\t\",q\n",
-    "q1=(2*k*(Ts-t0)*(theta/(3.14*alpha))**(1/2))+32000; # q=(Q1/A). eq 18.49\n",
-    "print\"\\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \\t\",q1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.3 pgno:646"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.3 \n",
-      "\n",
-      "\t X is :   0.0\n",
-      "\t t si :  F 861.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.3 \\n\"\n",
-    "Ts=1000; \n",
-    "t0=100;\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=15/60;\n",
-    "l=1; # ft\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "print\"\\t X is :  \",X\n",
-    "Y=0.155; # Y=f3*(X)from fig 18.9 when L=infinity\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.52\n",
-    "print\"\\t t si :  F\",round(t)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.4 pgno:648"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.4 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \t6.870372355\n",
-      "\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.3\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t7.170372355\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t3.55\n",
-      "\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \t5.3601861775\n",
-      "\t X is :  \t9.07776\n",
-      "\t Y is :  \t0.0827189224923\n",
-      "\t t is :  F \t502.6\n",
-      "\t for b \t\n",
-      "\t temperature of center plane is :  F \t512.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.4 \\t\"\n",
-    "T1=1100.; # F\n",
-    "T2=70.; # F\n",
-    "t1=T1+460; # R\n",
-    "t2=T2+460; # R\n",
-    "k=27; # from appendix\n",
-    "c=0.14; # from appendix\n",
-    "row=490; # from appendix\n",
-    "alpha=0.394;\n",
-    "theta=4.;\n",
-    "l=10./12.; # ft\n",
-    "x=0.173*10**(-8); # stefan constant\n",
-    "e=0.7; # emmisivity\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "# Assume the temperature is 500DegF after 4 hr. The coefficient from plate to air is the sum of the radiation and convection coefficients\n",
-    "hri=(e*x*(t1**4-t2**4))/(T1-T2);\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hri # eq 4.32\n",
-    "hci=(0.3*(T1-T2)**(1/4)); # eq 10.10\n",
-    "print\"\\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hci\n",
-    "hti=hri+hci;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hti\n",
-    "# For the 4-hr coefficient at 500DegF\n",
-    "hr=2.2; # Btu/(hr)*(ft**2)*(F)\n",
-    "hc=1.35; # Btu/(hr)*(ft**2)*(F)\n",
-    "ht=hr+hc;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ht\n",
-    "h=(hti+ht)/2;\n",
-    "print\"\\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",h\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Y=(h*l)/(2*k);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Y is :  \\t\",Y\n",
-    "Z=0.42; # Z=f3(X,Y), from fig 18.10\n",
-    "t=T2+((T1-T2)*Z); # eq 18.53\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "print\"\\t for b \\t\"\n",
-    "Z1=0.43; # Z=f4(X,Y), from fig 18.11\n",
-    "t1=T2+((T1-T2)*Z1); # eq 18.53\n",
-    "print\"\\t temperature of center plane is :  F \\t\",t1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.5 pgno:651"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.5 \t\n",
-      "\t X is :  \t1.0125\n",
-      "\t Z is :  \t1.5\n",
-      "\t t is :  F \t338.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.5 \\t\"\n",
-    "Ts=400.;\n",
-    "t0=200.;\n",
-    "k=25.; # from appendix\n",
-    "c=0.12; # from appendix\n",
-    "row=490.; # from appendix\n",
-    "alpha=0.45; # alpha=(k/(c*row))\n",
-    "theta=15./60.;\n",
-    "l=8./12.; # ft\n",
-    "h=50;\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Z=(2*k)/(h*l);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "Y=0.31; # Y=(Ts-t)/(Ts-t0), from fig 18.13\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.6 pgno:656"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.6 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X1 is :  \t0.0827733333333\n",
-      "\t Z1 is :  \t0.19512195122\n",
-      "\t X2 is :  \t0.331093333333\n",
-      "\t Z2 is :  \t0.390243902439\n",
-      "\t X3 is :  \t1.0727424\n",
-      "\t Z3 is :  \t0.70243902439\n",
-      "\t at centre (2*x/l) is zero \t\n",
-      "\t at surface (2*x/l) is one \t\n",
-      "\t center of brick \t\n",
-      "\t t1 is :  F \t227.3085\n",
-      "\t corner of brick \t\n",
-      "\t t2 is :  F \t294.6890125\n",
-      "\t center of 9 by 4.5in face \t\n",
-      "\t t3 is :  F \t258.58275\n",
-      "\t center of 9 by 2.5in face \t\n",
-      "\t t4 is :  F \t271.89262\n",
-      "\t center of 4.5 by 2.5in face \t\n",
-      "\t t5 is :  F \t275.893125\n",
-      "\t middle of long edge \t\n",
-      "\t t6 is :  F \t284.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.6 \\t\"\n",
-    "Ts=300.; \n",
-    "t0=70.;\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "k=0.3; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=103.; # lb/ft**3\n",
-    "alpha=0.01164; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=1.;\n",
-    "lx=9./12.;\n",
-    "ly=4.5/12.;\n",
-    "lz=2.5/12.;\n",
-    "h=4.1;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X1=(4*alpha*theta)/(lx**2);\n",
-    "Z1=(2*k)/(h*lx);\n",
-    "print\"\\t X1 is :  \\t\",X1\n",
-    "print\"\\t Z1 is :  \\t\",Z1\n",
-    "X2=(4*alpha*theta)/(ly**2);\n",
-    "Z2=(2*k)/(h*ly);\n",
-    "print\"\\t X2 is :  \\t\",X2\n",
-    "print\"\\t Z2 is :  \\t\",Z2\n",
-    "X3=(4*alpha*theta)/(lz**2);\n",
-    "Z3=(2*k)/(h*lz);\n",
-    "print\"\\t X3 is :  \\t\",X3\n",
-    "print\"\\t Z3 is :  \\t\",Z3\n",
-    "print\"\\t at centre (2*x/l) is zero \\t\"\n",
-    "Yx=0.98; # fig 18.12\n",
-    "Yy=0.75; # fig 18.12\n",
-    "Yz=0.43; # fig 18.12\n",
-    "print\"\\t at surface (2*x/l) is one \\t\"\n",
-    "Yx1=0.325; # fig 18.12\n",
-    "Yy1=0.29; # fig 18.12\n",
-    "Yz1=0.245; # fig 18.12\n",
-    "print\"\\t center of brick \\t\"\n",
-    "t1=Ts-(Yx*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t1 is :  F \\t\",t1\n",
-    "print\"\\t corner of brick \\t\"\n",
-    "t2=Ts-(Yx1*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t center of 9 by 4.5in face \\t\"\n",
-    "t3=Ts-(Yx*Yy*Yz1*(Ts-t0));\n",
-    "print\"\\t t3 is :  F \\t\",t3\n",
-    "print\"\\t center of 9 by 2.5in face \\t\"\n",
-    "t4=Ts-(Yx*Yy1*Yz*(Ts-t0));\n",
-    "print\"\\t t4 is :  F \\t\",t4\n",
-    "print\"\\t center of 4.5 by 2.5in face \\t\"\n",
-    "t5=Ts-(Yx1*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t5 is :  F \\t\",t5\n",
-    "print\"\\t middle of long edge \\t\"\n",
-    "t6=Ts-(Yx*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t6 is :  F \\t\",round(t6)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.7 pgno:659"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t deltheta is : hr \t0.03486125\n",
-      "\t number of steps required :  \t9.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.7 \\t\"\n",
-    "t=20.; # min\n",
-    "alpha=0.40; # ft**2/hr\n",
-    "delx=0.167; # ft\n",
-    "# From the conditions of Eq. (18.61) take time increments such that alpha(deltheta/delx**2)=1/2\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "deltheta=(delx**2/(2*alpha));\n",
-    "print\"\\t deltheta is : hr \\t\",deltheta\n",
-    "N=(t/(deltheta*60));\n",
-    "print\"\\t number of steps required :  \\t\",round(N,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.8 pgno:662"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.8 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t temperature lag 6in below the surface \t\n",
-      "\t theta is :  hr \t6.45\n",
-      "\t amplitude \t\n",
-      "\t deltom is :  F \t30.0\n",
-      "\t delt is :  F \t5.8\n",
-      "\t temperature deviation after 2 hr \t\n",
-      "\t deltx is :  F \t2.9\n",
-      "\t heat flow during the half period \t\n",
-      "\t heat flow is :  Btu/(hr)*(ft**2) \t326.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.8 \\t\"\n",
-    "k=0.3;\n",
-    "row=103.;\n",
-    "c=0.25;\n",
-    "alpha=0.01164;\n",
-    "f=1./24.;\n",
-    "t1=120.;\n",
-    "t2=60.;\n",
-    "from math import e\n",
-    "from math import cos\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t temperature lag 6in below the surface \\t\"\n",
-    "x=6./12.;\n",
-    "theta=6.45#(x/2.)*(1/(3.14*f*alpha))**(1/2); # eq 18.65\n",
-    "print\"\\t theta is :  hr \\t\",theta\n",
-    "print\"\\t amplitude \\t\"\n",
-    "deltom=(t1-t2)/2;\n",
-    "print\"\\t deltom is :  F \\t\",deltom\n",
-    "delt=5.8#(deltom)*(2.71)**(-x*(3.14*f/alpha)**(1/2)); # eq 18.67\n",
-    "print\"\\t delt is :  F \\t\",delt # calculation mistake in book\n",
-    "print\"\\t temperature deviation after 2 hr \\t\"\n",
-    "theta1=2; # hr\n",
-    "deltx=delt/2#(deltom)*((e)**(-x*(3.14*f/alpha)**(1/2)))*cos((2*3.14*f*theta1)-(x*(3.14*f/alpha)**(1/2))); # eq 18.69\n",
-    "print\"\\t deltx is :  F \\t\",deltx\n",
-    "print\"\\t heat flow during the half period \\t\"\n",
-    "q=(k*deltom*(2/(3.14*f*alpha))**(1/2))*36.2; # eq 18.70\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft**2) \\t\",round(q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.9 pgno:670"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.9 \t\n",
-      "\t h is : \t79.0241510219\n",
-      "\t X is : \t20.8736476395\n",
-      "\t Y is : \t0.266666666667\n",
-      "\t x is : ft \t4.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.9 \\t\"\n",
-    "G=60.; # lb/(hr)*(ft**2)\n",
-    "De=1./12.; # ft\n",
-    "theta=6; # hr\n",
-    "cs=41.3; # Btu/(ft**3)*(F)\n",
-    "c=0.0191; # Btu/(ft**3)*(F)\n",
-    "f=0.45; # void fraction\n",
-    "T=90.;\n",
-    "T1=200;\n",
-    "t0=50;\n",
-    "h=(0.79*(G/De)**0.7); # eq 18.90\n",
-    "print\"\\t h is : \\t\",h\n",
-    "X=(h*theta/(cs*(1-f)));\n",
-    "Y=(T-t0)/(T1-t0);\n",
-    "print\"\\t X is : \\t\",X\n",
-    "print\"\\t Y is : \\t\",Y\n",
-    "row=0.0807; # lb/(ft**3) air\n",
-    "Z=24.5; # Z=(h*x*row/(c*G)), by comparing X an Y in fig 18.21\n",
-    "x=24.5*(c*G/(h*row));\n",
-    "print\"\\t x is : ft \\t\",round(x,1)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_3.ipynb
deleted file mode 100755
index 09fa8a9f..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_18_Batch_and_Unsteady_State_Processes_3.ipynb
+++ /dev/null
@@ -1,616 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 18 Batch and Unsteady State Processes"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.1 pgno:635"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.1 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t weight of benzene is : lb \t54978.0\n",
-      "\t Q1 is : Btu/(hr)*(F) \t19200.0\n",
-      "\t Q2 is : Btu/(hr)*(F) \t6000.0\n",
-      "\t Ks is : \t0.101097824987\n",
-      "\t Z is : \t1.09861228867\n",
-      "\t theta is : hr \t5.20557650697\n",
-      "\t for b \t\n",
-      "\t R is : \t3.2\n",
-      "\t KT is : \t2.83393630769\n",
-      "\t S is : \t0.31793720236\n",
-      "\t theta1 is : hr \t5.67664533895\n",
-      "\t for c \t\n",
-      "\t K8 is : \t1.68342992361\n",
-      "\t S1 is : \t0.492221932725\n",
-      "\t theta2 is : hr \t5.35456617078\n",
-      "\t for d \t\n",
-      "\t K9 is : \t9.89140963346\n",
-      "\t S2 is : \t0.290071168513\n",
-      "\t t1 is : F \t187.021350554\n",
-      "\t t2 is : F \t248.800316267\n",
-      "\t t3 is : F \t292.658985206\n",
-      "\t t4 is : F \t323.795518797\n",
-      "\t fractional circulation is : \t0.23\n",
-      "\t total fractional circulation : \t3.23\n",
-      "\t theta3 is : \t4.44\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.1 \\t\"\n",
-    "# specific gravity of benzene is 0.88\n",
-    "# specific heat of benzene is 0.48 Btu/(lb)*(F)\n",
-    "U=50;\n",
-    "A=400;\n",
-    "T1=400;\n",
-    "t1=100;\n",
-    "t2=300;\n",
-    "c=0.48;\n",
-    "w=40000;\n",
-    "C=0.60;\n",
-    "W=10000;\n",
-    "from math import e\n",
-    "from math import log\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "M=(7500*8.33*0.88);\n",
-    "print\"\\t weight of benzene is : lb \\t\",M\n",
-    "Q1=(w*c);\n",
-    "print\"\\t Q1 is : Btu/(hr)*(F) \\t\",Q1\n",
-    "Q2=(W*C);\n",
-    "print\"\\t Q2 is : Btu/(hr)*(F) \\t\",Q2\n",
-    "Ks=((e)**(U*A*((1/Q1)-(1/Q2)))); # eq 18.16\n",
-    "print\"\\t Ks is : \\t\",Ks\n",
-    "Z=log((T1-t1)/(T1-t2));\n",
-    "print\"\\t Z is : \\t\",Z\n",
-    "theta=((M*(Z)*(Ks*6000-(19200)))/((Ks-1)*40000*6000));\n",
-    "print\"\\t theta is : hr \\t\",theta\n",
-    "print\"\\t for b \\t\"\n",
-    "R=(Q1/Q2);\n",
-    "print\"\\t R is : \\t\",R\n",
-    "KT=((e)**(U*(A/Q1)*(1+R**2)**(1/2)));\n",
-    "print\"\\t KT is : \\t\",KT\n",
-    "S=((2*(KT-1))/((KT*(R+1+(1+R**2)**(1/2)))-(R+1-(1+R**2)**(1/2)))); # eq 18.24\n",
-    "print\"\\t S is : \\t\",S\n",
-    "theta1=((M*Z)/(0.266*40000)); # eq 18.25\n",
-    "print\"\\t theta1 is : hr \\t\",theta1\n",
-    "print\"\\t for c \\t\"\n",
-    "U1=100;\n",
-    "A1=200;\n",
-    "K8=((e)**(U*(A/(2*Q1))*(1+R**2)**(1/2))); # eq 18.32\n",
-    "S1=((2*(K8-1)*(1+((1-0.266)*(1-(3.2*0.266)))**(1/2)))/(((K8-1)*(3.2+1))+((K8+1)*(1+3.2**2)**(1/2)))); # eq 18.31\n",
-    "print\"\\t K8 is : \\t\",K8\n",
-    "print\"\\t S1 is : \\t\",S1\n",
-    "theta2=((M*Z)/(0.282*40000)); # eq 18.25\n",
-    "print\"\\t theta2 is : hr \\t\",theta2\n",
-    "print\"\\t for d \\t\"\n",
-    "K9=((e)**(U*(A/(Q1))*(R-1)));\n",
-    "S2=((K9-1)/((K9*R)-1)); # eq 18.36\n",
-    "print\"\\t K9 is : \\t\",K9\n",
-    "print\"\\t S2 is : \\t\",S2\n",
-    "t=100;\n",
-    "t1=t+(S2*(T1-t)); # 18.37\n",
-    "print\"\\t t1 is : F \\t\",t1\n",
-    "t2=t1+(S2*(T1-t1));\n",
-    "print\"\\t t2 is : F \\t\",t2\n",
-    "t3=t2+(S2*(T1-t2));\n",
-    "print\"\\t t3 is : F \\t\",t3\n",
-    "t4=t3+(S2*(T1-t3));\n",
-    "print\"\\t t4 is : F \\t\",t4\n",
-    "x=0.23;\n",
-    "print\"\\t fractional circulation is : \\t\",x\n",
-    "N=3+x;\n",
-    "print\"\\t total fractional circulation : \\t\",N\n",
-    "theta3=(N*(M/w));\n",
-    "print\"\\t theta3 is : \\t\",round(theta3,2)\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 18.2 pgno:643"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.2 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X is : \t0.1665\n",
-      "\t t si : F \t872.2\n",
-      "\t q is : Btu/(hr)*(ft**2) \t21600.0\n",
-      "\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \t75200.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.2 \\t\"\n",
-    "tav=500.; # F\n",
-    "Ts=1000.; \n",
-    "t0=100.;\n",
-    "c=0.12; # Btu/(lb)*(F)\n",
-    "k=24; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=488; # lb/ft**3\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "x=0.333; # ft\n",
-    "theta=4;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X=(x/(2*(alpha*theta)**(1/2)));\n",
-    "print\"\\t X is : \\t\",X\n",
-    "Y=0.142; # Y=f1(X) from fig 18.7 \n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t si : F \\t\",t\n",
-    "q=((k*(Ts-t0))/(3.14*alpha*theta)**(1/2)); # q=(Q/A),from eq 18.47\n",
-    "print\"\\t q is : Btu/(hr)*(ft**2) \\t\",q\n",
-    "q1=(2*k*(Ts-t0)*(theta/(3.14*alpha))**(1/2))+32000; # q=(Q1/A). eq 18.49\n",
-    "print\"\\t The total heat which flowed through a square foot of wall in the 4 hr is :  Btu/ft**2 \\t\",q1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.3 pgno:646"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.3 \n",
-      "\n",
-      "\t X is :   0.0\n",
-      "\t t si :  F 861.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.3 \\n\"\n",
-    "Ts=1000; \n",
-    "t0=100;\n",
-    "alpha=0.41; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=15/60;\n",
-    "l=1; # ft\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "print\"\\t X is :  \",X\n",
-    "Y=0.155; # Y=f3*(X)from fig 18.9 when L=infinity\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.52\n",
-    "print\"\\t t si :  F\",round(t)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.4 pgno:648"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.4 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t for a \t\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \t6.870372355\n",
-      "\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \t0.3\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t7.170372355\n",
-      "\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \t3.55\n",
-      "\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \t5.3601861775\n",
-      "\t X is :  \t9.07776\n",
-      "\t Y is :  \t0.0827189224923\n",
-      "\t t is :  F \t502.6\n",
-      "\t for b \t\n",
-      "\t temperature of center plane is :  F \t512.9\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.4 \\t\"\n",
-    "T1=1100.; # F\n",
-    "T2=70.; # F\n",
-    "t1=T1+460; # R\n",
-    "t2=T2+460; # R\n",
-    "k=27; # from appendix\n",
-    "c=0.14; # from appendix\n",
-    "row=490; # from appendix\n",
-    "alpha=0.394;\n",
-    "theta=4.;\n",
-    "l=10./12.; # ft\n",
-    "x=0.173*10**(-8); # stefan constant\n",
-    "e=0.7; # emmisivity\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "print\"\\t for a \\t\"\n",
-    "# Assume the temperature is 500DegF after 4 hr. The coefficient from plate to air is the sum of the radiation and convection coefficients\n",
-    "hri=(e*x*(t1**4-t2**4))/(T1-T2);\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hri # eq 4.32\n",
-    "hci=(0.3*(T1-T2)**(1/4)); # eq 10.10\n",
-    "print\"\\t convection coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hci\n",
-    "hti=hri+hci;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",hti\n",
-    "# For the 4-hr coefficient at 500DegF\n",
-    "hr=2.2; # Btu/(hr)*(ft**2)*(F)\n",
-    "hc=1.35; # Btu/(hr)*(ft**2)*(F)\n",
-    "ht=hr+hc;\n",
-    "print\"\\t total intial coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ht\n",
-    "h=(hti+ht)/2;\n",
-    "print\"\\t mean coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",h\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Y=(h*l)/(2*k);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Y is :  \\t\",Y\n",
-    "Z=0.42; # Z=f3(X,Y), from fig 18.10\n",
-    "t=T2+((T1-T2)*Z); # eq 18.53\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "print\"\\t for b \\t\"\n",
-    "Z1=0.43; # Z=f4(X,Y), from fig 18.11\n",
-    "t1=T2+((T1-T2)*Z1); # eq 18.53\n",
-    "print\"\\t temperature of center plane is :  F \\t\",t1\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.5 pgno:651"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.5 \t\n",
-      "\t X is :  \t1.0125\n",
-      "\t Z is :  \t1.5\n",
-      "\t t is :  F \t338.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.5 \\t\"\n",
-    "Ts=400.;\n",
-    "t0=200.;\n",
-    "k=25.; # from appendix\n",
-    "c=0.12; # from appendix\n",
-    "row=490.; # from appendix\n",
-    "alpha=0.45; # alpha=(k/(c*row))\n",
-    "theta=15./60.;\n",
-    "l=8./12.; # ft\n",
-    "h=50;\n",
-    "X=(4*alpha*theta)/(l**2);\n",
-    "Z=(2*k)/(h*l);\n",
-    "print\"\\t X is :  \\t\",X\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "Y=0.31; # Y=(Ts-t)/(Ts-t0), from fig 18.13\n",
-    "t=Ts+(t0-Ts)*(Y); # eq 18.43\n",
-    "print\"\\t t is :  F \\t\",t\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.6 pgno:656"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.6 \t\n",
-      "\t values are approximately mentioned in the book \t\n",
-      "\t X1 is :  \t0.0827733333333\n",
-      "\t Z1 is :  \t0.19512195122\n",
-      "\t X2 is :  \t0.331093333333\n",
-      "\t Z2 is :  \t0.390243902439\n",
-      "\t X3 is :  \t1.0727424\n",
-      "\t Z3 is :  \t0.70243902439\n",
-      "\t at centre (2*x/l) is zero \t\n",
-      "\t at surface (2*x/l) is one \t\n",
-      "\t center of brick \t\n",
-      "\t t1 is :  F \t227.3085\n",
-      "\t corner of brick \t\n",
-      "\t t2 is :  F \t294.6890125\n",
-      "\t center of 9 by 4.5in face \t\n",
-      "\t t3 is :  F \t258.58275\n",
-      "\t center of 9 by 2.5in face \t\n",
-      "\t t4 is :  F \t271.89262\n",
-      "\t center of 4.5 by 2.5in face \t\n",
-      "\t t5 is :  F \t275.893125\n",
-      "\t middle of long edge \t\n",
-      "\t t6 is :  F \t284.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.6 \\t\"\n",
-    "Ts=300.; \n",
-    "t0=70.;\n",
-    "c=0.25; # Btu/(lb)*(F)\n",
-    "k=0.3; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "row=103.; # lb/ft**3\n",
-    "alpha=0.01164; # alpha=(k/(c*row)), ft**2/hr\n",
-    "theta=1.;\n",
-    "lx=9./12.;\n",
-    "ly=4.5/12.;\n",
-    "lz=2.5/12.;\n",
-    "h=4.1;\n",
-    "print\"\\t values are approximately mentioned in the book \\t\"\n",
-    "X1=(4*alpha*theta)/(lx**2);\n",
-    "Z1=(2*k)/(h*lx);\n",
-    "print\"\\t X1 is :  \\t\",X1\n",
-    "print\"\\t Z1 is :  \\t\",Z1\n",
-    "X2=(4*alpha*theta)/(ly**2);\n",
-    "Z2=(2*k)/(h*ly);\n",
-    "print\"\\t X2 is :  \\t\",X2\n",
-    "print\"\\t Z2 is :  \\t\",Z2\n",
-    "X3=(4*alpha*theta)/(lz**2);\n",
-    "Z3=(2*k)/(h*lz);\n",
-    "print\"\\t X3 is :  \\t\",X3\n",
-    "print\"\\t Z3 is :  \\t\",Z3\n",
-    "print\"\\t at centre (2*x/l) is zero \\t\"\n",
-    "Yx=0.98; # fig 18.12\n",
-    "Yy=0.75; # fig 18.12\n",
-    "Yz=0.43; # fig 18.12\n",
-    "print\"\\t at surface (2*x/l) is one \\t\"\n",
-    "Yx1=0.325; # fig 18.12\n",
-    "Yy1=0.29; # fig 18.12\n",
-    "Yz1=0.245; # fig 18.12\n",
-    "print\"\\t center of brick \\t\"\n",
-    "t1=Ts-(Yx*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t1 is :  F \\t\",t1\n",
-    "print\"\\t corner of brick \\t\"\n",
-    "t2=Ts-(Yx1*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t2 is :  F \\t\",t2\n",
-    "print\"\\t center of 9 by 4.5in face \\t\"\n",
-    "t3=Ts-(Yx*Yy*Yz1*(Ts-t0));\n",
-    "print\"\\t t3 is :  F \\t\",t3\n",
-    "print\"\\t center of 9 by 2.5in face \\t\"\n",
-    "t4=Ts-(Yx*Yy1*Yz*(Ts-t0));\n",
-    "print\"\\t t4 is :  F \\t\",t4\n",
-    "print\"\\t center of 4.5 by 2.5in face \\t\"\n",
-    "t5=Ts-(Yx1*Yy*Yz*(Ts-t0));\n",
-    "print\"\\t t5 is :  F \\t\",t5\n",
-    "print\"\\t middle of long edge \\t\"\n",
-    "t6=Ts-(Yx*Yy1*Yz1*(Ts-t0));\n",
-    "print\"\\t t6 is :  F \\t\",round(t6)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.7 pgno:659"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t deltheta is : hr \t0.03486125\n",
-      "\t number of steps required :  \t9.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.7 \\t\"\n",
-    "t=20.; # min\n",
-    "alpha=0.40; # ft**2/hr\n",
-    "delx=0.167; # ft\n",
-    "# From the conditions of Eq. (18.61) take time increments such that alpha(deltheta/delx**2)=1/2\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "deltheta=(delx**2/(2*alpha));\n",
-    "print\"\\t deltheta is : hr \\t\",deltheta\n",
-    "N=(t/(deltheta*60));\n",
-    "print\"\\t number of steps required :  \\t\",round(N,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.8 pgno:662"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.8 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t temperature lag 6in below the surface \t\n",
-      "\t theta is :  hr \t6.45\n",
-      "\t amplitude \t\n",
-      "\t deltom is :  F \t30.0\n",
-      "\t delt is :  F \t5.8\n",
-      "\t temperature deviation after 2 hr \t\n",
-      "\t deltx is :  F \t2.9\n",
-      "\t heat flow during the half period \t\n",
-      "\t heat flow is :  Btu/(hr)*(ft**2) \t326.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.8 \\t\"\n",
-    "k=0.3;\n",
-    "row=103.;\n",
-    "c=0.25;\n",
-    "alpha=0.01164;\n",
-    "f=1./24.;\n",
-    "t1=120.;\n",
-    "t2=60.;\n",
-    "from math import e\n",
-    "from math import cos\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t temperature lag 6in below the surface \\t\"\n",
-    "x=6./12.;\n",
-    "theta=6.45#(x/2.)*(1/(3.14*f*alpha))**(1/2); # eq 18.65\n",
-    "print\"\\t theta is :  hr \\t\",theta\n",
-    "print\"\\t amplitude \\t\"\n",
-    "deltom=(t1-t2)/2;\n",
-    "print\"\\t deltom is :  F \\t\",deltom\n",
-    "delt=5.8#(deltom)*(2.71)**(-x*(3.14*f/alpha)**(1/2)); # eq 18.67\n",
-    "print\"\\t delt is :  F \\t\",delt # calculation mistake in book\n",
-    "print\"\\t temperature deviation after 2 hr \\t\"\n",
-    "theta1=2; # hr\n",
-    "deltx=delt/2#(deltom)*((e)**(-x*(3.14*f/alpha)**(1/2)))*cos((2*3.14*f*theta1)-(x*(3.14*f/alpha)**(1/2))); # eq 18.69\n",
-    "print\"\\t deltx is :  F \\t\",deltx\n",
-    "print\"\\t heat flow during the half period \\t\"\n",
-    "q=(k*deltom*(2/(3.14*f*alpha))**(1/2))*36.2; # eq 18.70\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft**2) \\t\",round(q)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 18.9 pgno:670"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 18.9 \t\n",
-      "\t h is : \t79.0241510219\n",
-      "\t X is : \t20.8736476395\n",
-      "\t Y is : \t0.266666666667\n",
-      "\t x is : ft \t4.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 18.9 \\t\"\n",
-    "G=60.; # lb/(hr)*(ft**2)\n",
-    "De=1./12.; # ft\n",
-    "theta=6; # hr\n",
-    "cs=41.3; # Btu/(ft**3)*(F)\n",
-    "c=0.0191; # Btu/(ft**3)*(F)\n",
-    "f=0.45; # void fraction\n",
-    "T=90.;\n",
-    "T1=200;\n",
-    "t0=50;\n",
-    "h=(0.79*(G/De)**0.7); # eq 18.90\n",
-    "print\"\\t h is : \\t\",h\n",
-    "X=(h*theta/(cs*(1-f)));\n",
-    "Y=(T-t0)/(T1-t0);\n",
-    "print\"\\t X is : \\t\",X\n",
-    "print\"\\t Y is : \\t\",Y\n",
-    "row=0.0807; # lb/(ft**3) air\n",
-    "Z=24.5; # Z=(h*x*row/(c*G)), by comparing X an Y in fig 18.21\n",
-    "x=24.5*(c*G/(h*row));\n",
-    "print\"\\t x is : ft \\t\",round(x,1)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations.ipynb
deleted file mode 100755
index 072bc832..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations.ipynb
+++ /dev/null
@@ -1,401 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 19: Furnace Calculations"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.1 pgno:702 "
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.1 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t heat liberated by the fuel : Btu/hr \t66666666.6667\n",
-      "\t fuel quantity : lb/hr \t3891.8077447\n",
-      "\t air required : lb/hr \t67873.1270675\n",
-      "\t steam for atomizing : lb/hr \t1167.54232341\n",
-      "\t QA is : Btu/hr \t5565596.41954\n",
-      "\t QS is negligible \t\n",
-      "\t QW is : Btu/hr \t1333333.33333\n",
-      "\t Qnet is : Btu/hr \t70898929.7529\n",
-      "\t QG is : Btu/hr \t34715859.1166\n",
-      "\t Q1 is : Btu/hr \t36183070.6363\n",
-      "\t area of tube is : ft**2 \t50.3708333333\n",
-      "\t estimated number of tubes : \t59.8611475495\n",
-      "\t cold plane surface per tube : ft**2 \t27.2708333333\n",
-      "\t Acp1 is : ft**2 \t25.5527708333\n",
-      "\t total cold plane surface is : ft**2 \t1529.61818515\n",
-      "\t surface of end walls : ft**2 \t610.5264\n",
-      "\t surface of side wall : ft**2 \t574.42\n",
-      "\t surface of bridge walls : ft**2 \t376.915\n",
-      "\t surface of floor and arch : ft**2 \t1575.42\n",
-      "\t AT is : ft**2 \t3137.2814\n",
-      "\t AR is : ft**2 \t1607.66321485\n",
-      "\t ratio of areas is : \t1.05102255612\n",
-      "\t dimension ratio is 3:2:1 \t\n",
-      "\t length is : ft \t0.0\n",
-      "\t gas emissivity \t\n",
-      "\t percentage correction at P : \t0.464837049743\n",
-      "\t Pt is : \t3.5\n",
-      "\t eG is : \t0\n",
-      "\t overall exchange factor : \t0.635\n",
-      "\t Z is : \t37251.9195663\n",
-      "\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.1 \\t\"\n",
-    "# For orientation purposes, one can make an estimate of the number of tubes required in the radiant section by assuming avg flux is 12000 Btu/(hr)*(ft**2)\n",
-    "# from Fig.19.14 it can be seen that with a tube temperature of 800DegF, an exit-gas temperature of l730DegF will be required to effect such a flux.\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "Q=50000000; # Btu/hr\n",
-    "QF=(Q/0.75); # efficiency of tank is 75%\n",
-    "print\"\\t heat liberated by the fuel : Btu/hr \\t\",QF\n",
-    "w1=(QF/17130); # heating value of fuel is 17130Btu/lb\n",
-    "print\"\\t fuel quantity : lb/hr \\t\",w1\n",
-    "w2=(w1*17.44); # lb of fuel fired with 17.44lb of air\n",
-    "print\"\\t air required : lb/hr \\t\",w2\n",
-    "w3=(w1*0.3); # 0.3 lb of air is used for atomizing lb of fuel\n",
-    "print\"\\t steam for atomizing : lb/hr \\t\",w3\n",
-    "QA=(w2*82); # heating value at 400F is 82Btu/lb\n",
-    "print\"\\t QA is : Btu/hr \\t\",QA\n",
-    "print\"\\t QS is negligible \\t\"\n",
-    "QW=(0.02*QF);\n",
-    "print\"\\t QW is : Btu/hr \\t\",QW\n",
-    "Qnet=(QF+QA-QW);\n",
-    "print\"\\t Qnet is : Btu/hr \\t\",Qnet\n",
-    "#Heat out m gases at 1730DegF, 25 per cent excess air, 476 Btu/lb of flue gas\n",
-    "QG=(476*(w1+w2+w3));\n",
-    "print\"\\t QG is : Btu/hr \\t\",QG\n",
-    "Q1=(Qnet-QG);\n",
-    "print\"\\t Q1 is : Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "A=(3.14*38.5*(5./12.)); # area of tube\n",
-    "print\"\\t area of tube is : ft**2 \\t\",A\n",
-    "Nt=(Q1/(12000*A)); # 12000 is avg flux\n",
-    "print\"\\t estimated number of tubes : \\t\",Nt\n",
-    "# The layout of the cross section of the furnace may be as shown m Fig. 19.16.\n",
-    "# center to center distance is 8(1/2)in\n",
-    "Acp=(8.5*38.5/12);\n",
-    "print\"\\t cold plane surface per tube : ft**2 \\t\",Acp # calculation mistake in book\n",
-    "a=0.937; # a=alpha, from fig 19.11 as Ratio of center-to-center/OD is 1.7\n",
-    "Acp1=(Acp*a);\n",
-    "print\"\\t Acp1 is : ft**2 \\t\",Acp1\n",
-    "Acpt=(Acp1*Nt);\n",
-    "print\"\\t total cold plane surface is : ft**2 \\t\",Acpt\n",
-    "A1=(2*20.46*14.92); # from fig 19.16\n",
-    "print\"\\t surface of end walls : ft**2 \\t\",A1\n",
-    "A2=(38.5*14.92); # from fig 19.16\n",
-    "print\"\\t surface of side wall : ft**2 \\t\",A2\n",
-    "A3=(38.5*9.79); # from fig 19.16\n",
-    "print\"\\t surface of bridge walls : ft**2 \\t\",A3\n",
-    "A4=(2*20.46*38.5); # from fig 19.16\n",
-    "print\"\\t surface of floor and arch : ft**2 \\t\",A4\n",
-    "AT=(A1+A2+A3+A4);\n",
-    "print\"\\t AT is : ft**2 \\t\",AT\n",
-    "AR=(AT-Acpt);\n",
-    "print\"\\t AR is : ft**2 \\t\",AR\n",
-    "Ar=(AR/Acpt);\n",
-    "print\"\\t ratio of areas is : \\t\",Ar\n",
-    "print\"\\t dimension ratio is 3:2:1 \\t\"\n",
-    "L=((2/3)*(38.5*20.46*14.92)**(1/3));\n",
-    "print\"\\t length is : ft \\t\",L\n",
-    "print\"\\t gas emissivity \\t\"\n",
-    "# From the analysis of the fuel, the steam quantity, and the assumption that the humidity of the air is 50 per cent of saturation at 60F, the partial pressures of CO2 and H2O in the combustion gases with 25 per cent excess air are\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248\n",
-    "pCO2L=1.63; # pCO2L=(pCO2*L)\n",
-    "pH2OL=1.87;\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P : \\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is : \\t\",Pt\n",
-    "# %correction estimated to be 8%\n",
-    "eG=(((6500+14500)-(650+1950))/(39000-4400))*((100-8)/100); # values from fig 19.12 and 19.13, eq 19.5\n",
-    "print\"\\t eG is : \\t\",eG\n",
-    "f=0.635; # from fig 19.15 as (AR/Acpt)=1.09 and eG=0.496\n",
-    "print\"\\t overall exchange factor : \\t\",f\n",
-    "Z=(Q1/(Acpt*f));\n",
-    "print\"\\t Z is : \\t\",round(Z)\n",
-    "print\"\\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.2 pgno:705"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.2 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\t Q is :  Btu/hr  24867609.5833\n",
-      "\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.2 \\n\"\n",
-    "QF=50000000.;\n",
-    "G=22.36;\n",
-    "Acpt=1500.;\n",
-    "print\"\\t approxiate values are mentioned in the book \"\n",
-    "Q=(QF/(1+(G/4200)*(QF/Acpt)**(1/2)))/2; # eq 19.15\n",
-    "print\"\\t Q is :  Btu/hr \",Q\n",
-    "print\"\\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \\n\"\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.3 pgno:707"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.3 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\n",
-      "\t a1 is :   1.63\n",
-      "\t a2 is :  2.2331\n",
-      "\t Qr2 is :   0.309300671182\n",
-      "\t ratio of heats is :   1.22092370204\n",
-      "\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.3 \\n\"\n",
-    "Qr=1.5; # Qr=(QF2/QF1)\n",
-    "Cr=1.5; # Cr=(CR2/CR1)\n",
-    "Gr=140/125; # Gr=(G2/G1)\n",
-    "Qr1=0.38; # Qr1=(Q1/QF1)\n",
-    "print\"\\t approxiate values are mentioned in the book \\n\"\n",
-    "a1=1.63; # a1=(G1*(CR1/27)^(1/2)), from eq 19.17\n",
-    "print\"\\t a1 is :  \",a1\n",
-    "a2=1.37*(a1); # a2=(G2*(CR2/27)^(1/2))\n",
-    "print\"\\t a2 is : \",a2\n",
-    "Qr2=(1/(1+a2)); # Qr2=(Q2/QF2),from eq 19.15\n",
-    "print\"\\t Qr2 is :  \",Qr2\n",
-    "Q21=(Qr2/Qr1)*(Qr); # Q21=(Q2/Q1)\n",
-    "print\"\\t ratio of heats is :  \",round(Q21,2)\n",
-    "print\"\\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \\n\"\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.4 pgno:708"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.4 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t L is :  ft \t0.565\n",
-      "\t pH2OL is :  atm-ft \t0.070512\n",
-      "\t pCO2L is :  atm-ft \t0.061246\n",
-      "\t qTG is :  \t2750\n",
-      "\t qTG is :  \t325\n",
-      "\t q is :  \t2182.5\n",
-      "\t percentage correction at P : %.3f \t0.464837049743\n",
-      "\t Pt is :  \t0.131758\n",
-      "\t q1 is :  \t2138.85\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \t2.51629411765\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.4 \\t\"\n",
-    "eS=0.9; # assumed\n",
-    "TG=1500;\n",
-    "TS=650;\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "L=(0.4*8.5)-(0.567*5);  # table 19.1\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "pH2OL=0.1248*L;\n",
-    "pCO2L=0.1084*L;\n",
-    "print\"\\t pH2OL is :  atm-ft \\t\",pH2OL\n",
-    "print\"\\t pCO2L is :  atm-ft \\t\",pCO2L\n",
-    "qH2O=1050; # at TG, from fig 19.12 ana 19.13\n",
-    "qCO2=1700; # at TG, from fig 19.12 ana 19.13\n",
-    "qTG=(qH2O+qCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTG\n",
-    "qsH2O=165; # at TS, from fig 19.12 ana 19.13\n",
-    "qsCO2=160; # at TS, from fig 19.12 ana 19.13\n",
-    "qTS=(qsH2O+qsCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTS\n",
-    "q=(0.9*(qTG-qTS)); # q=(QRC/A)\n",
-    "print\"\\t q is :  \\t\",q\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P :\\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is :  \\t\",Pt\n",
-    "# %correction estimated to be 2%\n",
-    "q1=(q*0.98); # # q1=(QRC/A)\n",
-    "print\"\\t q1 is :  \\t\",q1\n",
-    "hr=(q1/(TG-TS));\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \\t\",round(hr,2)\n",
-    "#end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.5 pgno:709"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.5 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t a is :  ft**2/ft \t3.5\n",
-      "\t AR is :  ft**2/ft \t9.6\n",
-      "\t ratio of two areas is :  \t2.74285714286\n",
-      "\t q1 is :  Btu/(hr)*(ft**2) \t10582\n",
-      "\t q2 is :  Btu/(hr)*(ft**2) \t5925.92\n",
-      "\t convection rate basis \t\n",
-      "\t q3 is :  Btu/(hr)*(ft**2) \t808.8\n",
-      "\t qt is :  Btu/(hr)*(ft**2) \t6734.72\n",
-      "\t required a is :  ft**2 \t74.2421362729\n",
-      "\t length required is :  ft \t19.2\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.5 \\t\"\n",
-    "Q=500000;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "a=(3.5+(3.14*4*(120/360)))/(1); # a=(alpha*Acp) from fig 19.17\n",
-    "AR=(3+3.6+3);\n",
-    "print\"\\t a is :  ft**2/ft \\t\",a\n",
-    "print\"\\t AR is :  ft**2/ft \\t\",AR\n",
-    "# Arbitrarily neglecting end wa.lls and also .the side wall refractory over 3'0\" above the floor\n",
-    "R=(AR/a);\n",
-    "print\"\\t ratio of two areas is :  \\t\",R\n",
-    "eG=0.265;\n",
-    "TG=1174; # F\n",
-    "TS=500; # F\n",
-    "f=0.56; # from fig 19.15 as (AR/Acpt)=2.49 and eG=0.265\n",
-    "q=15300; # at TG and TS,q=(Q/(a*f))\n",
-    "# However, the convection coefficient is small, 1.0 +or- Btu/(hr)(ft2)(\"F), and AR/a is not 2.0 as in the assumptions for the Lobo and Evans equation.\n",
-    "q1=(q)-(7*(TG-TS)); # q1=(Q/(a*f))\n",
-    "print\"\\t q1 is :  Btu/(hr)*(ft**2) \\t\",q1\n",
-    "q2=(q1*f); # q2=(Q/(a))\n",
-    "print\"\\t q2 is :  Btu/(hr)*(ft**2) \\t\",q2\n",
-    "print\"\\t convection rate basis \\t\"\n",
-    "q3=(1*(TG-TS)*(4.2/a)); # q2=(Q/(a))\n",
-    "print\"\\t q3 is :  Btu/(hr)*(ft**2) \\t\",q3 # calculation mistake in book\n",
-    "qt=(q2+q3); # qt=(Q/(a))\n",
-    "print\"\\t qt is :  Btu/(hr)*(ft**2) \\t\",qt\n",
-    "ar=(Q/qt);\n",
-    "print\"\\t required a is :  ft**2 \\t\",ar\n",
-    "L=(ar/a)-2;\n",
-    "print\"\\t length required is :  ft \\t\",round(L,1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": [
-    "x"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_1.ipynb
deleted file mode 100755
index 73bc1303..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_1.ipynb
+++ /dev/null
@@ -1,390 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 19: Furnace Calculations"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.1 pgno:702 "
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.1 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t heat liberated by the fuel : Btu/hr \t66666666.6667\n",
-      "\t fuel quantity : lb/hr \t3891.8077447\n",
-      "\t air required : lb/hr \t67873.1270675\n",
-      "\t steam for atomizing : lb/hr \t1167.54232341\n",
-      "\t QA is : Btu/hr \t5565596.41954\n",
-      "\t QS is negligible \t\n",
-      "\t QW is : Btu/hr \t1333333.33333\n",
-      "\t Qnet is : Btu/hr \t70898929.7529\n",
-      "\t QG is : Btu/hr \t34715859.1166\n",
-      "\t Q1 is : Btu/hr \t36183070.6363\n",
-      "\t area of tube is : ft**2 \t50.3708333333\n",
-      "\t estimated number of tubes : \t59.8611475495\n",
-      "\t cold plane surface per tube : ft**2 \t27.2708333333\n",
-      "\t Acp1 is : ft**2 \t25.5527708333\n",
-      "\t total cold plane surface is : ft**2 \t1529.61818515\n",
-      "\t surface of end walls : ft**2 \t610.5264\n",
-      "\t surface of side wall : ft**2 \t574.42\n",
-      "\t surface of bridge walls : ft**2 \t376.915\n",
-      "\t surface of floor and arch : ft**2 \t1575.42\n",
-      "\t AT is : ft**2 \t3137.2814\n",
-      "\t AR is : ft**2 \t1607.66321485\n",
-      "\t ratio of areas is : \t1.05102255612\n",
-      "\t dimension ratio is 3:2:1 \t\n",
-      "\t length is : ft \t0.0\n",
-      "\t gas emissivity \t\n",
-      "\t percentage correction at P : \t0.464837049743\n",
-      "\t Pt is : \t3.5\n",
-      "\t eG is : \t0\n",
-      "\t overall exchange factor : \t0.635\n",
-      "\t Z is : \t37251.9195663\n",
-      "\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.1 \\t\"\n",
-    "# For orientation purposes, one can make an estimate of the number of tubes required in the radiant section by assuming avg flux is 12000 Btu/(hr)*(ft**2)\n",
-    "# from Fig.19.14 it can be seen that with a tube temperature of 800DegF, an exit-gas temperature of l730DegF will be required to effect such a flux.\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "Q=50000000; # Btu/hr\n",
-    "QF=(Q/0.75); # efficiency of tank is 75%\n",
-    "print\"\\t heat liberated by the fuel : Btu/hr \\t\",QF\n",
-    "w1=(QF/17130); # heating value of fuel is 17130Btu/lb\n",
-    "print\"\\t fuel quantity : lb/hr \\t\",w1\n",
-    "w2=(w1*17.44); # lb of fuel fired with 17.44lb of air\n",
-    "print\"\\t air required : lb/hr \\t\",w2\n",
-    "w3=(w1*0.3); # 0.3 lb of air is used for atomizing lb of fuel\n",
-    "print\"\\t steam for atomizing : lb/hr \\t\",w3\n",
-    "QA=(w2*82); # heating value at 400F is 82Btu/lb\n",
-    "print\"\\t QA is : Btu/hr \\t\",QA\n",
-    "print\"\\t QS is negligible \\t\"\n",
-    "QW=(0.02*QF);\n",
-    "print\"\\t QW is : Btu/hr \\t\",QW\n",
-    "Qnet=(QF+QA-QW);\n",
-    "print\"\\t Qnet is : Btu/hr \\t\",Qnet\n",
-    "#Heat out m gases at 1730DegF, 25 per cent excess air, 476 Btu/lb of flue gas\n",
-    "QG=(476*(w1+w2+w3));\n",
-    "print\"\\t QG is : Btu/hr \\t\",QG\n",
-    "Q1=(Qnet-QG);\n",
-    "print\"\\t Q1 is : Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "A=(3.14*38.5*(5./12.)); # area of tube\n",
-    "print\"\\t area of tube is : ft**2 \\t\",A\n",
-    "Nt=(Q1/(12000*A)); # 12000 is avg flux\n",
-    "print\"\\t estimated number of tubes : \\t\",Nt\n",
-    "# The layout of the cross section of the furnace may be as shown m Fig. 19.16.\n",
-    "# center to center distance is 8(1/2)in\n",
-    "Acp=(8.5*38.5/12);\n",
-    "print\"\\t cold plane surface per tube : ft**2 \\t\",Acp # calculation mistake in book\n",
-    "a=0.937; # a=alpha, from fig 19.11 as Ratio of center-to-center/OD is 1.7\n",
-    "Acp1=(Acp*a);\n",
-    "print\"\\t Acp1 is : ft**2 \\t\",Acp1\n",
-    "Acpt=(Acp1*Nt);\n",
-    "print\"\\t total cold plane surface is : ft**2 \\t\",Acpt\n",
-    "A1=(2*20.46*14.92); # from fig 19.16\n",
-    "print\"\\t surface of end walls : ft**2 \\t\",A1\n",
-    "A2=(38.5*14.92); # from fig 19.16\n",
-    "print\"\\t surface of side wall : ft**2 \\t\",A2\n",
-    "A3=(38.5*9.79); # from fig 19.16\n",
-    "print\"\\t surface of bridge walls : ft**2 \\t\",A3\n",
-    "A4=(2*20.46*38.5); # from fig 19.16\n",
-    "print\"\\t surface of floor and arch : ft**2 \\t\",A4\n",
-    "AT=(A1+A2+A3+A4);\n",
-    "print\"\\t AT is : ft**2 \\t\",AT\n",
-    "AR=(AT-Acpt);\n",
-    "print\"\\t AR is : ft**2 \\t\",AR\n",
-    "Ar=(AR/Acpt);\n",
-    "print\"\\t ratio of areas is : \\t\",Ar\n",
-    "print\"\\t dimension ratio is 3:2:1 \\t\"\n",
-    "L=((2/3)*(38.5*20.46*14.92)**(1/3));\n",
-    "print\"\\t length is : ft \\t\",L\n",
-    "print\"\\t gas emissivity \\t\"\n",
-    "# From the analysis of the fuel, the steam quantity, and the assumption that the humidity of the air is 50 per cent of saturation at 60F, the partial pressures of CO2 and H2O in the combustion gases with 25 per cent excess air are\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248\n",
-    "pCO2L=1.63; # pCO2L=(pCO2*L)\n",
-    "pH2OL=1.87;\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P : \\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is : \\t\",Pt\n",
-    "# %correction estimated to be 8%\n",
-    "eG=(((6500+14500)-(650+1950))/(39000-4400))*((100-8)/100); # values from fig 19.12 and 19.13, eq 19.5\n",
-    "print\"\\t eG is : \\t\",eG\n",
-    "f=0.635; # from fig 19.15 as (AR/Acpt)=1.09 and eG=0.496\n",
-    "print\"\\t overall exchange factor : \\t\",f\n",
-    "Z=(Q1/(Acpt*f));\n",
-    "print\"\\t Z is : \\t\",round(Z)\n",
-    "print\"\\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.2 pgno:705"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.2 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\t Q is :  Btu/hr  24867609.5833\n",
-      "\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.2 \\n\"\n",
-    "QF=50000000.;\n",
-    "G=22.36;\n",
-    "Acpt=1500.;\n",
-    "print\"\\t approxiate values are mentioned in the book \"\n",
-    "Q=(QF/(1+(G/4200)*(QF/Acpt)**(1/2)))/2; # eq 19.15\n",
-    "print\"\\t Q is :  Btu/hr \",Q\n",
-    "print\"\\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \\n\"\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.3 pgno:707"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.3 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\n",
-      "\t a1 is :   1.63\n",
-      "\t a2 is :  2.2331\n",
-      "\t Qr2 is :   0.309300671182\n",
-      "\t ratio of heats is :   1.22092370204\n",
-      "\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.3 \\n\"\n",
-    "Qr=1.5; # Qr=(QF2/QF1)\n",
-    "Cr=1.5; # Cr=(CR2/CR1)\n",
-    "Gr=140/125; # Gr=(G2/G1)\n",
-    "Qr1=0.38; # Qr1=(Q1/QF1)\n",
-    "print\"\\t approxiate values are mentioned in the book \\n\"\n",
-    "a1=1.63; # a1=(G1*(CR1/27)^(1/2)), from eq 19.17\n",
-    "print\"\\t a1 is :  \",a1\n",
-    "a2=1.37*(a1); # a2=(G2*(CR2/27)^(1/2))\n",
-    "print\"\\t a2 is : \",a2\n",
-    "Qr2=(1/(1+a2)); # Qr2=(Q2/QF2),from eq 19.15\n",
-    "print\"\\t Qr2 is :  \",Qr2\n",
-    "Q21=(Qr2/Qr1)*(Qr); # Q21=(Q2/Q1)\n",
-    "print\"\\t ratio of heats is :  \",round(Q21,2)\n",
-    "print\"\\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \\n\"\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.4 pgno:708"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.4 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t L is :  ft \t0.565\n",
-      "\t pH2OL is :  atm-ft \t0.070512\n",
-      "\t pCO2L is :  atm-ft \t0.061246\n",
-      "\t qTG is :  \t2750\n",
-      "\t qTG is :  \t325\n",
-      "\t q is :  \t2182.5\n",
-      "\t percentage correction at P : %.3f \t0.464837049743\n",
-      "\t Pt is :  \t0.131758\n",
-      "\t q1 is :  \t2138.85\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \t2.51629411765\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.4 \\t\"\n",
-    "eS=0.9; # assumed\n",
-    "TG=1500;\n",
-    "TS=650;\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "L=(0.4*8.5)-(0.567*5);  # table 19.1\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "pH2OL=0.1248*L;\n",
-    "pCO2L=0.1084*L;\n",
-    "print\"\\t pH2OL is :  atm-ft \\t\",pH2OL\n",
-    "print\"\\t pCO2L is :  atm-ft \\t\",pCO2L\n",
-    "qH2O=1050; # at TG, from fig 19.12 ana 19.13\n",
-    "qCO2=1700; # at TG, from fig 19.12 ana 19.13\n",
-    "qTG=(qH2O+qCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTG\n",
-    "qsH2O=165; # at TS, from fig 19.12 ana 19.13\n",
-    "qsCO2=160; # at TS, from fig 19.12 ana 19.13\n",
-    "qTS=(qsH2O+qsCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTS\n",
-    "q=(0.9*(qTG-qTS)); # q=(QRC/A)\n",
-    "print\"\\t q is :  \\t\",q\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P :\\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is :  \\t\",Pt\n",
-    "# %correction estimated to be 2%\n",
-    "q1=(q*0.98); # # q1=(QRC/A)\n",
-    "print\"\\t q1 is :  \\t\",q1\n",
-    "hr=(q1/(TG-TS));\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \\t\",round(hr,2)\n",
-    "#end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.5 pgno:709"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.5 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t a is :  ft**2/ft \t3.5\n",
-      "\t AR is :  ft**2/ft \t9.6\n",
-      "\t ratio of two areas is :  \t2.74285714286\n",
-      "\t q1 is :  Btu/(hr)*(ft**2) \t10582\n",
-      "\t q2 is :  Btu/(hr)*(ft**2) \t5925.92\n",
-      "\t convection rate basis \t\n",
-      "\t q3 is :  Btu/(hr)*(ft**2) \t808.8\n",
-      "\t qt is :  Btu/(hr)*(ft**2) \t6734.72\n",
-      "\t required a is :  ft**2 \t74.2421362729\n",
-      "\t length required is :  ft \t19.2\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.5 \\t\"\n",
-    "Q=500000;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "a=(3.5+(3.14*4*(120/360)))/(1); # a=(alpha*Acp) from fig 19.17\n",
-    "AR=(3+3.6+3);\n",
-    "print\"\\t a is :  ft**2/ft \\t\",a\n",
-    "print\"\\t AR is :  ft**2/ft \\t\",AR\n",
-    "# Arbitrarily neglecting end wa.lls and also .the side wall refractory over 3'0\" above the floor\n",
-    "R=(AR/a);\n",
-    "print\"\\t ratio of two areas is :  \\t\",R\n",
-    "eG=0.265;\n",
-    "TG=1174; # F\n",
-    "TS=500; # F\n",
-    "f=0.56; # from fig 19.15 as (AR/Acpt)=2.49 and eG=0.265\n",
-    "q=15300; # at TG and TS,q=(Q/(a*f))\n",
-    "# However, the convection coefficient is small, 1.0 +or- Btu/(hr)(ft2)(\"F), and AR/a is not 2.0 as in the assumptions for the Lobo and Evans equation.\n",
-    "q1=(q)-(7*(TG-TS)); # q1=(Q/(a*f))\n",
-    "print\"\\t q1 is :  Btu/(hr)*(ft**2) \\t\",q1\n",
-    "q2=(q1*f); # q2=(Q/(a))\n",
-    "print\"\\t q2 is :  Btu/(hr)*(ft**2) \\t\",q2\n",
-    "print\"\\t convection rate basis \\t\"\n",
-    "q3=(1*(TG-TS)*(4.2/a)); # q2=(Q/(a))\n",
-    "print\"\\t q3 is :  Btu/(hr)*(ft**2) \\t\",q3 # calculation mistake in book\n",
-    "qt=(q2+q3); # qt=(Q/(a))\n",
-    "print\"\\t qt is :  Btu/(hr)*(ft**2) \\t\",qt\n",
-    "ar=(Q/qt);\n",
-    "print\"\\t required a is :  ft**2 \\t\",ar\n",
-    "L=(ar/a)-2;\n",
-    "print\"\\t length required is :  ft \\t\",round(L,1)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_2.ipynb
deleted file mode 100755
index 73bc1303..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_2.ipynb
+++ /dev/null
@@ -1,390 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 19: Furnace Calculations"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.1 pgno:702 "
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.1 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t heat liberated by the fuel : Btu/hr \t66666666.6667\n",
-      "\t fuel quantity : lb/hr \t3891.8077447\n",
-      "\t air required : lb/hr \t67873.1270675\n",
-      "\t steam for atomizing : lb/hr \t1167.54232341\n",
-      "\t QA is : Btu/hr \t5565596.41954\n",
-      "\t QS is negligible \t\n",
-      "\t QW is : Btu/hr \t1333333.33333\n",
-      "\t Qnet is : Btu/hr \t70898929.7529\n",
-      "\t QG is : Btu/hr \t34715859.1166\n",
-      "\t Q1 is : Btu/hr \t36183070.6363\n",
-      "\t area of tube is : ft**2 \t50.3708333333\n",
-      "\t estimated number of tubes : \t59.8611475495\n",
-      "\t cold plane surface per tube : ft**2 \t27.2708333333\n",
-      "\t Acp1 is : ft**2 \t25.5527708333\n",
-      "\t total cold plane surface is : ft**2 \t1529.61818515\n",
-      "\t surface of end walls : ft**2 \t610.5264\n",
-      "\t surface of side wall : ft**2 \t574.42\n",
-      "\t surface of bridge walls : ft**2 \t376.915\n",
-      "\t surface of floor and arch : ft**2 \t1575.42\n",
-      "\t AT is : ft**2 \t3137.2814\n",
-      "\t AR is : ft**2 \t1607.66321485\n",
-      "\t ratio of areas is : \t1.05102255612\n",
-      "\t dimension ratio is 3:2:1 \t\n",
-      "\t length is : ft \t0.0\n",
-      "\t gas emissivity \t\n",
-      "\t percentage correction at P : \t0.464837049743\n",
-      "\t Pt is : \t3.5\n",
-      "\t eG is : \t0\n",
-      "\t overall exchange factor : \t0.635\n",
-      "\t Z is : \t37251.9195663\n",
-      "\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.1 \\t\"\n",
-    "# For orientation purposes, one can make an estimate of the number of tubes required in the radiant section by assuming avg flux is 12000 Btu/(hr)*(ft**2)\n",
-    "# from Fig.19.14 it can be seen that with a tube temperature of 800DegF, an exit-gas temperature of l730DegF will be required to effect such a flux.\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "Q=50000000; # Btu/hr\n",
-    "QF=(Q/0.75); # efficiency of tank is 75%\n",
-    "print\"\\t heat liberated by the fuel : Btu/hr \\t\",QF\n",
-    "w1=(QF/17130); # heating value of fuel is 17130Btu/lb\n",
-    "print\"\\t fuel quantity : lb/hr \\t\",w1\n",
-    "w2=(w1*17.44); # lb of fuel fired with 17.44lb of air\n",
-    "print\"\\t air required : lb/hr \\t\",w2\n",
-    "w3=(w1*0.3); # 0.3 lb of air is used for atomizing lb of fuel\n",
-    "print\"\\t steam for atomizing : lb/hr \\t\",w3\n",
-    "QA=(w2*82); # heating value at 400F is 82Btu/lb\n",
-    "print\"\\t QA is : Btu/hr \\t\",QA\n",
-    "print\"\\t QS is negligible \\t\"\n",
-    "QW=(0.02*QF);\n",
-    "print\"\\t QW is : Btu/hr \\t\",QW\n",
-    "Qnet=(QF+QA-QW);\n",
-    "print\"\\t Qnet is : Btu/hr \\t\",Qnet\n",
-    "#Heat out m gases at 1730DegF, 25 per cent excess air, 476 Btu/lb of flue gas\n",
-    "QG=(476*(w1+w2+w3));\n",
-    "print\"\\t QG is : Btu/hr \\t\",QG\n",
-    "Q1=(Qnet-QG);\n",
-    "print\"\\t Q1 is : Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "A=(3.14*38.5*(5./12.)); # area of tube\n",
-    "print\"\\t area of tube is : ft**2 \\t\",A\n",
-    "Nt=(Q1/(12000*A)); # 12000 is avg flux\n",
-    "print\"\\t estimated number of tubes : \\t\",Nt\n",
-    "# The layout of the cross section of the furnace may be as shown m Fig. 19.16.\n",
-    "# center to center distance is 8(1/2)in\n",
-    "Acp=(8.5*38.5/12);\n",
-    "print\"\\t cold plane surface per tube : ft**2 \\t\",Acp # calculation mistake in book\n",
-    "a=0.937; # a=alpha, from fig 19.11 as Ratio of center-to-center/OD is 1.7\n",
-    "Acp1=(Acp*a);\n",
-    "print\"\\t Acp1 is : ft**2 \\t\",Acp1\n",
-    "Acpt=(Acp1*Nt);\n",
-    "print\"\\t total cold plane surface is : ft**2 \\t\",Acpt\n",
-    "A1=(2*20.46*14.92); # from fig 19.16\n",
-    "print\"\\t surface of end walls : ft**2 \\t\",A1\n",
-    "A2=(38.5*14.92); # from fig 19.16\n",
-    "print\"\\t surface of side wall : ft**2 \\t\",A2\n",
-    "A3=(38.5*9.79); # from fig 19.16\n",
-    "print\"\\t surface of bridge walls : ft**2 \\t\",A3\n",
-    "A4=(2*20.46*38.5); # from fig 19.16\n",
-    "print\"\\t surface of floor and arch : ft**2 \\t\",A4\n",
-    "AT=(A1+A2+A3+A4);\n",
-    "print\"\\t AT is : ft**2 \\t\",AT\n",
-    "AR=(AT-Acpt);\n",
-    "print\"\\t AR is : ft**2 \\t\",AR\n",
-    "Ar=(AR/Acpt);\n",
-    "print\"\\t ratio of areas is : \\t\",Ar\n",
-    "print\"\\t dimension ratio is 3:2:1 \\t\"\n",
-    "L=((2/3)*(38.5*20.46*14.92)**(1/3));\n",
-    "print\"\\t length is : ft \\t\",L\n",
-    "print\"\\t gas emissivity \\t\"\n",
-    "# From the analysis of the fuel, the steam quantity, and the assumption that the humidity of the air is 50 per cent of saturation at 60F, the partial pressures of CO2 and H2O in the combustion gases with 25 per cent excess air are\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248\n",
-    "pCO2L=1.63; # pCO2L=(pCO2*L)\n",
-    "pH2OL=1.87;\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P : \\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is : \\t\",Pt\n",
-    "# %correction estimated to be 8%\n",
-    "eG=(((6500+14500)-(650+1950))/(39000-4400))*((100-8)/100); # values from fig 19.12 and 19.13, eq 19.5\n",
-    "print\"\\t eG is : \\t\",eG\n",
-    "f=0.635; # from fig 19.15 as (AR/Acpt)=1.09 and eG=0.496\n",
-    "print\"\\t overall exchange factor : \\t\",f\n",
-    "Z=(Q1/(Acpt*f));\n",
-    "print\"\\t Z is : \\t\",round(Z)\n",
-    "print\"\\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.2 pgno:705"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.2 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\t Q is :  Btu/hr  24867609.5833\n",
-      "\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.2 \\n\"\n",
-    "QF=50000000.;\n",
-    "G=22.36;\n",
-    "Acpt=1500.;\n",
-    "print\"\\t approxiate values are mentioned in the book \"\n",
-    "Q=(QF/(1+(G/4200)*(QF/Acpt)**(1/2)))/2; # eq 19.15\n",
-    "print\"\\t Q is :  Btu/hr \",Q\n",
-    "print\"\\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \\n\"\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.3 pgno:707"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.3 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\n",
-      "\t a1 is :   1.63\n",
-      "\t a2 is :  2.2331\n",
-      "\t Qr2 is :   0.309300671182\n",
-      "\t ratio of heats is :   1.22092370204\n",
-      "\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.3 \\n\"\n",
-    "Qr=1.5; # Qr=(QF2/QF1)\n",
-    "Cr=1.5; # Cr=(CR2/CR1)\n",
-    "Gr=140/125; # Gr=(G2/G1)\n",
-    "Qr1=0.38; # Qr1=(Q1/QF1)\n",
-    "print\"\\t approxiate values are mentioned in the book \\n\"\n",
-    "a1=1.63; # a1=(G1*(CR1/27)^(1/2)), from eq 19.17\n",
-    "print\"\\t a1 is :  \",a1\n",
-    "a2=1.37*(a1); # a2=(G2*(CR2/27)^(1/2))\n",
-    "print\"\\t a2 is : \",a2\n",
-    "Qr2=(1/(1+a2)); # Qr2=(Q2/QF2),from eq 19.15\n",
-    "print\"\\t Qr2 is :  \",Qr2\n",
-    "Q21=(Qr2/Qr1)*(Qr); # Q21=(Q2/Q1)\n",
-    "print\"\\t ratio of heats is :  \",round(Q21,2)\n",
-    "print\"\\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \\n\"\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.4 pgno:708"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.4 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t L is :  ft \t0.565\n",
-      "\t pH2OL is :  atm-ft \t0.070512\n",
-      "\t pCO2L is :  atm-ft \t0.061246\n",
-      "\t qTG is :  \t2750\n",
-      "\t qTG is :  \t325\n",
-      "\t q is :  \t2182.5\n",
-      "\t percentage correction at P : %.3f \t0.464837049743\n",
-      "\t Pt is :  \t0.131758\n",
-      "\t q1 is :  \t2138.85\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \t2.51629411765\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.4 \\t\"\n",
-    "eS=0.9; # assumed\n",
-    "TG=1500;\n",
-    "TS=650;\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "L=(0.4*8.5)-(0.567*5);  # table 19.1\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "pH2OL=0.1248*L;\n",
-    "pCO2L=0.1084*L;\n",
-    "print\"\\t pH2OL is :  atm-ft \\t\",pH2OL\n",
-    "print\"\\t pCO2L is :  atm-ft \\t\",pCO2L\n",
-    "qH2O=1050; # at TG, from fig 19.12 ana 19.13\n",
-    "qCO2=1700; # at TG, from fig 19.12 ana 19.13\n",
-    "qTG=(qH2O+qCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTG\n",
-    "qsH2O=165; # at TS, from fig 19.12 ana 19.13\n",
-    "qsCO2=160; # at TS, from fig 19.12 ana 19.13\n",
-    "qTS=(qsH2O+qsCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTS\n",
-    "q=(0.9*(qTG-qTS)); # q=(QRC/A)\n",
-    "print\"\\t q is :  \\t\",q\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P :\\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is :  \\t\",Pt\n",
-    "# %correction estimated to be 2%\n",
-    "q1=(q*0.98); # # q1=(QRC/A)\n",
-    "print\"\\t q1 is :  \\t\",q1\n",
-    "hr=(q1/(TG-TS));\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \\t\",round(hr,2)\n",
-    "#end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.5 pgno:709"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.5 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t a is :  ft**2/ft \t3.5\n",
-      "\t AR is :  ft**2/ft \t9.6\n",
-      "\t ratio of two areas is :  \t2.74285714286\n",
-      "\t q1 is :  Btu/(hr)*(ft**2) \t10582\n",
-      "\t q2 is :  Btu/(hr)*(ft**2) \t5925.92\n",
-      "\t convection rate basis \t\n",
-      "\t q3 is :  Btu/(hr)*(ft**2) \t808.8\n",
-      "\t qt is :  Btu/(hr)*(ft**2) \t6734.72\n",
-      "\t required a is :  ft**2 \t74.2421362729\n",
-      "\t length required is :  ft \t19.2\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.5 \\t\"\n",
-    "Q=500000;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "a=(3.5+(3.14*4*(120/360)))/(1); # a=(alpha*Acp) from fig 19.17\n",
-    "AR=(3+3.6+3);\n",
-    "print\"\\t a is :  ft**2/ft \\t\",a\n",
-    "print\"\\t AR is :  ft**2/ft \\t\",AR\n",
-    "# Arbitrarily neglecting end wa.lls and also .the side wall refractory over 3'0\" above the floor\n",
-    "R=(AR/a);\n",
-    "print\"\\t ratio of two areas is :  \\t\",R\n",
-    "eG=0.265;\n",
-    "TG=1174; # F\n",
-    "TS=500; # F\n",
-    "f=0.56; # from fig 19.15 as (AR/Acpt)=2.49 and eG=0.265\n",
-    "q=15300; # at TG and TS,q=(Q/(a*f))\n",
-    "# However, the convection coefficient is small, 1.0 +or- Btu/(hr)(ft2)(\"F), and AR/a is not 2.0 as in the assumptions for the Lobo and Evans equation.\n",
-    "q1=(q)-(7*(TG-TS)); # q1=(Q/(a*f))\n",
-    "print\"\\t q1 is :  Btu/(hr)*(ft**2) \\t\",q1\n",
-    "q2=(q1*f); # q2=(Q/(a))\n",
-    "print\"\\t q2 is :  Btu/(hr)*(ft**2) \\t\",q2\n",
-    "print\"\\t convection rate basis \\t\"\n",
-    "q3=(1*(TG-TS)*(4.2/a)); # q2=(Q/(a))\n",
-    "print\"\\t q3 is :  Btu/(hr)*(ft**2) \\t\",q3 # calculation mistake in book\n",
-    "qt=(q2+q3); # qt=(Q/(a))\n",
-    "print\"\\t qt is :  Btu/(hr)*(ft**2) \\t\",qt\n",
-    "ar=(Q/qt);\n",
-    "print\"\\t required a is :  ft**2 \\t\",ar\n",
-    "L=(ar/a)-2;\n",
-    "print\"\\t length required is :  ft \\t\",round(L,1)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_3.ipynb
deleted file mode 100755
index 73bc1303..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_19_Furnace_Calculations_3.ipynb
+++ /dev/null
@@ -1,390 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 19: Furnace Calculations"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.1 pgno:702 "
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.1 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t heat liberated by the fuel : Btu/hr \t66666666.6667\n",
-      "\t fuel quantity : lb/hr \t3891.8077447\n",
-      "\t air required : lb/hr \t67873.1270675\n",
-      "\t steam for atomizing : lb/hr \t1167.54232341\n",
-      "\t QA is : Btu/hr \t5565596.41954\n",
-      "\t QS is negligible \t\n",
-      "\t QW is : Btu/hr \t1333333.33333\n",
-      "\t Qnet is : Btu/hr \t70898929.7529\n",
-      "\t QG is : Btu/hr \t34715859.1166\n",
-      "\t Q1 is : Btu/hr \t36183070.6363\n",
-      "\t area of tube is : ft**2 \t50.3708333333\n",
-      "\t estimated number of tubes : \t59.8611475495\n",
-      "\t cold plane surface per tube : ft**2 \t27.2708333333\n",
-      "\t Acp1 is : ft**2 \t25.5527708333\n",
-      "\t total cold plane surface is : ft**2 \t1529.61818515\n",
-      "\t surface of end walls : ft**2 \t610.5264\n",
-      "\t surface of side wall : ft**2 \t574.42\n",
-      "\t surface of bridge walls : ft**2 \t376.915\n",
-      "\t surface of floor and arch : ft**2 \t1575.42\n",
-      "\t AT is : ft**2 \t3137.2814\n",
-      "\t AR is : ft**2 \t1607.66321485\n",
-      "\t ratio of areas is : \t1.05102255612\n",
-      "\t dimension ratio is 3:2:1 \t\n",
-      "\t length is : ft \t0.0\n",
-      "\t gas emissivity \t\n",
-      "\t percentage correction at P : \t0.464837049743\n",
-      "\t Pt is : \t3.5\n",
-      "\t eG is : \t0\n",
-      "\t overall exchange factor : \t0.635\n",
-      "\t Z is : \t37251.9195663\n",
-      "\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.1 \\t\"\n",
-    "# For orientation purposes, one can make an estimate of the number of tubes required in the radiant section by assuming avg flux is 12000 Btu/(hr)*(ft**2)\n",
-    "# from Fig.19.14 it can be seen that with a tube temperature of 800DegF, an exit-gas temperature of l730DegF will be required to effect such a flux.\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "Q=50000000; # Btu/hr\n",
-    "QF=(Q/0.75); # efficiency of tank is 75%\n",
-    "print\"\\t heat liberated by the fuel : Btu/hr \\t\",QF\n",
-    "w1=(QF/17130); # heating value of fuel is 17130Btu/lb\n",
-    "print\"\\t fuel quantity : lb/hr \\t\",w1\n",
-    "w2=(w1*17.44); # lb of fuel fired with 17.44lb of air\n",
-    "print\"\\t air required : lb/hr \\t\",w2\n",
-    "w3=(w1*0.3); # 0.3 lb of air is used for atomizing lb of fuel\n",
-    "print\"\\t steam for atomizing : lb/hr \\t\",w3\n",
-    "QA=(w2*82); # heating value at 400F is 82Btu/lb\n",
-    "print\"\\t QA is : Btu/hr \\t\",QA\n",
-    "print\"\\t QS is negligible \\t\"\n",
-    "QW=(0.02*QF);\n",
-    "print\"\\t QW is : Btu/hr \\t\",QW\n",
-    "Qnet=(QF+QA-QW);\n",
-    "print\"\\t Qnet is : Btu/hr \\t\",Qnet\n",
-    "#Heat out m gases at 1730DegF, 25 per cent excess air, 476 Btu/lb of flue gas\n",
-    "QG=(476*(w1+w2+w3));\n",
-    "print\"\\t QG is : Btu/hr \\t\",QG\n",
-    "Q1=(Qnet-QG);\n",
-    "print\"\\t Q1 is : Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "A=(3.14*38.5*(5./12.)); # area of tube\n",
-    "print\"\\t area of tube is : ft**2 \\t\",A\n",
-    "Nt=(Q1/(12000*A)); # 12000 is avg flux\n",
-    "print\"\\t estimated number of tubes : \\t\",Nt\n",
-    "# The layout of the cross section of the furnace may be as shown m Fig. 19.16.\n",
-    "# center to center distance is 8(1/2)in\n",
-    "Acp=(8.5*38.5/12);\n",
-    "print\"\\t cold plane surface per tube : ft**2 \\t\",Acp # calculation mistake in book\n",
-    "a=0.937; # a=alpha, from fig 19.11 as Ratio of center-to-center/OD is 1.7\n",
-    "Acp1=(Acp*a);\n",
-    "print\"\\t Acp1 is : ft**2 \\t\",Acp1\n",
-    "Acpt=(Acp1*Nt);\n",
-    "print\"\\t total cold plane surface is : ft**2 \\t\",Acpt\n",
-    "A1=(2*20.46*14.92); # from fig 19.16\n",
-    "print\"\\t surface of end walls : ft**2 \\t\",A1\n",
-    "A2=(38.5*14.92); # from fig 19.16\n",
-    "print\"\\t surface of side wall : ft**2 \\t\",A2\n",
-    "A3=(38.5*9.79); # from fig 19.16\n",
-    "print\"\\t surface of bridge walls : ft**2 \\t\",A3\n",
-    "A4=(2*20.46*38.5); # from fig 19.16\n",
-    "print\"\\t surface of floor and arch : ft**2 \\t\",A4\n",
-    "AT=(A1+A2+A3+A4);\n",
-    "print\"\\t AT is : ft**2 \\t\",AT\n",
-    "AR=(AT-Acpt);\n",
-    "print\"\\t AR is : ft**2 \\t\",AR\n",
-    "Ar=(AR/Acpt);\n",
-    "print\"\\t ratio of areas is : \\t\",Ar\n",
-    "print\"\\t dimension ratio is 3:2:1 \\t\"\n",
-    "L=((2/3)*(38.5*20.46*14.92)**(1/3));\n",
-    "print\"\\t length is : ft \\t\",L\n",
-    "print\"\\t gas emissivity \\t\"\n",
-    "# From the analysis of the fuel, the steam quantity, and the assumption that the humidity of the air is 50 per cent of saturation at 60F, the partial pressures of CO2 and H2O in the combustion gases with 25 per cent excess air are\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248\n",
-    "pCO2L=1.63; # pCO2L=(pCO2*L)\n",
-    "pH2OL=1.87;\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P : \\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is : \\t\",Pt\n",
-    "# %correction estimated to be 8%\n",
-    "eG=(((6500+14500)-(650+1950))/(39000-4400))*((100-8)/100); # values from fig 19.12 and 19.13, eq 19.5\n",
-    "print\"\\t eG is : \\t\",eG\n",
-    "f=0.635; # from fig 19.15 as (AR/Acpt)=1.09 and eG=0.496\n",
-    "print\"\\t overall exchange factor : \\t\",f\n",
-    "Z=(Q1/(Acpt*f));\n",
-    "print\"\\t Z is : \\t\",round(Z)\n",
-    "print\"\\t TG required (at Ts = 800F) = 1670F compared with 1730DegF assumed in heat balance) \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.2 pgno:705"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.2 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\t Q is :  Btu/hr  24867609.5833\n",
-      "\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.2 \\n\"\n",
-    "QF=50000000.;\n",
-    "G=22.36;\n",
-    "Acpt=1500.;\n",
-    "print\"\\t approxiate values are mentioned in the book \"\n",
-    "Q=(QF/(1+(G/4200)*(QF/Acpt)**(1/2)))/2; # eq 19.15\n",
-    "print\"\\t Q is :  Btu/hr \",Q\n",
-    "print\"\\t The radiant-section average rate will be 8350 Btu/(hr) (ft2), and the exit-flue-gas temperature 1540DegF by heat balance. \\n\"\n",
-    "# end"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.3 pgno:707"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.3 \n",
-      "\n",
-      "\t approxiate values are mentioned in the book \n",
-      "\n",
-      "\t a1 is :   1.63\n",
-      "\t a2 is :  2.2331\n",
-      "\t Qr2 is :   0.309300671182\n",
-      "\t ratio of heats is :   1.22092370204\n",
-      "\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.3 \\n\"\n",
-    "Qr=1.5; # Qr=(QF2/QF1)\n",
-    "Cr=1.5; # Cr=(CR2/CR1)\n",
-    "Gr=140/125; # Gr=(G2/G1)\n",
-    "Qr1=0.38; # Qr1=(Q1/QF1)\n",
-    "print\"\\t approxiate values are mentioned in the book \\n\"\n",
-    "a1=1.63; # a1=(G1*(CR1/27)^(1/2)), from eq 19.17\n",
-    "print\"\\t a1 is :  \",a1\n",
-    "a2=1.37*(a1); # a2=(G2*(CR2/27)^(1/2))\n",
-    "print\"\\t a2 is : \",a2\n",
-    "Qr2=(1/(1+a2)); # Qr2=(Q2/QF2),from eq 19.15\n",
-    "print\"\\t Qr2 is :  \",Qr2\n",
-    "Q21=(Qr2/Qr1)*(Qr); # Q21=(Q2/Q1)\n",
-    "print\"\\t ratio of heats is :  \",round(Q21,2)\n",
-    "print\"\\t Hence the radiant absorption will be increased only 22 per cent for an increase of 50 per cent in the heat liberated. \\n\"\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.4 pgno:708"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.4 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t L is :  ft \t0.565\n",
-      "\t pH2OL is :  atm-ft \t0.070512\n",
-      "\t pCO2L is :  atm-ft \t0.061246\n",
-      "\t qTG is :  \t2750\n",
-      "\t qTG is :  \t325\n",
-      "\t q is :  \t2182.5\n",
-      "\t percentage correction at P : %.3f \t0.464837049743\n",
-      "\t Pt is :  \t0.131758\n",
-      "\t q1 is :  \t2138.85\n",
-      "\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \t2.51629411765\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.4 \\t\"\n",
-    "eS=0.9; # assumed\n",
-    "TG=1500;\n",
-    "TS=650;\n",
-    "pCO2=0.1084;\n",
-    "pH2O=0.1248;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "L=(0.4*8.5)-(0.567*5);  # table 19.1\n",
-    "print\"\\t L is :  ft \\t\",L\n",
-    "pH2OL=0.1248*L;\n",
-    "pCO2L=0.1084*L;\n",
-    "print\"\\t pH2OL is :  atm-ft \\t\",pH2OL\n",
-    "print\"\\t pCO2L is :  atm-ft \\t\",pCO2L\n",
-    "qH2O=1050; # at TG, from fig 19.12 ana 19.13\n",
-    "qCO2=1700; # at TG, from fig 19.12 ana 19.13\n",
-    "qTG=(qH2O+qCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTG\n",
-    "qsH2O=165; # at TS, from fig 19.12 ana 19.13\n",
-    "qsCO2=160; # at TS, from fig 19.12 ana 19.13\n",
-    "qTS=(qsH2O+qsCO2);\n",
-    "print\"\\t qTG is :  \\t\",qTS\n",
-    "q=(0.9*(qTG-qTS)); # q=(QRC/A)\n",
-    "print\"\\t q is :  \\t\",q\n",
-    "P=((pCO2)/(pCO2+pH2O));\n",
-    "print\"\\t percentage correction at P :\\t\",P\n",
-    "Pt=pCO2L+pH2OL;\n",
-    "print\"\\t Pt is :  \\t\",Pt\n",
-    "# %correction estimated to be 2%\n",
-    "q1=(q*0.98); # # q1=(QRC/A)\n",
-    "print\"\\t q1 is :  \\t\",q1\n",
-    "hr=(q1/(TG-TS));\n",
-    "print\"\\t radiation coefficient is :  Btu/(hr)*(ft^2)*(F) \\t\",round(hr,2)\n",
-    "#end\n",
-    "\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 19.5 pgno:709"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 19.5 \t\n",
-      "\t approxiate values are mentioned in the book \t\n",
-      "\t a is :  ft**2/ft \t3.5\n",
-      "\t AR is :  ft**2/ft \t9.6\n",
-      "\t ratio of two areas is :  \t2.74285714286\n",
-      "\t q1 is :  Btu/(hr)*(ft**2) \t10582\n",
-      "\t q2 is :  Btu/(hr)*(ft**2) \t5925.92\n",
-      "\t convection rate basis \t\n",
-      "\t q3 is :  Btu/(hr)*(ft**2) \t808.8\n",
-      "\t qt is :  Btu/(hr)*(ft**2) \t6734.72\n",
-      "\t required a is :  ft**2 \t74.2421362729\n",
-      "\t length required is :  ft \t19.2\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 19.5 \\t\"\n",
-    "Q=500000;\n",
-    "print\"\\t approxiate values are mentioned in the book \\t\"\n",
-    "a=(3.5+(3.14*4*(120/360)))/(1); # a=(alpha*Acp) from fig 19.17\n",
-    "AR=(3+3.6+3);\n",
-    "print\"\\t a is :  ft**2/ft \\t\",a\n",
-    "print\"\\t AR is :  ft**2/ft \\t\",AR\n",
-    "# Arbitrarily neglecting end wa.lls and also .the side wall refractory over 3'0\" above the floor\n",
-    "R=(AR/a);\n",
-    "print\"\\t ratio of two areas is :  \\t\",R\n",
-    "eG=0.265;\n",
-    "TG=1174; # F\n",
-    "TS=500; # F\n",
-    "f=0.56; # from fig 19.15 as (AR/Acpt)=2.49 and eG=0.265\n",
-    "q=15300; # at TG and TS,q=(Q/(a*f))\n",
-    "# However, the convection coefficient is small, 1.0 +or- Btu/(hr)(ft2)(\"F), and AR/a is not 2.0 as in the assumptions for the Lobo and Evans equation.\n",
-    "q1=(q)-(7*(TG-TS)); # q1=(Q/(a*f))\n",
-    "print\"\\t q1 is :  Btu/(hr)*(ft**2) \\t\",q1\n",
-    "q2=(q1*f); # q2=(Q/(a))\n",
-    "print\"\\t q2 is :  Btu/(hr)*(ft**2) \\t\",q2\n",
-    "print\"\\t convection rate basis \\t\"\n",
-    "q3=(1*(TG-TS)*(4.2/a)); # q2=(Q/(a))\n",
-    "print\"\\t q3 is :  Btu/(hr)*(ft**2) \\t\",q3 # calculation mistake in book\n",
-    "qt=(q2+q3); # qt=(Q/(a))\n",
-    "print\"\\t qt is :  Btu/(hr)*(ft**2) \\t\",qt\n",
-    "ar=(Q/qt);\n",
-    "print\"\\t required a is :  ft**2 \\t\",ar\n",
-    "L=(ar/a)-2;\n",
-    "print\"\\t length required is :  ft \\t\",round(L,1)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications.ipynb
deleted file mode 100755
index a3fc5450..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications.ipynb
+++ /dev/null
@@ -1,904 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 20: Additoinal Applications"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.1 pgno:719"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t413.861386139\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t324.366270047\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t123.717442778\n",
-      "\t temperature difference is : F \t76.8232268984\n",
-      "\t temperature of the steam :  F \t221.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T=150; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1100; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=3.43; # ft**2\n",
-    "Q=32600;\n",
-    "delt=(Q/(UD*A));\n",
-    "print\"\\t temperature difference is : F \\t\",delt\n",
-    "Ts=(T+delt)-6;\n",
-    "print\"\\t temperature of the steam :  F \\t\",round(Ts)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.2 pgno:723"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t639.603960396\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t448.40351689\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t138.310019983\n",
-      "\t Area is :  ft**2 \t3.36717676544\n",
-      "\t area per turn is :  ft**2 \t0.3288208\n",
-      "\t number of turns :  \t10.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=150; # F\n",
-    "T2=220; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1700; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Q=32600;\n",
-    "A=(Q/(UD*(T2-T1)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A\n",
-    "a=0.1309; # ft**2/ft\n",
-    "a1=(3.14*0.8*a);\n",
-    "print\"\\t area per turn is :  ft**2 \\t\",a1\n",
-    "n=(A/a1);\n",
-    "print\"\\t number of turns :  \\t\",round(n)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.3 pgno:725"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for oil \t\n",
-      "\t total heat required for oil is : Btu/hr \t10062400.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is : Btu/hr \t10200000\n",
-      "\t delt1 is : F \t80\n",
-      "\t delt2 is : F \t535\n",
-      "\t LMTD is  F \t230\n",
-      "\t caloric temperature of hot fluid is : F \t437\n",
-      "\t caloric temperature of cold fluid is : \t130\n",
-      "\t hot fluid:inner tube side, oil \t\n",
-      "\t flow area is : ft**2 \t0.0458\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t722707.423581\n",
-      "\t reynolds number is : \t31455.9705947\n",
-      "\t hi is : Btu/(hr)*(ft**2)*(F) \t101.239669421\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t83.8842975207\n",
-      "\t tw is : F \t240.107773852\n",
-      "\t tf is : F \t185.053886926\n",
-      "\t Uc is : Btu/(hr)*(ft**2)*(F) \t53.7985865724\n",
-      "\t hd is : \t100.0\n",
-      "\t UD is : Btu/(hr)*(ft**2)*(F) \t34.9798966111\n",
-      "\t Area is : ft**2 \t1267.80895267\n",
-      "\t pipe length : \t58.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=675; # inlet hot fluid,F\n",
-    "T2=200; # outlet hot fluid,F\n",
-    "t1=120; # inlet cold fluid,F\n",
-    "t2=140; # outlet cold fluid,F\n",
-    "W=33100; # lb/hr\n",
-    "w=510000; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for oil \\t\"\n",
-    "c=0.64; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is : Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=230;\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, oil \\t\"\n",
-    "at=0.0458; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=5.56; # at 400F,lb/(ft)*(hr)\n",
-    "D=0.242; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "jH=100; # from fig.24\n",
-    "Z=0.245; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft), fig 16\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is : Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=2.9; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=150; # Btu/(hr)*(ft**2)\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is : F \\t\",tw\n",
-    "tf=(tw+tc)/2;\n",
-    "print\"\\t tf is : F \\t\",tf\n",
-    "delt=110; # F\n",
-    "d0=3.5; # in, fig 10.4\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is : \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is : ft**2 \\t\",A\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "L=(A/(a*24));\n",
-    "print\"\\t pipe length : \\t\",round(L)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.4 pgno:729"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for SO2 \t\n",
-      "\t total heat required for SO2 is :  Btu/hr \t166320.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t166500.0\n",
-      "\t delt1 is :  F \t65.0\n",
-      "\t delt2 is :  F \t350.0\n",
-      "\t LMTD is : F \t169.475824421\n",
-      "\t delt is :  F \t166.086307932\n",
-      "\t caloric temperature of hot fluid is :  F \t300.0\n",
-      "\t caloric temperature of cold fluid is :  \t92.5\n",
-      "\t hot fluid:inner tube side, SO2 \t\n",
-      "\t flow area is :  ft**2 \t0.0512\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t65625.0\n",
-      "\t reynolds number is :  \t409756.097561\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t21.0800390625\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t18.4781599554\n",
-      "\t cold fluid water \t\n",
-      "\t G :  lb/(hr)*(ft) \t693\n",
-      "\t Re is : \t1428.86597938\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t65.0\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t14.3879596501\n",
-      "\t hd is :  \t100.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t12.5782116353\n",
-      "\t Area is :  ft**2 \t78.10657332\n",
-      "\t pipe length :  \t8.75\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=3360; # lb/hr\n",
-    "w=11100; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for SO2 \\t\"\n",
-    "c=0.165; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for SO2 is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=20;\n",
-    "S=0.0412;\n",
-    "FT=0.98; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, SO2 \\t\"\n",
-    "at=0.0512; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.041; # at 300F,lb/(ft)*(hr), fig 15\n",
-    "D=0.256; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=790; # from fig.24\n",
-    "Z=0.006831; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft)\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=3.068; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid water \\t\"\n",
-    "L=8; # ft\n",
-    "G=(w/(2*L));\n",
-    "print\"\\t G :  lb/(hr)*(ft) \\t\",G\n",
-    "mu1=1.94; # at 92.5F, lb/(ft)*(hr)\n",
-    "Re=(4*G/mu1);\n",
-    "print\"\\t Re is : \\t\",Re\n",
-    "Do=0.292; # ft\n",
-    "ho=(65*(G/Do)**(1/3));\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A # calculation mistake in book\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "l=(A/(a*8))-1.9;\n",
-    "print\"\\t pipe length :  \\t\",round(l,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 20.5 pgno:736"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t evaporation percentage is :  \t0.121913091814\n",
-      "\t heat load is :  Btu/hr \t1917500\n",
-      "\t sensible heat is :  Btu/hr \t1687400.0\n",
-      "\t final spray temperature is :  F \t110.088095238\n",
-      "\t total spray :  lb/hr \t84000.0\n",
-      "\t m is :  lb/(hr)*(ft**2) \t875.0\n",
-      "\t Z is :  \t1.12568513365\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t316.940192565\n",
-      "\t tube side coefficient \t\n",
-      "\t assuming even number of passes and tube side velocity about 8fps \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1903225.80645\n",
-      "\t velocity is :  fps \t8.45878136201\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1861.8\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t270.83506906\n",
-      "\t total surface is :  ft**2 \t471.24\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t33.0\n",
-      "\t LMTD is : F \t36.4287504681\n",
-      "\t delt is :  F \t35.3358879541\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t115.153519517\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Nt=25.; # number of tubes\n",
-    "A=50.; # total projected area\n",
-    "Tav=100.; # F\n",
-    "s=28.; # assumption spray, lb/(min)*(ft**2)\n",
-    "Do=0.0833; # ft\n",
-    "PH=0.1562;\n",
-    "Y=0.874;\n",
-    "Z=0.466;\n",
-    "E=(0.171*(Do*Y*Z)**0.1); # (E/(Do*Y*Z)**0.1)=0.171, from fig 20.10\n",
-    "from math import log10\n",
-    "print\"\\t evaporation percentage is :  \\t\",E\n",
-    "Q=(295*500*(143-130));\n",
-    "print\"\\t heat load is :  Btu/hr \\t\",Q\n",
-    "Q1=(Q*(1-0.12));\n",
-    "print\"\\t sensible heat is :  Btu/hr \\t\",Q1\n",
-    "t2=(90)+(Q1/(28*60*50));\n",
-    "print\"\\t final spray temperature is :  F \\t\",t2\n",
-    "w=(s*60*50);\n",
-    "print\"\\t total spray :  lb/hr \\t\",w\n",
-    "m=(w/(2*4*12));\n",
-    "print\"\\t m is :  lb/(hr)*(ft**2) \\t\",m\n",
-    "mu=1.84; # lb/(ft)*(hr)\n",
-    "Z=((m**0.3)*Do*Y*Z/(mu*0.125));\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "N=3; # assume 3 horizontal rows\n",
-    "ho=300*(N**0.05); # (ho/(N**0.05))=300, from fig 20.11\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t tube side coefficient \\t\"\n",
-    "print\"\\t assuming even number of passes and tube side velocity about 8fps \\t\"\n",
-    "at=0.0775; # ft**2\n",
-    "Gt=(295*500/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "hi=2140; # Btu/(hr)*(ft**2)*(F), fig 25\n",
-    "ID=0.87; # ft\n",
-    "OD=1; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "a=0.2618; # ft**2, table 11\n",
-    "A1=(2*3*25*12*a);\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A1\n",
-    "T1=143; # inlet hot fluid,F\n",
-    "T2=130; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=110; # outlet cold fluid,F\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "delt1=40.;\n",
-    "delt2=33.;\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD # calculation mistake in book\n",
-    "R=0.65;\n",
-    "S=0.377;\n",
-    "FT=0.97; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "UD=(Q/(A1*(delt)));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.6 pgno:745"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t R is :  \t2.0\n",
-      "\t V is :  \t1.5\n",
-      "\t F is :  \t1\n",
-      "\t Z is :  \t0.733333333333\n",
-      "\t deltD is :  \t1.1745\n",
-      "\t delt is :  \t58.725\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t72.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=50.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "from math import log10\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "V=((T1+T2-t1-t2)/(t2-t1))/(2);\n",
-    "print\"\\t V is :  \\t\",V\n",
-    "u=120;\n",
-    "U=60;\n",
-    "F=((u*1)/(U*2));\n",
-    "print\"\\t F is :  \\t\",F\n",
-    "E=1.1; # In Fig.20.18b for R = 2.0and F = l.O,the abscissa and ordinate intersect at E =1.10.\n",
-    "Z=(E/V);\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "deltD=0.783*V; # deltD/V=0.783, from fig 20.17\n",
-    "print\"\\t deltD is :  \\t\",deltD\n",
-    "delt=(deltD*(t2-t1));\n",
-    "print\"\\t delt is :  \\t\",delt\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.7 pgno:752"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t beta is : \t0.0036\n",
-      "\t for sand \t\n",
-      "\t total heat required for sand is : Btu/hr \t36000.0\n",
-      "\t w is : lb/hr \t2000.0\n",
-      "\t R is : \t0.1\n",
-      "\t S is : \t0.909090909091\n",
-      "\t rate per tube is : lb/hr \t62.475\n",
-      "\t number of tubes : \t16.006402561\n",
-      "\t for air assume hoi=9 and Beta=0.2 \t\n",
-      "\t w1 is : lb/hr \t8000.0\n",
-      "\t rate per tube is : lb/hr \t39.0\n",
-      "\t number of tubes : \t25.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=284.; # inlet hot fluid,F\n",
-    "T2=104.; # outlet hot fluid,F\n",
-    "t1=86.; # inlet cold fluid,F\n",
-    "t2=104.; # outlet cold fluid,F\n",
-    "W=1000; # lb/hr\n",
-    "k=0.15; # thermal conductivity\n",
-    "L=10;\n",
-    "Beta=((2*k)/(500*(2./12.))); # hoi=500Btu/(hr)*(ft^2)*(F) for water\n",
-    "print\"\\t beta is : \\t\",Beta\n",
-    "print\"\\t for sand \\t\"\n",
-    "C=0.2; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for sand is : Btu/hr \\t\",Q\n",
-    "c=1;\n",
-    "w=(Q/(t2-t1));\n",
-    "print\"\\t w is : lb/hr \\t\",w\n",
-    "R=((W*C)/(w*c));\n",
-    "print\"\\t R is : \\t\",R\n",
-    "S=((T2-T1)/(t1-T1));\n",
-    "print\"\\t S is : \\t\",S\n",
-    "W1=(8.33*(k*L)/C); # ((W1*C)/(k*L))=8.33 from fig 20.20b for Beta=0\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",W1\n",
-    "N1=(W/W1);\n",
-    "print\"\\t number of tubes : \\t\",N1\n",
-    "print\"\\t for air assume hoi=9 and Beta=0.2 \\t\"\n",
-    "c1=0.25;\n",
-    "w1=(Q/(c1*(t2-t1)));\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "W2=(5.23*(k*L)/C); # ((W1*C)/(k*L))=5.23 from fig 20.20b for Beta=0.2\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",round(W2)\n",
-    "N2=(W/W2);\n",
-    "print\"\\t number of tubes : \\t\",round(N2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8a pgno758"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8a \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t Lb of water is :  lb \t375.0\n",
-      "\t heat to be supplied :  kwhr \t5.49531066823\n",
-      "\t losses \t\n",
-      "\t from surface of water :  kwhr \t1\n",
-      "\t from sides of vessel :  kwhr \t0.11\n",
-      "\t losses from bottom are negigible \t\n",
-      "\t total requirement :  kwhr \t6.60531066823\n",
-      "\t steady state \t\n",
-      "\t heat to be supplied :  kwhr \t1.9531066823\n",
-      "\t total requirement :  kwhr \t3.06\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8a \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "L=3; # ft\n",
-    "B=2; # ft\n",
-    "h=18/12; # ft , height of water present in tank\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*h*62.5);\n",
-    "print\"\\t Lb of water is :  lb \\t\",m\n",
-    "t1=50;\n",
-    "t2=150;\n",
-    "c=1;\n",
-    "Q=(m*c*(t2-t1))/(2*3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Q\n",
-    "print\"\\t losses \\t\"\n",
-    "Q1=(L*B*260)/(1000); # from fig 20.25c\n",
-    "print\"\\t from surface of water :  kwhr \\t\",Q1\n",
-    "Q2=(5.5*((2*B*2)+(2*L*B))/(1000)); # from fig 20.25c\n",
-    "print\"\\t from sides of vessel :  kwhr \\t\",Q2\n",
-    "print\"\\t losses from bottom are negigible \\t\"\n",
-    "Qt=(Q+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",Qt\n",
-    "print\"\\t steady state \\t\"\n",
-    "m1=8; # gal/hr\n",
-    "Qs=(m1*8.33*c*(t2-t1))/(3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Qs\n",
-    "Qts=(Qs+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",round(Qts,2)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8b pgno:760"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8b \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat to steel charge :  Btu \t3600.0\n",
-      "\t heat to air :  Btu \t540.0\n",
-      "\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \t\n",
-      "\t total requirement :  kw \t3.71\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8b \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=100; # lb\n",
-    "t1=70;\n",
-    "t2=370; \n",
-    "L=4;\n",
-    "B=3;\n",
-    "n=4; # number of air changers\n",
-    "c1=0.12\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat to steel charge :  Btu \\t\",Q1\n",
-    "c2=0.25\n",
-    "Q2=(n*L*B*2*0.075*c2*(t2-t1));\n",
-    "print\"\\t heat to air :  Btu \\t\",Q2\n",
-    "print\"\\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \\t\"\n",
-    "Qt=((Q1+Q2)/(3412))+(2.5)\n",
-    "print\"\\t total requirement :  kw \\t\",round(Qt,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8c pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8c \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat :  Btu \t15187.5\n",
-      "\t velocity is :  fps \t2.0\n",
-      "\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \t\n",
-      "\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8c \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=270; # cfm\n",
-    "t1=70;\n",
-    "t2=120; \n",
-    "L=1.5; # ft\n",
-    "B=1.5; # ft\n",
-    "c=0.25\n",
-    "row=0.075; # lb/ft^3\n",
-    "Q=(m*row*60*c*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q\n",
-    "V=(m/(L*B*60)); # fps\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "print\"\\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \\t\"\n",
-    "print\"\\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8d pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8d \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t weight of plate :  lb \t81.25\n",
-      "\t heat :  Btu \t2429.375\n",
-      "\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \t\n",
-      "\t radiation loss :  kw \t0.7722\n",
-      "\t total requirement :  kw \t1.48420908558\n",
-      "\t staedy state \t\n",
-      "\t heat :  Btu \t3542.0\n",
-      "\t total requirement :  kw \t1.83810082063\n",
-      "\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \t\n",
-      "\t delt is :  F \t264.0\n",
-      "\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8d \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=70;\n",
-    "t2=300; \n",
-    "L=26; # in\n",
-    "B=12; # in\n",
-    "H=1; # in\n",
-    "c1=0.13\n",
-    "# specific gravity of cast iron is 7.2\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*H*62.5*7.2/1728); # lb\n",
-    "print\"\\t weight of plate :  lb \\t\",m\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q1\n",
-    "print\"\\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \\t\"\n",
-    "Q2=(2*26*12*1.5*0.825/1000); # ke\n",
-    "print\"\\t radiation loss :  kw \\t\",Q2\n",
-    "Qt=((Q1)/(3412))+(Q2);\n",
-    "print\"\\t total requirement :  kw \\t\",Qt\n",
-    "print\"\\t staedy state \\t\"\n",
-    "m2=70;\n",
-    "c2=0.22;\n",
-    "Qs=(m2*c2*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Qs\n",
-    "Ql=0.8; # kw\n",
-    "Qts=((Qs)/(3412))+(Ql);\n",
-    "print\"\\t total requirement :  kw \\t\",Qts\n",
-    "print\"\\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \\t\"\n",
-    "delt=(16*16.5);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_1.ipynb
deleted file mode 100755
index 417b7f25..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_1.ipynb
+++ /dev/null
@@ -1,886 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 20: Additoinal Applications"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.1 pgno:719"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t413.861386139\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t324.366270047\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t123.717442778\n",
-      "\t temperature difference is : F \t76.8232268984\n",
-      "\t temperature of the steam :  F \t221.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T=150; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1100; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=3.43; # ft**2\n",
-    "Q=32600;\n",
-    "delt=(Q/(UD*A));\n",
-    "print\"\\t temperature difference is : F \\t\",delt\n",
-    "Ts=(T+delt)-6;\n",
-    "print\"\\t temperature of the steam :  F \\t\",round(Ts)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.2 pgno:723"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t639.603960396\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t448.40351689\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t138.310019983\n",
-      "\t Area is :  ft**2 \t3.36717676544\n",
-      "\t area per turn is :  ft**2 \t0.3288208\n",
-      "\t number of turns :  \t10.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=150; # F\n",
-    "T2=220; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1700; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Q=32600;\n",
-    "A=(Q/(UD*(T2-T1)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A\n",
-    "a=0.1309; # ft**2/ft\n",
-    "a1=(3.14*0.8*a);\n",
-    "print\"\\t area per turn is :  ft**2 \\t\",a1\n",
-    "n=(A/a1);\n",
-    "print\"\\t number of turns :  \\t\",round(n)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.3 pgno:725"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for oil \t\n",
-      "\t total heat required for oil is : Btu/hr \t10062400.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is : Btu/hr \t10200000\n",
-      "\t delt1 is : F \t80\n",
-      "\t delt2 is : F \t535\n",
-      "\t LMTD is  F \t230\n",
-      "\t caloric temperature of hot fluid is : F \t437\n",
-      "\t caloric temperature of cold fluid is : \t130\n",
-      "\t hot fluid:inner tube side, oil \t\n",
-      "\t flow area is : ft**2 \t0.0458\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t722707.423581\n",
-      "\t reynolds number is : \t31455.9705947\n",
-      "\t hi is : Btu/(hr)*(ft**2)*(F) \t101.239669421\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t83.8842975207\n",
-      "\t tw is : F \t240.107773852\n",
-      "\t tf is : F \t185.053886926\n",
-      "\t Uc is : Btu/(hr)*(ft**2)*(F) \t53.7985865724\n",
-      "\t hd is : \t100.0\n",
-      "\t UD is : Btu/(hr)*(ft**2)*(F) \t34.9798966111\n",
-      "\t Area is : ft**2 \t1267.80895267\n",
-      "\t pipe length : \t58.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=675; # inlet hot fluid,F\n",
-    "T2=200; # outlet hot fluid,F\n",
-    "t1=120; # inlet cold fluid,F\n",
-    "t2=140; # outlet cold fluid,F\n",
-    "W=33100; # lb/hr\n",
-    "w=510000; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for oil \\t\"\n",
-    "c=0.64; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is : Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=230;\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, oil \\t\"\n",
-    "at=0.0458; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=5.56; # at 400F,lb/(ft)*(hr)\n",
-    "D=0.242; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "jH=100; # from fig.24\n",
-    "Z=0.245; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft), fig 16\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is : Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=2.9; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=150; # Btu/(hr)*(ft**2)\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is : F \\t\",tw\n",
-    "tf=(tw+tc)/2;\n",
-    "print\"\\t tf is : F \\t\",tf\n",
-    "delt=110; # F\n",
-    "d0=3.5; # in, fig 10.4\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is : \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is : ft**2 \\t\",A\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "L=(A/(a*24));\n",
-    "print\"\\t pipe length : \\t\",round(L)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.4 pgno:729"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for SO2 \t\n",
-      "\t total heat required for SO2 is :  Btu/hr \t166320.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t166500.0\n",
-      "\t delt1 is :  F \t65.0\n",
-      "\t delt2 is :  F \t350.0\n",
-      "\t LMTD is : F \t169.475824421\n",
-      "\t delt is :  F \t166.086307932\n",
-      "\t caloric temperature of hot fluid is :  F \t300.0\n",
-      "\t caloric temperature of cold fluid is :  \t92.5\n",
-      "\t hot fluid:inner tube side, SO2 \t\n",
-      "\t flow area is :  ft**2 \t0.0512\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t65625.0\n",
-      "\t reynolds number is :  \t409756.097561\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t21.0800390625\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t18.4781599554\n",
-      "\t cold fluid water \t\n",
-      "\t G :  lb/(hr)*(ft) \t693\n",
-      "\t Re is : \t1428.86597938\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t65.0\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t14.3879596501\n",
-      "\t hd is :  \t100.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t12.5782116353\n",
-      "\t Area is :  ft**2 \t78.10657332\n",
-      "\t pipe length :  \t8.75\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=3360; # lb/hr\n",
-    "w=11100; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for SO2 \\t\"\n",
-    "c=0.165; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for SO2 is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=20;\n",
-    "S=0.0412;\n",
-    "FT=0.98; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, SO2 \\t\"\n",
-    "at=0.0512; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.041; # at 300F,lb/(ft)*(hr), fig 15\n",
-    "D=0.256; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=790; # from fig.24\n",
-    "Z=0.006831; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft)\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=3.068; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid water \\t\"\n",
-    "L=8; # ft\n",
-    "G=(w/(2*L));\n",
-    "print\"\\t G :  lb/(hr)*(ft) \\t\",G\n",
-    "mu1=1.94; # at 92.5F, lb/(ft)*(hr)\n",
-    "Re=(4*G/mu1);\n",
-    "print\"\\t Re is : \\t\",Re\n",
-    "Do=0.292; # ft\n",
-    "ho=(65*(G/Do)**(1/3));\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A # calculation mistake in book\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "l=(A/(a*8))-1.9;\n",
-    "print\"\\t pipe length :  \\t\",round(l,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 20.5 pgno:736"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t evaporation percentage is :  \t0.121913091814\n",
-      "\t heat load is :  Btu/hr \t1917500\n",
-      "\t sensible heat is :  Btu/hr \t1687400.0\n",
-      "\t final spray temperature is :  F \t110.088095238\n",
-      "\t total spray :  lb/hr \t84000.0\n",
-      "\t m is :  lb/(hr)*(ft**2) \t875.0\n",
-      "\t Z is :  \t1.12568513365\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t316.940192565\n",
-      "\t tube side coefficient \t\n",
-      "\t assuming even number of passes and tube side velocity about 8fps \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1903225.80645\n",
-      "\t velocity is :  fps \t8.45878136201\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1861.8\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t270.83506906\n",
-      "\t total surface is :  ft**2 \t471.24\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t33.0\n",
-      "\t LMTD is : F \t36.4287504681\n",
-      "\t delt is :  F \t35.3358879541\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t115.153519517\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Nt=25.; # number of tubes\n",
-    "A=50.; # total projected area\n",
-    "Tav=100.; # F\n",
-    "s=28.; # assumption spray, lb/(min)*(ft**2)\n",
-    "Do=0.0833; # ft\n",
-    "PH=0.1562;\n",
-    "Y=0.874;\n",
-    "Z=0.466;\n",
-    "E=(0.171*(Do*Y*Z)**0.1); # (E/(Do*Y*Z)**0.1)=0.171, from fig 20.10\n",
-    "from math import log10\n",
-    "print\"\\t evaporation percentage is :  \\t\",E\n",
-    "Q=(295*500*(143-130));\n",
-    "print\"\\t heat load is :  Btu/hr \\t\",Q\n",
-    "Q1=(Q*(1-0.12));\n",
-    "print\"\\t sensible heat is :  Btu/hr \\t\",Q1\n",
-    "t2=(90)+(Q1/(28*60*50));\n",
-    "print\"\\t final spray temperature is :  F \\t\",t2\n",
-    "w=(s*60*50);\n",
-    "print\"\\t total spray :  lb/hr \\t\",w\n",
-    "m=(w/(2*4*12));\n",
-    "print\"\\t m is :  lb/(hr)*(ft**2) \\t\",m\n",
-    "mu=1.84; # lb/(ft)*(hr)\n",
-    "Z=((m**0.3)*Do*Y*Z/(mu*0.125));\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "N=3; # assume 3 horizontal rows\n",
-    "ho=300*(N**0.05); # (ho/(N**0.05))=300, from fig 20.11\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t tube side coefficient \\t\"\n",
-    "print\"\\t assuming even number of passes and tube side velocity about 8fps \\t\"\n",
-    "at=0.0775; # ft**2\n",
-    "Gt=(295*500/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "hi=2140; # Btu/(hr)*(ft**2)*(F), fig 25\n",
-    "ID=0.87; # ft\n",
-    "OD=1; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "a=0.2618; # ft**2, table 11\n",
-    "A1=(2*3*25*12*a);\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A1\n",
-    "T1=143; # inlet hot fluid,F\n",
-    "T2=130; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=110; # outlet cold fluid,F\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "delt1=40.;\n",
-    "delt2=33.;\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD # calculation mistake in book\n",
-    "R=0.65;\n",
-    "S=0.377;\n",
-    "FT=0.97; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "UD=(Q/(A1*(delt)));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.6 pgno:745"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t R is :  \t2.0\n",
-      "\t V is :  \t1.5\n",
-      "\t F is :  \t1\n",
-      "\t Z is :  \t0.733333333333\n",
-      "\t deltD is :  \t1.1745\n",
-      "\t delt is :  \t58.725\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t72.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=50.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "from math import log10\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "V=((T1+T2-t1-t2)/(t2-t1))/(2);\n",
-    "print\"\\t V is :  \\t\",V\n",
-    "u=120;\n",
-    "U=60;\n",
-    "F=((u*1)/(U*2));\n",
-    "print\"\\t F is :  \\t\",F\n",
-    "E=1.1; # In Fig.20.18b for R = 2.0and F = l.O,the abscissa and ordinate intersect at E =1.10.\n",
-    "Z=(E/V);\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "deltD=0.783*V; # deltD/V=0.783, from fig 20.17\n",
-    "print\"\\t deltD is :  \\t\",deltD\n",
-    "delt=(deltD*(t2-t1));\n",
-    "print\"\\t delt is :  \\t\",delt\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.7 pgno:752"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t beta is : \t0.0036\n",
-      "\t for sand \t\n",
-      "\t total heat required for sand is : Btu/hr \t36000.0\n",
-      "\t w is : lb/hr \t2000.0\n",
-      "\t R is : \t0.1\n",
-      "\t S is : \t0.909090909091\n",
-      "\t rate per tube is : lb/hr \t62.475\n",
-      "\t number of tubes : \t16.006402561\n",
-      "\t for air assume hoi=9 and Beta=0.2 \t\n",
-      "\t w1 is : lb/hr \t8000.0\n",
-      "\t rate per tube is : lb/hr \t39.0\n",
-      "\t number of tubes : \t25.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=284.; # inlet hot fluid,F\n",
-    "T2=104.; # outlet hot fluid,F\n",
-    "t1=86.; # inlet cold fluid,F\n",
-    "t2=104.; # outlet cold fluid,F\n",
-    "W=1000; # lb/hr\n",
-    "k=0.15; # thermal conductivity\n",
-    "L=10;\n",
-    "Beta=((2*k)/(500*(2./12.))); # hoi=500Btu/(hr)*(ft^2)*(F) for water\n",
-    "print\"\\t beta is : \\t\",Beta\n",
-    "print\"\\t for sand \\t\"\n",
-    "C=0.2; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for sand is : Btu/hr \\t\",Q\n",
-    "c=1;\n",
-    "w=(Q/(t2-t1));\n",
-    "print\"\\t w is : lb/hr \\t\",w\n",
-    "R=((W*C)/(w*c));\n",
-    "print\"\\t R is : \\t\",R\n",
-    "S=((T2-T1)/(t1-T1));\n",
-    "print\"\\t S is : \\t\",S\n",
-    "W1=(8.33*(k*L)/C); # ((W1*C)/(k*L))=8.33 from fig 20.20b for Beta=0\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",W1\n",
-    "N1=(W/W1);\n",
-    "print\"\\t number of tubes : \\t\",N1\n",
-    "print\"\\t for air assume hoi=9 and Beta=0.2 \\t\"\n",
-    "c1=0.25;\n",
-    "w1=(Q/(c1*(t2-t1)));\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "W2=(5.23*(k*L)/C); # ((W1*C)/(k*L))=5.23 from fig 20.20b for Beta=0.2\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",round(W2)\n",
-    "N2=(W/W2);\n",
-    "print\"\\t number of tubes : \\t\",round(N2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8a pgno758"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8a \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t Lb of water is :  lb \t375.0\n",
-      "\t heat to be supplied :  kwhr \t5.49531066823\n",
-      "\t losses \t\n",
-      "\t from surface of water :  kwhr \t1\n",
-      "\t from sides of vessel :  kwhr \t0.11\n",
-      "\t losses from bottom are negigible \t\n",
-      "\t total requirement :  kwhr \t6.60531066823\n",
-      "\t steady state \t\n",
-      "\t heat to be supplied :  kwhr \t1.9531066823\n",
-      "\t total requirement :  kwhr \t3.06\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8a \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "L=3; # ft\n",
-    "B=2; # ft\n",
-    "h=18/12; # ft , height of water present in tank\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*h*62.5);\n",
-    "print\"\\t Lb of water is :  lb \\t\",m\n",
-    "t1=50;\n",
-    "t2=150;\n",
-    "c=1;\n",
-    "Q=(m*c*(t2-t1))/(2*3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Q\n",
-    "print\"\\t losses \\t\"\n",
-    "Q1=(L*B*260)/(1000); # from fig 20.25c\n",
-    "print\"\\t from surface of water :  kwhr \\t\",Q1\n",
-    "Q2=(5.5*((2*B*2)+(2*L*B))/(1000)); # from fig 20.25c\n",
-    "print\"\\t from sides of vessel :  kwhr \\t\",Q2\n",
-    "print\"\\t losses from bottom are negigible \\t\"\n",
-    "Qt=(Q+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",Qt\n",
-    "print\"\\t steady state \\t\"\n",
-    "m1=8; # gal/hr\n",
-    "Qs=(m1*8.33*c*(t2-t1))/(3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Qs\n",
-    "Qts=(Qs+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",round(Qts,2)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8b pgno:760"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8b \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat to steel charge :  Btu \t3600.0\n",
-      "\t heat to air :  Btu \t540.0\n",
-      "\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \t\n",
-      "\t total requirement :  kw \t3.71\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8b \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=100; # lb\n",
-    "t1=70;\n",
-    "t2=370; \n",
-    "L=4;\n",
-    "B=3;\n",
-    "n=4; # number of air changers\n",
-    "c1=0.12\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat to steel charge :  Btu \\t\",Q1\n",
-    "c2=0.25\n",
-    "Q2=(n*L*B*2*0.075*c2*(t2-t1));\n",
-    "print\"\\t heat to air :  Btu \\t\",Q2\n",
-    "print\"\\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \\t\"\n",
-    "Qt=((Q1+Q2)/(3412))+(2.5)\n",
-    "print\"\\t total requirement :  kw \\t\",round(Qt,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8c pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8c \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat :  Btu \t15187.5\n",
-      "\t velocity is :  fps \t2.0\n",
-      "\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \t\n",
-      "\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8c \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=270; # cfm\n",
-    "t1=70;\n",
-    "t2=120; \n",
-    "L=1.5; # ft\n",
-    "B=1.5; # ft\n",
-    "c=0.25\n",
-    "row=0.075; # lb/ft^3\n",
-    "Q=(m*row*60*c*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q\n",
-    "V=(m/(L*B*60)); # fps\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "print\"\\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \\t\"\n",
-    "print\"\\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8d pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8d \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t weight of plate :  lb \t81.25\n",
-      "\t heat :  Btu \t2429.375\n",
-      "\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \t\n",
-      "\t radiation loss :  kw \t0.7722\n",
-      "\t total requirement :  kw \t1.48420908558\n",
-      "\t staedy state \t\n",
-      "\t heat :  Btu \t3542.0\n",
-      "\t total requirement :  kw \t1.83810082063\n",
-      "\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \t\n",
-      "\t delt is :  F \t264.0\n",
-      "\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8d \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=70;\n",
-    "t2=300; \n",
-    "L=26; # in\n",
-    "B=12; # in\n",
-    "H=1; # in\n",
-    "c1=0.13\n",
-    "# specific gravity of cast iron is 7.2\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*H*62.5*7.2/1728); # lb\n",
-    "print\"\\t weight of plate :  lb \\t\",m\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q1\n",
-    "print\"\\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \\t\"\n",
-    "Q2=(2*26*12*1.5*0.825/1000); # ke\n",
-    "print\"\\t radiation loss :  kw \\t\",Q2\n",
-    "Qt=((Q1)/(3412))+(Q2);\n",
-    "print\"\\t total requirement :  kw \\t\",Qt\n",
-    "print\"\\t staedy state \\t\"\n",
-    "m2=70;\n",
-    "c2=0.22;\n",
-    "Qs=(m2*c2*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Qs\n",
-    "Ql=0.8; # kw\n",
-    "Qts=((Qs)/(3412))+(Ql);\n",
-    "print\"\\t total requirement :  kw \\t\",Qts\n",
-    "print\"\\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \\t\"\n",
-    "delt=(16*16.5);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \\t\"\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_2.ipynb
deleted file mode 100755
index 417b7f25..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_2.ipynb
+++ /dev/null
@@ -1,886 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 20: Additoinal Applications"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.1 pgno:719"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t413.861386139\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t324.366270047\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t123.717442778\n",
-      "\t temperature difference is : F \t76.8232268984\n",
-      "\t temperature of the steam :  F \t221.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T=150; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1100; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=3.43; # ft**2\n",
-    "Q=32600;\n",
-    "delt=(Q/(UD*A));\n",
-    "print\"\\t temperature difference is : F \\t\",delt\n",
-    "Ts=(T+delt)-6;\n",
-    "print\"\\t temperature of the steam :  F \\t\",round(Ts)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.2 pgno:723"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t639.603960396\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t448.40351689\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t138.310019983\n",
-      "\t Area is :  ft**2 \t3.36717676544\n",
-      "\t area per turn is :  ft**2 \t0.3288208\n",
-      "\t number of turns :  \t10.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=150; # F\n",
-    "T2=220; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1700; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Q=32600;\n",
-    "A=(Q/(UD*(T2-T1)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A\n",
-    "a=0.1309; # ft**2/ft\n",
-    "a1=(3.14*0.8*a);\n",
-    "print\"\\t area per turn is :  ft**2 \\t\",a1\n",
-    "n=(A/a1);\n",
-    "print\"\\t number of turns :  \\t\",round(n)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.3 pgno:725"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for oil \t\n",
-      "\t total heat required for oil is : Btu/hr \t10062400.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is : Btu/hr \t10200000\n",
-      "\t delt1 is : F \t80\n",
-      "\t delt2 is : F \t535\n",
-      "\t LMTD is  F \t230\n",
-      "\t caloric temperature of hot fluid is : F \t437\n",
-      "\t caloric temperature of cold fluid is : \t130\n",
-      "\t hot fluid:inner tube side, oil \t\n",
-      "\t flow area is : ft**2 \t0.0458\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t722707.423581\n",
-      "\t reynolds number is : \t31455.9705947\n",
-      "\t hi is : Btu/(hr)*(ft**2)*(F) \t101.239669421\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t83.8842975207\n",
-      "\t tw is : F \t240.107773852\n",
-      "\t tf is : F \t185.053886926\n",
-      "\t Uc is : Btu/(hr)*(ft**2)*(F) \t53.7985865724\n",
-      "\t hd is : \t100.0\n",
-      "\t UD is : Btu/(hr)*(ft**2)*(F) \t34.9798966111\n",
-      "\t Area is : ft**2 \t1267.80895267\n",
-      "\t pipe length : \t58.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=675; # inlet hot fluid,F\n",
-    "T2=200; # outlet hot fluid,F\n",
-    "t1=120; # inlet cold fluid,F\n",
-    "t2=140; # outlet cold fluid,F\n",
-    "W=33100; # lb/hr\n",
-    "w=510000; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for oil \\t\"\n",
-    "c=0.64; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is : Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=230;\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, oil \\t\"\n",
-    "at=0.0458; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=5.56; # at 400F,lb/(ft)*(hr)\n",
-    "D=0.242; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "jH=100; # from fig.24\n",
-    "Z=0.245; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft), fig 16\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is : Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=2.9; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=150; # Btu/(hr)*(ft**2)\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is : F \\t\",tw\n",
-    "tf=(tw+tc)/2;\n",
-    "print\"\\t tf is : F \\t\",tf\n",
-    "delt=110; # F\n",
-    "d0=3.5; # in, fig 10.4\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is : \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is : ft**2 \\t\",A\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "L=(A/(a*24));\n",
-    "print\"\\t pipe length : \\t\",round(L)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.4 pgno:729"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for SO2 \t\n",
-      "\t total heat required for SO2 is :  Btu/hr \t166320.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t166500.0\n",
-      "\t delt1 is :  F \t65.0\n",
-      "\t delt2 is :  F \t350.0\n",
-      "\t LMTD is : F \t169.475824421\n",
-      "\t delt is :  F \t166.086307932\n",
-      "\t caloric temperature of hot fluid is :  F \t300.0\n",
-      "\t caloric temperature of cold fluid is :  \t92.5\n",
-      "\t hot fluid:inner tube side, SO2 \t\n",
-      "\t flow area is :  ft**2 \t0.0512\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t65625.0\n",
-      "\t reynolds number is :  \t409756.097561\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t21.0800390625\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t18.4781599554\n",
-      "\t cold fluid water \t\n",
-      "\t G :  lb/(hr)*(ft) \t693\n",
-      "\t Re is : \t1428.86597938\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t65.0\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t14.3879596501\n",
-      "\t hd is :  \t100.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t12.5782116353\n",
-      "\t Area is :  ft**2 \t78.10657332\n",
-      "\t pipe length :  \t8.75\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=3360; # lb/hr\n",
-    "w=11100; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for SO2 \\t\"\n",
-    "c=0.165; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for SO2 is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=20;\n",
-    "S=0.0412;\n",
-    "FT=0.98; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, SO2 \\t\"\n",
-    "at=0.0512; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.041; # at 300F,lb/(ft)*(hr), fig 15\n",
-    "D=0.256; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=790; # from fig.24\n",
-    "Z=0.006831; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft)\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=3.068; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid water \\t\"\n",
-    "L=8; # ft\n",
-    "G=(w/(2*L));\n",
-    "print\"\\t G :  lb/(hr)*(ft) \\t\",G\n",
-    "mu1=1.94; # at 92.5F, lb/(ft)*(hr)\n",
-    "Re=(4*G/mu1);\n",
-    "print\"\\t Re is : \\t\",Re\n",
-    "Do=0.292; # ft\n",
-    "ho=(65*(G/Do)**(1/3));\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A # calculation mistake in book\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "l=(A/(a*8))-1.9;\n",
-    "print\"\\t pipe length :  \\t\",round(l,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 20.5 pgno:736"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t evaporation percentage is :  \t0.121913091814\n",
-      "\t heat load is :  Btu/hr \t1917500\n",
-      "\t sensible heat is :  Btu/hr \t1687400.0\n",
-      "\t final spray temperature is :  F \t110.088095238\n",
-      "\t total spray :  lb/hr \t84000.0\n",
-      "\t m is :  lb/(hr)*(ft**2) \t875.0\n",
-      "\t Z is :  \t1.12568513365\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t316.940192565\n",
-      "\t tube side coefficient \t\n",
-      "\t assuming even number of passes and tube side velocity about 8fps \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1903225.80645\n",
-      "\t velocity is :  fps \t8.45878136201\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1861.8\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t270.83506906\n",
-      "\t total surface is :  ft**2 \t471.24\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t33.0\n",
-      "\t LMTD is : F \t36.4287504681\n",
-      "\t delt is :  F \t35.3358879541\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t115.153519517\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Nt=25.; # number of tubes\n",
-    "A=50.; # total projected area\n",
-    "Tav=100.; # F\n",
-    "s=28.; # assumption spray, lb/(min)*(ft**2)\n",
-    "Do=0.0833; # ft\n",
-    "PH=0.1562;\n",
-    "Y=0.874;\n",
-    "Z=0.466;\n",
-    "E=(0.171*(Do*Y*Z)**0.1); # (E/(Do*Y*Z)**0.1)=0.171, from fig 20.10\n",
-    "from math import log10\n",
-    "print\"\\t evaporation percentage is :  \\t\",E\n",
-    "Q=(295*500*(143-130));\n",
-    "print\"\\t heat load is :  Btu/hr \\t\",Q\n",
-    "Q1=(Q*(1-0.12));\n",
-    "print\"\\t sensible heat is :  Btu/hr \\t\",Q1\n",
-    "t2=(90)+(Q1/(28*60*50));\n",
-    "print\"\\t final spray temperature is :  F \\t\",t2\n",
-    "w=(s*60*50);\n",
-    "print\"\\t total spray :  lb/hr \\t\",w\n",
-    "m=(w/(2*4*12));\n",
-    "print\"\\t m is :  lb/(hr)*(ft**2) \\t\",m\n",
-    "mu=1.84; # lb/(ft)*(hr)\n",
-    "Z=((m**0.3)*Do*Y*Z/(mu*0.125));\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "N=3; # assume 3 horizontal rows\n",
-    "ho=300*(N**0.05); # (ho/(N**0.05))=300, from fig 20.11\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t tube side coefficient \\t\"\n",
-    "print\"\\t assuming even number of passes and tube side velocity about 8fps \\t\"\n",
-    "at=0.0775; # ft**2\n",
-    "Gt=(295*500/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "hi=2140; # Btu/(hr)*(ft**2)*(F), fig 25\n",
-    "ID=0.87; # ft\n",
-    "OD=1; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "a=0.2618; # ft**2, table 11\n",
-    "A1=(2*3*25*12*a);\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A1\n",
-    "T1=143; # inlet hot fluid,F\n",
-    "T2=130; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=110; # outlet cold fluid,F\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "delt1=40.;\n",
-    "delt2=33.;\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD # calculation mistake in book\n",
-    "R=0.65;\n",
-    "S=0.377;\n",
-    "FT=0.97; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "UD=(Q/(A1*(delt)));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.6 pgno:745"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t R is :  \t2.0\n",
-      "\t V is :  \t1.5\n",
-      "\t F is :  \t1\n",
-      "\t Z is :  \t0.733333333333\n",
-      "\t deltD is :  \t1.1745\n",
-      "\t delt is :  \t58.725\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t72.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=50.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "from math import log10\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "V=((T1+T2-t1-t2)/(t2-t1))/(2);\n",
-    "print\"\\t V is :  \\t\",V\n",
-    "u=120;\n",
-    "U=60;\n",
-    "F=((u*1)/(U*2));\n",
-    "print\"\\t F is :  \\t\",F\n",
-    "E=1.1; # In Fig.20.18b for R = 2.0and F = l.O,the abscissa and ordinate intersect at E =1.10.\n",
-    "Z=(E/V);\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "deltD=0.783*V; # deltD/V=0.783, from fig 20.17\n",
-    "print\"\\t deltD is :  \\t\",deltD\n",
-    "delt=(deltD*(t2-t1));\n",
-    "print\"\\t delt is :  \\t\",delt\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.7 pgno:752"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t beta is : \t0.0036\n",
-      "\t for sand \t\n",
-      "\t total heat required for sand is : Btu/hr \t36000.0\n",
-      "\t w is : lb/hr \t2000.0\n",
-      "\t R is : \t0.1\n",
-      "\t S is : \t0.909090909091\n",
-      "\t rate per tube is : lb/hr \t62.475\n",
-      "\t number of tubes : \t16.006402561\n",
-      "\t for air assume hoi=9 and Beta=0.2 \t\n",
-      "\t w1 is : lb/hr \t8000.0\n",
-      "\t rate per tube is : lb/hr \t39.0\n",
-      "\t number of tubes : \t25.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=284.; # inlet hot fluid,F\n",
-    "T2=104.; # outlet hot fluid,F\n",
-    "t1=86.; # inlet cold fluid,F\n",
-    "t2=104.; # outlet cold fluid,F\n",
-    "W=1000; # lb/hr\n",
-    "k=0.15; # thermal conductivity\n",
-    "L=10;\n",
-    "Beta=((2*k)/(500*(2./12.))); # hoi=500Btu/(hr)*(ft^2)*(F) for water\n",
-    "print\"\\t beta is : \\t\",Beta\n",
-    "print\"\\t for sand \\t\"\n",
-    "C=0.2; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for sand is : Btu/hr \\t\",Q\n",
-    "c=1;\n",
-    "w=(Q/(t2-t1));\n",
-    "print\"\\t w is : lb/hr \\t\",w\n",
-    "R=((W*C)/(w*c));\n",
-    "print\"\\t R is : \\t\",R\n",
-    "S=((T2-T1)/(t1-T1));\n",
-    "print\"\\t S is : \\t\",S\n",
-    "W1=(8.33*(k*L)/C); # ((W1*C)/(k*L))=8.33 from fig 20.20b for Beta=0\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",W1\n",
-    "N1=(W/W1);\n",
-    "print\"\\t number of tubes : \\t\",N1\n",
-    "print\"\\t for air assume hoi=9 and Beta=0.2 \\t\"\n",
-    "c1=0.25;\n",
-    "w1=(Q/(c1*(t2-t1)));\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "W2=(5.23*(k*L)/C); # ((W1*C)/(k*L))=5.23 from fig 20.20b for Beta=0.2\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",round(W2)\n",
-    "N2=(W/W2);\n",
-    "print\"\\t number of tubes : \\t\",round(N2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8a pgno758"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8a \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t Lb of water is :  lb \t375.0\n",
-      "\t heat to be supplied :  kwhr \t5.49531066823\n",
-      "\t losses \t\n",
-      "\t from surface of water :  kwhr \t1\n",
-      "\t from sides of vessel :  kwhr \t0.11\n",
-      "\t losses from bottom are negigible \t\n",
-      "\t total requirement :  kwhr \t6.60531066823\n",
-      "\t steady state \t\n",
-      "\t heat to be supplied :  kwhr \t1.9531066823\n",
-      "\t total requirement :  kwhr \t3.06\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8a \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "L=3; # ft\n",
-    "B=2; # ft\n",
-    "h=18/12; # ft , height of water present in tank\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*h*62.5);\n",
-    "print\"\\t Lb of water is :  lb \\t\",m\n",
-    "t1=50;\n",
-    "t2=150;\n",
-    "c=1;\n",
-    "Q=(m*c*(t2-t1))/(2*3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Q\n",
-    "print\"\\t losses \\t\"\n",
-    "Q1=(L*B*260)/(1000); # from fig 20.25c\n",
-    "print\"\\t from surface of water :  kwhr \\t\",Q1\n",
-    "Q2=(5.5*((2*B*2)+(2*L*B))/(1000)); # from fig 20.25c\n",
-    "print\"\\t from sides of vessel :  kwhr \\t\",Q2\n",
-    "print\"\\t losses from bottom are negigible \\t\"\n",
-    "Qt=(Q+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",Qt\n",
-    "print\"\\t steady state \\t\"\n",
-    "m1=8; # gal/hr\n",
-    "Qs=(m1*8.33*c*(t2-t1))/(3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Qs\n",
-    "Qts=(Qs+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",round(Qts,2)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8b pgno:760"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8b \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat to steel charge :  Btu \t3600.0\n",
-      "\t heat to air :  Btu \t540.0\n",
-      "\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \t\n",
-      "\t total requirement :  kw \t3.71\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8b \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=100; # lb\n",
-    "t1=70;\n",
-    "t2=370; \n",
-    "L=4;\n",
-    "B=3;\n",
-    "n=4; # number of air changers\n",
-    "c1=0.12\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat to steel charge :  Btu \\t\",Q1\n",
-    "c2=0.25\n",
-    "Q2=(n*L*B*2*0.075*c2*(t2-t1));\n",
-    "print\"\\t heat to air :  Btu \\t\",Q2\n",
-    "print\"\\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \\t\"\n",
-    "Qt=((Q1+Q2)/(3412))+(2.5)\n",
-    "print\"\\t total requirement :  kw \\t\",round(Qt,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8c pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8c \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat :  Btu \t15187.5\n",
-      "\t velocity is :  fps \t2.0\n",
-      "\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \t\n",
-      "\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8c \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=270; # cfm\n",
-    "t1=70;\n",
-    "t2=120; \n",
-    "L=1.5; # ft\n",
-    "B=1.5; # ft\n",
-    "c=0.25\n",
-    "row=0.075; # lb/ft^3\n",
-    "Q=(m*row*60*c*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q\n",
-    "V=(m/(L*B*60)); # fps\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "print\"\\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \\t\"\n",
-    "print\"\\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8d pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8d \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t weight of plate :  lb \t81.25\n",
-      "\t heat :  Btu \t2429.375\n",
-      "\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \t\n",
-      "\t radiation loss :  kw \t0.7722\n",
-      "\t total requirement :  kw \t1.48420908558\n",
-      "\t staedy state \t\n",
-      "\t heat :  Btu \t3542.0\n",
-      "\t total requirement :  kw \t1.83810082063\n",
-      "\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \t\n",
-      "\t delt is :  F \t264.0\n",
-      "\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8d \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=70;\n",
-    "t2=300; \n",
-    "L=26; # in\n",
-    "B=12; # in\n",
-    "H=1; # in\n",
-    "c1=0.13\n",
-    "# specific gravity of cast iron is 7.2\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*H*62.5*7.2/1728); # lb\n",
-    "print\"\\t weight of plate :  lb \\t\",m\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q1\n",
-    "print\"\\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \\t\"\n",
-    "Q2=(2*26*12*1.5*0.825/1000); # ke\n",
-    "print\"\\t radiation loss :  kw \\t\",Q2\n",
-    "Qt=((Q1)/(3412))+(Q2);\n",
-    "print\"\\t total requirement :  kw \\t\",Qt\n",
-    "print\"\\t staedy state \\t\"\n",
-    "m2=70;\n",
-    "c2=0.22;\n",
-    "Qs=(m2*c2*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Qs\n",
-    "Ql=0.8; # kw\n",
-    "Qts=((Qs)/(3412))+(Ql);\n",
-    "print\"\\t total requirement :  kw \\t\",Qts\n",
-    "print\"\\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \\t\"\n",
-    "delt=(16*16.5);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \\t\"\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_3.ipynb
deleted file mode 100755
index 417b7f25..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_20_Additoinal_Applications_3.ipynb
+++ /dev/null
@@ -1,886 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 20: Additoinal Applications"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.1 pgno:719"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 19,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t413.861386139\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t324.366270047\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t123.717442778\n",
-      "\t temperature difference is : F \t76.8232268984\n",
-      "\t temperature of the steam :  F \t221.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T=150; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1100; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=3.43; # ft**2\n",
-    "Q=32600;\n",
-    "delt=(Q/(UD*A));\n",
-    "print\"\\t temperature difference is : F \\t\",delt\n",
-    "Ts=(T+delt)-6;\n",
-    "print\"\\t temperature of the steam :  F \\t\",round(Ts)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.2 pgno:723"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 20,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t Rej is :  \t159198.113208\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t639.603960396\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t448.40351689\n",
-      "\t hd is :  \t200.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t138.310019983\n",
-      "\t Area is :  ft**2 \t3.36717676544\n",
-      "\t area per turn is :  ft**2 \t0.3288208\n",
-      "\t number of turns :  \t10.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=150; # F\n",
-    "T2=220; # F\n",
-    "L=0.6; # ft\n",
-    "N=7500; # rev/hr\n",
-    "row=62.5; # lb/ft**3\n",
-    "mu=1.06; # at 150 F and from fig 14, lb/ft*hr\n",
-    "k=0.38; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Rej=(L**2)*(N)*(row)/(mu);\n",
-    "print\"\\t Rej is :  \\t\",Rej\n",
-    "Z=1; # Z=(mu/muw)**(0.14), regarded as 1 for water\n",
-    "Dj=1.01; # ft, from table 11\n",
-    "j=1700; # fig 20.2\n",
-    "hi=((j)*(k/Dj)*((c*mu/k)**(1/3))*(Z)**(0.14));\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "hoi=1500; # Btu/(hr)*(ft**2)*(F)\n",
-    "Uc=((hi*hoi)/(hi+hoi)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.005;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Q=32600;\n",
-    "A=(Q/(UD*(T2-T1)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A\n",
-    "a=0.1309; # ft**2/ft\n",
-    "a1=(3.14*0.8*a);\n",
-    "print\"\\t area per turn is :  ft**2 \\t\",a1\n",
-    "n=(A/a1);\n",
-    "print\"\\t number of turns :  \\t\",round(n)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.3 pgno:725"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 21,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for oil \t\n",
-      "\t total heat required for oil is : Btu/hr \t10062400.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is : Btu/hr \t10200000\n",
-      "\t delt1 is : F \t80\n",
-      "\t delt2 is : F \t535\n",
-      "\t LMTD is  F \t230\n",
-      "\t caloric temperature of hot fluid is : F \t437\n",
-      "\t caloric temperature of cold fluid is : \t130\n",
-      "\t hot fluid:inner tube side, oil \t\n",
-      "\t flow area is : ft**2 \t0.0458\n",
-      "\t mass velocity is : lb/(hr)*(ft**2) \t722707.423581\n",
-      "\t reynolds number is : \t31455.9705947\n",
-      "\t hi is : Btu/(hr)*(ft**2)*(F) \t101.239669421\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t83.8842975207\n",
-      "\t tw is : F \t240.107773852\n",
-      "\t tf is : F \t185.053886926\n",
-      "\t Uc is : Btu/(hr)*(ft**2)*(F) \t53.7985865724\n",
-      "\t hd is : \t100.0\n",
-      "\t UD is : Btu/(hr)*(ft**2)*(F) \t34.9798966111\n",
-      "\t Area is : ft**2 \t1267.80895267\n",
-      "\t pipe length : \t58.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=675; # inlet hot fluid,F\n",
-    "T2=200; # outlet hot fluid,F\n",
-    "t1=120; # inlet cold fluid,F\n",
-    "t2=140; # outlet cold fluid,F\n",
-    "W=33100; # lb/hr\n",
-    "w=510000; # lb/hr\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for oil \\t\"\n",
-    "c=0.64; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is : Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is : F \\t\",delt1\n",
-    "print\"\\t delt2 is : F \\t\",delt2\n",
-    "LMTD=230;\n",
-    "print\"\\t LMTD is  F \\t\",LMTD\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, oil \\t\"\n",
-    "at=0.0458; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is : ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is : lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=5.56; # at 400F,lb/(ft)*(hr)\n",
-    "D=0.242; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \\t\",Ret\n",
-    "jH=100; # from fig.24\n",
-    "Z=0.245; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft), fig 16\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is : Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=2.9; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "ho=150; # Btu/(hr)*(ft**2)\n",
-    "tw=(tc)+(((hio)/(hio+ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is : F \\t\",tw\n",
-    "tf=(tw+tc)/2;\n",
-    "print\"\\t tf is : F \\t\",tf\n",
-    "delt=110; # F\n",
-    "d0=3.5; # in, fig 10.4\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is : Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is : \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is : Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is : ft**2 \\t\",A\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "L=(A/(a*24));\n",
-    "print\"\\t pipe length : \\t\",round(L)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.4 pgno:729"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 22,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.4 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for SO2 \t\n",
-      "\t total heat required for SO2 is :  Btu/hr \t166320.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t166500.0\n",
-      "\t delt1 is :  F \t65.0\n",
-      "\t delt2 is :  F \t350.0\n",
-      "\t LMTD is : F \t169.475824421\n",
-      "\t delt is :  F \t166.086307932\n",
-      "\t caloric temperature of hot fluid is :  F \t300.0\n",
-      "\t caloric temperature of cold fluid is :  \t92.5\n",
-      "\t hot fluid:inner tube side, SO2 \t\n",
-      "\t flow area is :  ft**2 \t0.0512\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t65625.0\n",
-      "\t reynolds number is :  \t409756.097561\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t21.0800390625\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t18.4781599554\n",
-      "\t cold fluid water \t\n",
-      "\t G :  lb/(hr)*(ft) \t693\n",
-      "\t Re is : \t1428.86597938\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t65.0\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t14.3879596501\n",
-      "\t hd is :  \t100.0\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t12.5782116353\n",
-      "\t Area is :  ft**2 \t78.10657332\n",
-      "\t pipe length :  \t8.75\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.4 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "W=3360; # lb/hr\n",
-    "w=11100; # lb/hr\n",
-    "from math import log10\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for SO2 \\t\"\n",
-    "c=0.165; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for SO2 is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=20;\n",
-    "S=0.0412;\n",
-    "FT=0.98; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/(2); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/(2); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  \\t\",tc\n",
-    "print\"\\t hot fluid:inner tube side, SO2 \\t\"\n",
-    "at=0.0512; # flow area, ft**2, table 11\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(W/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.041; # at 300F,lb/(ft)*(hr), fig 15\n",
-    "D=0.256; # ft, table 11\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=790; # from fig.24\n",
-    "Z=0.006831; # Z=(k(c*mu/k)**(1/3)), Btu/(hr)*(ft)*(F/ft)\n",
-    "hi=((jH)*(Z/D)); #Hi=(hi/phyp),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=3.068; # ft\n",
-    "OD=3.5; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "print\"\\t cold fluid water \\t\"\n",
-    "L=8; # ft\n",
-    "G=(w/(2*L));\n",
-    "print\"\\t G :  lb/(hr)*(ft) \\t\",G\n",
-    "mu1=1.94; # at 92.5F, lb/(ft)*(hr)\n",
-    "Re=(4*G/mu1);\n",
-    "print\"\\t Re is : \\t\",Re\n",
-    "Do=0.292; # ft\n",
-    "ho=(65*(G/Do)**(1/3));\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.01;\n",
-    "hd=(1/Rd);\n",
-    "print\"\\t hd is :  \\t\",hd\n",
-    "UD=((Uc*hd)/(Uc+hd));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=(Q/(UD*(LMTD)));\n",
-    "print\"\\t Area is :  ft**2 \\t\",A # calculation mistake in book\n",
-    "a=0.917; # ft**2/ft, table 11\n",
-    "l=(A/(a*8))-1.9;\n",
-    "print\"\\t pipe length :  \\t\",round(l,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Example 20.5 pgno:736"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 23,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t evaporation percentage is :  \t0.121913091814\n",
-      "\t heat load is :  Btu/hr \t1917500\n",
-      "\t sensible heat is :  Btu/hr \t1687400.0\n",
-      "\t final spray temperature is :  F \t110.088095238\n",
-      "\t total spray :  lb/hr \t84000.0\n",
-      "\t m is :  lb/(hr)*(ft**2) \t875.0\n",
-      "\t Z is :  \t1.12568513365\n",
-      "\t ho is :  Btu/(hr)*(ft**2)*(F) \t316.940192565\n",
-      "\t tube side coefficient \t\n",
-      "\t assuming even number of passes and tube side velocity about 8fps \t\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1903225.80645\n",
-      "\t velocity is :  fps \t8.45878136201\n",
-      "\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t1861.8\n",
-      "\t Uc is :  Btu/(hr)*(ft**2)*(F) \t270.83506906\n",
-      "\t total surface is :  ft**2 \t471.24\n",
-      "\t delt1 is :  F \t40.0\n",
-      "\t delt2 is :  F \t33.0\n",
-      "\t LMTD is : F \t36.4287504681\n",
-      "\t delt is :  F \t35.3358879541\n",
-      "\t UD is :  Btu/(hr)*(ft**2)*(F) \t115.153519517\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t0.005\n",
-      "\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "Nt=25.; # number of tubes\n",
-    "A=50.; # total projected area\n",
-    "Tav=100.; # F\n",
-    "s=28.; # assumption spray, lb/(min)*(ft**2)\n",
-    "Do=0.0833; # ft\n",
-    "PH=0.1562;\n",
-    "Y=0.874;\n",
-    "Z=0.466;\n",
-    "E=(0.171*(Do*Y*Z)**0.1); # (E/(Do*Y*Z)**0.1)=0.171, from fig 20.10\n",
-    "from math import log10\n",
-    "print\"\\t evaporation percentage is :  \\t\",E\n",
-    "Q=(295*500*(143-130));\n",
-    "print\"\\t heat load is :  Btu/hr \\t\",Q\n",
-    "Q1=(Q*(1-0.12));\n",
-    "print\"\\t sensible heat is :  Btu/hr \\t\",Q1\n",
-    "t2=(90)+(Q1/(28*60*50));\n",
-    "print\"\\t final spray temperature is :  F \\t\",t2\n",
-    "w=(s*60*50);\n",
-    "print\"\\t total spray :  lb/hr \\t\",w\n",
-    "m=(w/(2*4*12));\n",
-    "print\"\\t m is :  lb/(hr)*(ft**2) \\t\",m\n",
-    "mu=1.84; # lb/(ft)*(hr)\n",
-    "Z=((m**0.3)*Do*Y*Z/(mu*0.125));\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "N=3; # assume 3 horizontal rows\n",
-    "ho=300*(N**0.05); # (ho/(N**0.05))=300, from fig 20.11\n",
-    "print\"\\t ho is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t tube side coefficient \\t\"\n",
-    "print\"\\t assuming even number of passes and tube side velocity about 8fps \\t\"\n",
-    "at=0.0775; # ft**2\n",
-    "Gt=(295*500/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "hi=2140; # Btu/(hr)*(ft**2)*(F), fig 25\n",
-    "ID=0.87; # ft\n",
-    "OD=1; # ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hio to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((ho*hio)/(ho+hio)); # from eq 6.38\n",
-    "print\"\\t Uc is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "a=0.2618; # ft**2, table 11\n",
-    "A1=(2*3*25*12*a);\n",
-    "print\"\\t total surface is :  ft**2 \\t\",A1\n",
-    "T1=143; # inlet hot fluid,F\n",
-    "T2=130; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=110; # outlet cold fluid,F\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "delt1=40.;\n",
-    "delt2=33.;\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD # calculation mistake in book\n",
-    "R=0.65;\n",
-    "S=0.377;\n",
-    "FT=0.97; # fig 18\n",
-    "delt=(FT*LMTD);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "UD=(Q/(A1*(delt)));\n",
-    "print\"\\t UD is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",round(Rd,4)\n",
-    "print\"\\t The assumption of three horizontal rows is satisfactory, since a dirt factor of 0.004 was required \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.6 pgno:745"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 24,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.6 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t R is :  \t2.0\n",
-      "\t V is :  \t1.5\n",
-      "\t F is :  \t1\n",
-      "\t Z is :  \t0.733333333333\n",
-      "\t deltD is :  \t1.1745\n",
-      "\t delt is :  \t58.725\n",
-      "\t delt1 is :  F \t50.0\n",
-      "\t delt2 is :  F \t100.0\n",
-      "\t LMTD is : F \t72.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.6 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=200.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=50.; # inlet cold fluid,F\n",
-    "t2=100.; # outlet cold fluid,F\n",
-    "from math import log10\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "V=((T1+T2-t1-t2)/(t2-t1))/(2);\n",
-    "print\"\\t V is :  \\t\",V\n",
-    "u=120;\n",
-    "U=60;\n",
-    "F=((u*1)/(U*2));\n",
-    "print\"\\t F is :  \\t\",F\n",
-    "E=1.1; # In Fig.20.18b for R = 2.0and F = l.O,the abscissa and ordinate intersect at E =1.10.\n",
-    "Z=(E/V);\n",
-    "print\"\\t Z is :  \\t\",Z\n",
-    "deltD=0.783*V; # deltD/V=0.783, from fig 20.17\n",
-    "print\"\\t deltD is :  \\t\",deltD\n",
-    "delt=(deltD*(t2-t1));\n",
-    "print\"\\t delt is :  \\t\",delt\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log10(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.7 pgno:752"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.7 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t beta is : \t0.0036\n",
-      "\t for sand \t\n",
-      "\t total heat required for sand is : Btu/hr \t36000.0\n",
-      "\t w is : lb/hr \t2000.0\n",
-      "\t R is : \t0.1\n",
-      "\t S is : \t0.909090909091\n",
-      "\t rate per tube is : lb/hr \t62.475\n",
-      "\t number of tubes : \t16.006402561\n",
-      "\t for air assume hoi=9 and Beta=0.2 \t\n",
-      "\t w1 is : lb/hr \t8000.0\n",
-      "\t rate per tube is : lb/hr \t39.0\n",
-      "\t number of tubes : \t25.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.7 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=284.; # inlet hot fluid,F\n",
-    "T2=104.; # outlet hot fluid,F\n",
-    "t1=86.; # inlet cold fluid,F\n",
-    "t2=104.; # outlet cold fluid,F\n",
-    "W=1000; # lb/hr\n",
-    "k=0.15; # thermal conductivity\n",
-    "L=10;\n",
-    "Beta=((2*k)/(500*(2./12.))); # hoi=500Btu/(hr)*(ft^2)*(F) for water\n",
-    "print\"\\t beta is : \\t\",Beta\n",
-    "print\"\\t for sand \\t\"\n",
-    "C=0.2; # Btu/(lb)*(F)\n",
-    "Q=((W)*(C)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for sand is : Btu/hr \\t\",Q\n",
-    "c=1;\n",
-    "w=(Q/(t2-t1));\n",
-    "print\"\\t w is : lb/hr \\t\",w\n",
-    "R=((W*C)/(w*c));\n",
-    "print\"\\t R is : \\t\",R\n",
-    "S=((T2-T1)/(t1-T1));\n",
-    "print\"\\t S is : \\t\",S\n",
-    "W1=(8.33*(k*L)/C); # ((W1*C)/(k*L))=8.33 from fig 20.20b for Beta=0\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",W1\n",
-    "N1=(W/W1);\n",
-    "print\"\\t number of tubes : \\t\",N1\n",
-    "print\"\\t for air assume hoi=9 and Beta=0.2 \\t\"\n",
-    "c1=0.25;\n",
-    "w1=(Q/(c1*(t2-t1)));\n",
-    "print\"\\t w1 is : lb/hr \\t\",w1\n",
-    "W2=(5.23*(k*L)/C); # ((W1*C)/(k*L))=5.23 from fig 20.20b for Beta=0.2\n",
-    "print\"\\t rate per tube is : lb/hr \\t\",round(W2)\n",
-    "N2=(W/W2);\n",
-    "print\"\\t number of tubes : \\t\",round(N2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8a pgno758"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8a \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t Lb of water is :  lb \t375.0\n",
-      "\t heat to be supplied :  kwhr \t5.49531066823\n",
-      "\t losses \t\n",
-      "\t from surface of water :  kwhr \t1\n",
-      "\t from sides of vessel :  kwhr \t0.11\n",
-      "\t losses from bottom are negigible \t\n",
-      "\t total requirement :  kwhr \t6.60531066823\n",
-      "\t steady state \t\n",
-      "\t heat to be supplied :  kwhr \t1.9531066823\n",
-      "\t total requirement :  kwhr \t3.06\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8a \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "L=3; # ft\n",
-    "B=2; # ft\n",
-    "h=18/12; # ft , height of water present in tank\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*h*62.5);\n",
-    "print\"\\t Lb of water is :  lb \\t\",m\n",
-    "t1=50;\n",
-    "t2=150;\n",
-    "c=1;\n",
-    "Q=(m*c*(t2-t1))/(2*3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Q\n",
-    "print\"\\t losses \\t\"\n",
-    "Q1=(L*B*260)/(1000); # from fig 20.25c\n",
-    "print\"\\t from surface of water :  kwhr \\t\",Q1\n",
-    "Q2=(5.5*((2*B*2)+(2*L*B))/(1000)); # from fig 20.25c\n",
-    "print\"\\t from sides of vessel :  kwhr \\t\",Q2\n",
-    "print\"\\t losses from bottom are negigible \\t\"\n",
-    "Qt=(Q+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",Qt\n",
-    "print\"\\t steady state \\t\"\n",
-    "m1=8; # gal/hr\n",
-    "Qs=(m1*8.33*c*(t2-t1))/(3412); # kwhr\n",
-    "print\"\\t heat to be supplied :  kwhr \\t\",Qs\n",
-    "Qts=(Qs+Q1+Q2);\n",
-    "print\"\\t total requirement :  kwhr \\t\",round(Qts,2)\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8b pgno:760"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8b \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat to steel charge :  Btu \t3600.0\n",
-      "\t heat to air :  Btu \t540.0\n",
-      "\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \t\n",
-      "\t total requirement :  kw \t3.71\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8b \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=100; # lb\n",
-    "t1=70;\n",
-    "t2=370; \n",
-    "L=4;\n",
-    "B=3;\n",
-    "n=4; # number of air changers\n",
-    "c1=0.12\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat to steel charge :  Btu \\t\",Q1\n",
-    "c2=0.25\n",
-    "Q2=(n*L*B*2*0.075*c2*(t2-t1));\n",
-    "print\"\\t heat to air :  Btu \\t\",Q2\n",
-    "print\"\\t From Fig. 20.25a for 52ft^2 of oven outside surface and a temperature rise of 300F the loss is 5kw for 1 in.thick insulations.For 2 in.thick insulation the loss is 2.5kw \\t\"\n",
-    "Qt=((Q1+Q2)/(3412))+(2.5)\n",
-    "print\"\\t total requirement :  kw \\t\",round(Qt,2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8c pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8c \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t heat :  Btu \t15187.5\n",
-      "\t velocity is :  fps \t2.0\n",
-      "\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \t\n",
-      "\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8c \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "m=270; # cfm\n",
-    "t1=70;\n",
-    "t2=120; \n",
-    "L=1.5; # ft\n",
-    "B=1.5; # ft\n",
-    "c=0.25\n",
-    "row=0.075; # lb/ft^3\n",
-    "Q=(m*row*60*c*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q\n",
-    "V=(m/(L*B*60)); # fps\n",
-    "print\"\\t velocity is :  fps \\t\",V\n",
-    "print\"\\t Refer to Fig.20.22a.The air is capable of removing 33watts/in which is the maximum dissipation which may be expected. Any group of heaters providing 5 kw which do not require a dissipation of more than 33 w/in. and which will fit into the duct will be satisfactory \\t\"\n",
-    "print\"\\t Thus in Table 20.3 elements of 350 watts with a total length each of 18 in. each are satisfactory \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 20.8d pgno:762"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 20.8d \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t unsteady state \t\n",
-      "\t weight of plate :  lb \t81.25\n",
-      "\t heat :  Btu \t2429.375\n",
-      "\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \t\n",
-      "\t radiation loss :  kw \t0.7722\n",
-      "\t total requirement :  kw \t1.48420908558\n",
-      "\t staedy state \t\n",
-      "\t heat :  Btu \t3542.0\n",
-      "\t total requirement :  kw \t1.83810082063\n",
-      "\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \t\n",
-      "\t delt is :  F \t264.0\n",
-      "\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 20.8d \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "t1=70;\n",
-    "t2=300; \n",
-    "L=26; # in\n",
-    "B=12; # in\n",
-    "H=1; # in\n",
-    "c1=0.13\n",
-    "# specific gravity of cast iron is 7.2\n",
-    "print\"\\t unsteady state \\t\"\n",
-    "m=(L*B*H*62.5*7.2/1728); # lb\n",
-    "print\"\\t weight of plate :  lb \\t\",m\n",
-    "Q1=(m*c1*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Q1\n",
-    "print\"\\t From Figure 20.25b for a black body the radiation is 1.5w/in^2.The radiation from the top is actually 110 per cent of this value, and from the bottom of the plate it is 55 per cent for an average of 82.5 per cent is taken \\t\"\n",
-    "Q2=(2*26*12*1.5*0.825/1000); # ke\n",
-    "print\"\\t radiation loss :  kw \\t\",Q2\n",
-    "Qt=((Q1)/(3412))+(Q2);\n",
-    "print\"\\t total requirement :  kw \\t\",Qt\n",
-    "print\"\\t staedy state \\t\"\n",
-    "m2=70;\n",
-    "c2=0.22;\n",
-    "Qs=(m2*c2*(t2-t1));\n",
-    "print\"\\t heat :  Btu \\t\",Qs\n",
-    "Ql=0.8; # kw\n",
-    "Qts=((Qs)/(3412))+(Ql);\n",
-    "print\"\\t total requirement :  kw \\t\",Qts\n",
-    "print\"\\t The steady state is controlling.The requirements are satisfied, by four 24-in. strip heaters, but the sheath temperature must now be checked. Since the temperature drop per unit flux density is 14 to 19F, assume an average of 16.5DegF. For clamp-on strips 24 in. long the watts per square inch deliverable are 16 \\t\"\n",
-    "delt=(16*16.5);\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "print\"\\t The sheath temperature is then 300 + 264 = 564DegF, which is satisfactory for steel sheathed elements with a 750F maximum. \\t\"\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction.ipynb
deleted file mode 100755
index 8bc5413c..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction.ipynb
+++ /dev/null
@@ -1,281 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 2:CONDUCTION"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.1 pg:13"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      " heat is  Btu/hr  69120.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "Tavg=900; # average temperature of the wall,F\n",
-    "k=0.15; # Thermal conductivity at 932 F,Btu/(hr)(ft^2)(F/ft)\n",
-    "T1=1500; # hot side temperature,F\n",
-    "T2=300; # cold side temperature,F\n",
-    "A=192; # surface area,ft^2\n",
-    "L=0.5; # thickness,ft\n",
-    "#solution\n",
-    "Q=(k)*(A)*(T1-T2)/L; # formula for heat,Btu/hr\n",
-    "print \" heat is  Btu/hr \",Q\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.2 pg:14"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t resistance offered by firebrick :  (hr)*(F)/Btu  0.97\n",
-      "\t resistance offered by insulating brick : (hr)*(F)/Btu  2.2\n",
-      "\t resistance offered by buildingbrick : (hr)*(F)/Btu  1.25\n",
-      "\t total resistance offered by three walls : (hr)*(F)/Btu  4.42\n",
-      "\t heat loss/ft^2 :  Btu/hr  331.0\n",
-      "\t delta is : F  322.0\n",
-      "\t temperature at interface of firebrick and insulating brick  F  1278.0\n",
-      "\t deltb is :  F  729.0\n",
-      "\t temperature at interface of insulating brick and building brick  F  549.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "La=0.66; # Thickness of firebrick wall,ft\n",
-    "Lb=0.33; # Thickness of insulating brick wall,ft\n",
-    "Lc=0.5; # Thickness of building brick wall,ft\n",
-    "Ka=0.68; # themal conductivity of firebrick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kb=0.15; # themal conductivity of insulating brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kc=0.40; # themal conductivity of building brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "A=1.; # surface area,ft^2\n",
-    "Ta=1600.; # temperature of inner wall,F\n",
-    "Tb=125.; # temperature of outer wall.F\n",
-    "#solution\n",
-    "Ra=La/(Ka)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by firebrick :  (hr)*(F)/Btu \",round(Ra,2)\n",
-    "Rb=Lb/(Kb)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by insulating brick : (hr)*(F)/Btu \",round(Rb,2)\n",
-    "Rc=Lc/(Kc)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by buildingbrick : (hr)*(F)/Btu \",round(Rc,2)\n",
-    "R=Ra+Rb+Rc; # total resistance offered by three walls,(hr)*(F)/Btu\n",
-    "print\"\\t total resistance offered by three walls : (hr)*(F)/Btu \",round(R,2)\n",
-    "Q=(1600-125)/4.45; # using formula for heat loss/ft^2,Btu/hr\n",
-    "print\"\\t heat loss/ft^2 :  Btu/hr \",round(Q,0)\n",
-    "# T1,T2 are temperatures at interface of firebrick and insulating brick, and insulating brick and building brick respectively,F\n",
-    "delta=(Q)*(Ra); # formula for temperature difference,F\n",
-    "print\"\\t delta is : F \",round(delta,0)\n",
-    "T1=Ta-((Q)*(Ra)); # temperature at interface of firebrick and insulating brick,F\n",
-    "print\"\\t temperature at interface of firebrick and insulating brick  F \",round(T1,0)\n",
-    "deltb=Q*(Rb);\n",
-    "print\"\\t deltb is :  F \",round(deltb,0)\n",
-    "T2=T1-((Q)*(Rb)); #temperature at interface of insulating brick and building brick,F\n",
-    "print\"\\t temperature at interface of insulating brick and building brick  F \",round(T2,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.3 pg:15"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t resistance offered by air film (hr)(F)/Btu  0.79\n",
-      "\t total resistance  (hr)(F)/Btu  5.24\n",
-      "\t heat loss  Btu/hr  282.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "Lair=0.25/12; # thickness of air film,ft\n",
-    "Kair=0.0265; # thermal conductivity of air at 572F,Btu/(hr)*(ft^2)(F/ft)\n",
-    "A=1; # surface area,ft^2\n",
-    "#solution\n",
-    "Rair=Lair/(Kair*(A)); # resistance offered by air film, (hr)(F)/Btu\n",
-    "print\"\\t resistance offered by air film (hr)(F)/Btu \",round(Rair,2)\n",
-    "R=4.45; # resistance from previous example 2.2,(hr)(F)/Btu\n",
-    "Rt=(R)+Rair; # total resistance,(hr)(F)/Btu\n",
-    "print\"\\t total resistance  (hr)(F)/Btu \",round(Rt,2)\n",
-    "Ta=1600; # temperature of inner wall,F\n",
-    "Tb=125; # temperature of outer wall,F\n",
-    "Q=(1600-125)/Rt; # heat loss, Btu/hr\n",
-    "print\"\\t heat loss  Btu/hr \",round(Q,0)\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.4 pg 16"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": [
-    "\n",
-    "#given\n",
-    "k=0.63; # thermal conductivity of pipe, Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Do=6. # in\n",
-    "Di=5. # in\n",
-    "Ti=200.;# inner side temperature,F\n",
-    "To=175.; # outer side temperature,F\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(2*(3.14)*(k)*(Ti-To))/(log (Do/Di)); # formula for heat flow,Btu/(hr)*(ft)\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft) \",round(q,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "# caculation mistake in book\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "##Example2.5 pg 19"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft)  104.4\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is :  F  122.300238658\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft) 102.9\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is : F  125.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "t1=150; # assume temperature of outer surface of rockwool,F\n",
-    "ta=70; # temperature of surrounding air,F\n",
-    "ha=2.23; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(3.14)*(300-70)/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.23)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft), calculation mistake\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft) \",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((104.8)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=125; # assume temperature of outer surface of rockwool,F\n",
-    "ha=2.10; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "q=((3.14)*(300-70))/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.10)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft)\",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((103)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is : F \",round(t1,1)\n",
-    "# end \n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_1.ipynb
deleted file mode 100755
index d13df346..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_1.ipynb
+++ /dev/null
@@ -1,282 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 2:CONDUCTION"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.1 pg:13"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      " heat is  Btu/hr  69120.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "Tavg=900; # average temperature of the wall,F\n",
-    "k=0.15; # Thermal conductivity at 932 F,Btu/(hr)(ft^2)(F/ft)\n",
-    "T1=1500; # hot side temperature,F\n",
-    "T2=300; # cold side temperature,F\n",
-    "A=192; # surface area,ft^2\n",
-    "L=0.5; # thickness,ft\n",
-    "#solution\n",
-    "Q=(k)*(A)*(T1-T2)/L; # formula for heat,Btu/hr\n",
-    "print \" heat is  Btu/hr \",Q\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.2 pg:14"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t resistance offered by firebrick :  (hr)*(F)/Btu  0.97\n",
-      "\t resistance offered by insulating brick : (hr)*(F)/Btu  2.2\n",
-      "\t resistance offered by buildingbrick : (hr)*(F)/Btu  1.25\n",
-      "\t total resistance offered by three walls : (hr)*(F)/Btu  4.42\n",
-      "\t heat loss/ft^2 :  Btu/hr  331.0\n",
-      "\t delta is : F  322.0\n",
-      "\t temperature at interface of firebrick and insulating brick  F  1278.0\n",
-      "\t deltb is :  F  729.0\n",
-      "\t temperature at interface of insulating brick and building brick  F  549.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "La=0.66; # Thickness of firebrick wall,ft\n",
-    "Lb=0.33; # Thickness of insulating brick wall,ft\n",
-    "Lc=0.5; # Thickness of building brick wall,ft\n",
-    "Ka=0.68; # themal conductivity of firebrick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kb=0.15; # themal conductivity of insulating brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kc=0.40; # themal conductivity of building brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "A=1.; # surface area,ft^2\n",
-    "Ta=1600.; # temperature of inner wall,F\n",
-    "Tb=125.; # temperature of outer wall.F\n",
-    "#solution\n",
-    "Ra=La/(Ka)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by firebrick :  (hr)*(F)/Btu \",round(Ra,2)\n",
-    "Rb=Lb/(Kb)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by insulating brick : (hr)*(F)/Btu \",round(Rb,2)\n",
-    "Rc=Lc/(Kc)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by buildingbrick : (hr)*(F)/Btu \",round(Rc,2)\n",
-    "R=Ra+Rb+Rc; # total resistance offered by three walls,(hr)*(F)/Btu\n",
-    "print\"\\t total resistance offered by three walls : (hr)*(F)/Btu \",round(R,2)\n",
-    "Q=(1600-125)/4.45; # using formula for heat loss/ft^2,Btu/hr\n",
-    "print\"\\t heat loss/ft^2 :  Btu/hr \",round(Q,0)\n",
-    "# T1,T2 are temperatures at interface of firebrick and insulating brick, and insulating brick and building brick respectively,F\n",
-    "delta=(Q)*(Ra); # formula for temperature difference,F\n",
-    "print\"\\t delta is : F \",round(delta,0)\n",
-    "T1=Ta-((Q)*(Ra)); # temperature at interface of firebrick and insulating brick,F\n",
-    "print\"\\t temperature at interface of firebrick and insulating brick  F \",round(T1,0)\n",
-    "deltb=Q*(Rb);\n",
-    "print\"\\t deltb is :  F \",round(deltb,0)\n",
-    "T2=T1-((Q)*(Rb)); #temperature at interface of insulating brick and building brick,F\n",
-    "print\"\\t temperature at interface of insulating brick and building brick  F \",round(T2,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.3 pg:15"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t resistance offered by air film (hr)(F)/Btu  0.79\n",
-      "\t total resistance  (hr)(F)/Btu  5.24\n",
-      "\t heat loss  Btu/hr  282.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "Lair=0.25/12; # thickness of air film,ft\n",
-    "Kair=0.0265; # thermal conductivity of air at 572F,Btu/(hr)*(ft^2)(F/ft)\n",
-    "A=1; # surface area,ft^2\n",
-    "#solution\n",
-    "Rair=Lair/(Kair*(A)); # resistance offered by air film, (hr)(F)/Btu\n",
-    "print\"\\t resistance offered by air film (hr)(F)/Btu \",round(Rair,2)\n",
-    "R=4.45; # resistance from previous example 2.2,(hr)(F)/Btu\n",
-    "Rt=(R)+Rair; # total resistance,(hr)(F)/Btu\n",
-    "print\"\\t total resistance  (hr)(F)/Btu \",round(Rt,2)\n",
-    "Ta=1600; # temperature of inner wall,F\n",
-    "Tb=125; # temperature of outer wall,F\n",
-    "Q=(1600-125)/Rt; # heat loss, Btu/hr\n",
-    "print\"\\t heat loss  Btu/hr \",round(Q,0)\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.4 pg 16"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t heat flow is :  Btu/(hr)*(ft)  543.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "k=0.63; # thermal conductivity of pipe, Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Do=6. # in\n",
-    "Di=5. # in\n",
-    "Ti=200.;# inner side temperature,F\n",
-    "To=175.; # outer side temperature,F\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(2*(3.14)*(k)*(Ti-To))/(log (Do/Di)); # formula for heat flow,Btu/(hr)*(ft)\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft) \",round(q,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "# caculation mistake in book\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "##Example2.5 pg 19"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft)  104.4\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is :  F  122.300238658\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft) 102.9\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is : F  125.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "t1=150; # assume temperature of outer surface of rockwool,F\n",
-    "ta=70; # temperature of surrounding air,F\n",
-    "ha=2.23; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(3.14)*(300-70)/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.23)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft), calculation mistake\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft) \",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((104.8)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=125; # assume temperature of outer surface of rockwool,F\n",
-    "ha=2.10; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "q=((3.14)*(300-70))/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.10)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft)\",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((103)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is : F \",round(t1,1)\n",
-    "# end \n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_2.ipynb
deleted file mode 100755
index d13df346..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_2.ipynb
+++ /dev/null
@@ -1,282 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 2:CONDUCTION"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.1 pg:13"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      " heat is  Btu/hr  69120.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "Tavg=900; # average temperature of the wall,F\n",
-    "k=0.15; # Thermal conductivity at 932 F,Btu/(hr)(ft^2)(F/ft)\n",
-    "T1=1500; # hot side temperature,F\n",
-    "T2=300; # cold side temperature,F\n",
-    "A=192; # surface area,ft^2\n",
-    "L=0.5; # thickness,ft\n",
-    "#solution\n",
-    "Q=(k)*(A)*(T1-T2)/L; # formula for heat,Btu/hr\n",
-    "print \" heat is  Btu/hr \",Q\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.2 pg:14"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t resistance offered by firebrick :  (hr)*(F)/Btu  0.97\n",
-      "\t resistance offered by insulating brick : (hr)*(F)/Btu  2.2\n",
-      "\t resistance offered by buildingbrick : (hr)*(F)/Btu  1.25\n",
-      "\t total resistance offered by three walls : (hr)*(F)/Btu  4.42\n",
-      "\t heat loss/ft^2 :  Btu/hr  331.0\n",
-      "\t delta is : F  322.0\n",
-      "\t temperature at interface of firebrick and insulating brick  F  1278.0\n",
-      "\t deltb is :  F  729.0\n",
-      "\t temperature at interface of insulating brick and building brick  F  549.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "La=0.66; # Thickness of firebrick wall,ft\n",
-    "Lb=0.33; # Thickness of insulating brick wall,ft\n",
-    "Lc=0.5; # Thickness of building brick wall,ft\n",
-    "Ka=0.68; # themal conductivity of firebrick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kb=0.15; # themal conductivity of insulating brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kc=0.40; # themal conductivity of building brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "A=1.; # surface area,ft^2\n",
-    "Ta=1600.; # temperature of inner wall,F\n",
-    "Tb=125.; # temperature of outer wall.F\n",
-    "#solution\n",
-    "Ra=La/(Ka)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by firebrick :  (hr)*(F)/Btu \",round(Ra,2)\n",
-    "Rb=Lb/(Kb)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by insulating brick : (hr)*(F)/Btu \",round(Rb,2)\n",
-    "Rc=Lc/(Kc)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by buildingbrick : (hr)*(F)/Btu \",round(Rc,2)\n",
-    "R=Ra+Rb+Rc; # total resistance offered by three walls,(hr)*(F)/Btu\n",
-    "print\"\\t total resistance offered by three walls : (hr)*(F)/Btu \",round(R,2)\n",
-    "Q=(1600-125)/4.45; # using formula for heat loss/ft^2,Btu/hr\n",
-    "print\"\\t heat loss/ft^2 :  Btu/hr \",round(Q,0)\n",
-    "# T1,T2 are temperatures at interface of firebrick and insulating brick, and insulating brick and building brick respectively,F\n",
-    "delta=(Q)*(Ra); # formula for temperature difference,F\n",
-    "print\"\\t delta is : F \",round(delta,0)\n",
-    "T1=Ta-((Q)*(Ra)); # temperature at interface of firebrick and insulating brick,F\n",
-    "print\"\\t temperature at interface of firebrick and insulating brick  F \",round(T1,0)\n",
-    "deltb=Q*(Rb);\n",
-    "print\"\\t deltb is :  F \",round(deltb,0)\n",
-    "T2=T1-((Q)*(Rb)); #temperature at interface of insulating brick and building brick,F\n",
-    "print\"\\t temperature at interface of insulating brick and building brick  F \",round(T2,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.3 pg:15"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t resistance offered by air film (hr)(F)/Btu  0.79\n",
-      "\t total resistance  (hr)(F)/Btu  5.24\n",
-      "\t heat loss  Btu/hr  282.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "Lair=0.25/12; # thickness of air film,ft\n",
-    "Kair=0.0265; # thermal conductivity of air at 572F,Btu/(hr)*(ft^2)(F/ft)\n",
-    "A=1; # surface area,ft^2\n",
-    "#solution\n",
-    "Rair=Lair/(Kair*(A)); # resistance offered by air film, (hr)(F)/Btu\n",
-    "print\"\\t resistance offered by air film (hr)(F)/Btu \",round(Rair,2)\n",
-    "R=4.45; # resistance from previous example 2.2,(hr)(F)/Btu\n",
-    "Rt=(R)+Rair; # total resistance,(hr)(F)/Btu\n",
-    "print\"\\t total resistance  (hr)(F)/Btu \",round(Rt,2)\n",
-    "Ta=1600; # temperature of inner wall,F\n",
-    "Tb=125; # temperature of outer wall,F\n",
-    "Q=(1600-125)/Rt; # heat loss, Btu/hr\n",
-    "print\"\\t heat loss  Btu/hr \",round(Q,0)\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.4 pg 16"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t heat flow is :  Btu/(hr)*(ft)  543.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "k=0.63; # thermal conductivity of pipe, Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Do=6. # in\n",
-    "Di=5. # in\n",
-    "Ti=200.;# inner side temperature,F\n",
-    "To=175.; # outer side temperature,F\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(2*(3.14)*(k)*(Ti-To))/(log (Do/Di)); # formula for heat flow,Btu/(hr)*(ft)\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft) \",round(q,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "# caculation mistake in book\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "##Example2.5 pg 19"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft)  104.4\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is :  F  122.300238658\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft) 102.9\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is : F  125.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "t1=150; # assume temperature of outer surface of rockwool,F\n",
-    "ta=70; # temperature of surrounding air,F\n",
-    "ha=2.23; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(3.14)*(300-70)/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.23)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft), calculation mistake\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft) \",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((104.8)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=125; # assume temperature of outer surface of rockwool,F\n",
-    "ha=2.10; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "q=((3.14)*(300-70))/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.10)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft)\",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((103)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is : F \",round(t1,1)\n",
-    "# end \n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_3.ipynb
deleted file mode 100755
index d13df346..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_2_Conduction_3.ipynb
+++ /dev/null
@@ -1,282 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 2:CONDUCTION"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.1 pg:13"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      " heat is  Btu/hr  69120.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "Tavg=900; # average temperature of the wall,F\n",
-    "k=0.15; # Thermal conductivity at 932 F,Btu/(hr)(ft^2)(F/ft)\n",
-    "T1=1500; # hot side temperature,F\n",
-    "T2=300; # cold side temperature,F\n",
-    "A=192; # surface area,ft^2\n",
-    "L=0.5; # thickness,ft\n",
-    "#solution\n",
-    "Q=(k)*(A)*(T1-T2)/L; # formula for heat,Btu/hr\n",
-    "print \" heat is  Btu/hr \",Q\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.2 pg:14"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t resistance offered by firebrick :  (hr)*(F)/Btu  0.97\n",
-      "\t resistance offered by insulating brick : (hr)*(F)/Btu  2.2\n",
-      "\t resistance offered by buildingbrick : (hr)*(F)/Btu  1.25\n",
-      "\t total resistance offered by three walls : (hr)*(F)/Btu  4.42\n",
-      "\t heat loss/ft^2 :  Btu/hr  331.0\n",
-      "\t delta is : F  322.0\n",
-      "\t temperature at interface of firebrick and insulating brick  F  1278.0\n",
-      "\t deltb is :  F  729.0\n",
-      "\t temperature at interface of insulating brick and building brick  F  549.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "La=0.66; # Thickness of firebrick wall,ft\n",
-    "Lb=0.33; # Thickness of insulating brick wall,ft\n",
-    "Lc=0.5; # Thickness of building brick wall,ft\n",
-    "Ka=0.68; # themal conductivity of firebrick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kb=0.15; # themal conductivity of insulating brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Kc=0.40; # themal conductivity of building brick,Btu/(hr)*(ft^2)*(F/ft)\n",
-    "A=1.; # surface area,ft^2\n",
-    "Ta=1600.; # temperature of inner wall,F\n",
-    "Tb=125.; # temperature of outer wall.F\n",
-    "#solution\n",
-    "Ra=La/(Ka)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by firebrick :  (hr)*(F)/Btu \",round(Ra,2)\n",
-    "Rb=Lb/(Kb)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by insulating brick : (hr)*(F)/Btu \",round(Rb,2)\n",
-    "Rc=Lc/(Kc)*(A); # formula for resistance,(hr)*(F)/Btu\n",
-    "print\"\\t resistance offered by buildingbrick : (hr)*(F)/Btu \",round(Rc,2)\n",
-    "R=Ra+Rb+Rc; # total resistance offered by three walls,(hr)*(F)/Btu\n",
-    "print\"\\t total resistance offered by three walls : (hr)*(F)/Btu \",round(R,2)\n",
-    "Q=(1600-125)/4.45; # using formula for heat loss/ft^2,Btu/hr\n",
-    "print\"\\t heat loss/ft^2 :  Btu/hr \",round(Q,0)\n",
-    "# T1,T2 are temperatures at interface of firebrick and insulating brick, and insulating brick and building brick respectively,F\n",
-    "delta=(Q)*(Ra); # formula for temperature difference,F\n",
-    "print\"\\t delta is : F \",round(delta,0)\n",
-    "T1=Ta-((Q)*(Ra)); # temperature at interface of firebrick and insulating brick,F\n",
-    "print\"\\t temperature at interface of firebrick and insulating brick  F \",round(T1,0)\n",
-    "deltb=Q*(Rb);\n",
-    "print\"\\t deltb is :  F \",round(deltb,0)\n",
-    "T2=T1-((Q)*(Rb)); #temperature at interface of insulating brick and building brick,F\n",
-    "print\"\\t temperature at interface of insulating brick and building brick  F \",round(T2,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.3 pg:15"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t resistance offered by air film (hr)(F)/Btu  0.79\n",
-      "\t total resistance  (hr)(F)/Btu  5.24\n",
-      "\t heat loss  Btu/hr  282.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "Lair=0.25/12; # thickness of air film,ft\n",
-    "Kair=0.0265; # thermal conductivity of air at 572F,Btu/(hr)*(ft^2)(F/ft)\n",
-    "A=1; # surface area,ft^2\n",
-    "#solution\n",
-    "Rair=Lair/(Kair*(A)); # resistance offered by air film, (hr)(F)/Btu\n",
-    "print\"\\t resistance offered by air film (hr)(F)/Btu \",round(Rair,2)\n",
-    "R=4.45; # resistance from previous example 2.2,(hr)(F)/Btu\n",
-    "Rt=(R)+Rair; # total resistance,(hr)(F)/Btu\n",
-    "print\"\\t total resistance  (hr)(F)/Btu \",round(Rt,2)\n",
-    "Ta=1600; # temperature of inner wall,F\n",
-    "Tb=125; # temperature of outer wall,F\n",
-    "Q=(1600-125)/Rt; # heat loss, Btu/hr\n",
-    "print\"\\t heat loss  Btu/hr \",round(Q,0)\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example2.4 pg 16"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t heat flow is :  Btu/(hr)*(ft)  543.0\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "k=0.63; # thermal conductivity of pipe, Btu/(hr)*(ft^2)*(F/ft)\n",
-    "Do=6. # in\n",
-    "Di=5. # in\n",
-    "Ti=200.;# inner side temperature,F\n",
-    "To=175.; # outer side temperature,F\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(2*(3.14)*(k)*(Ti-To))/(log (Do/Di)); # formula for heat flow,Btu/(hr)*(ft)\n",
-    "print\"\\t heat flow is :  Btu/(hr)*(ft) \",round(q,0)\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "# caculation mistake in book\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "##Example2.5 pg 19"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft)  104.4\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is :  F  122.300238658\n",
-      "\t heat loss for linear foot is :  Btu/(hr)*(lin ft) 102.9\n",
-      "\t Check between ts and t1, since delt/R = deltc/Rc \n",
-      "\t t1 is : F  125.4\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "t1=150; # assume temperature of outer surface of rockwool,F\n",
-    "ta=70; # temperature of surrounding air,F\n",
-    "ha=2.23; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "#solution\n",
-    "import math\n",
-    "from math import log\n",
-    "q=(3.14)*(300-70)/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.23)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft), calculation mistake\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft) \",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((104.8)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=125; # assume temperature of outer surface of rockwool,F\n",
-    "ha=2.10; # surface coefficient,Btu/(hr)*(ft^2)*(F)\n",
-    "q=((3.14)*(300-70))/(((1/(2*0.033))*log(3.375/2.375))+(1/((2.10)*(3.375/12)))); # using formula for heat loss,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss for linear foot is :  Btu/(hr)*(lin ft)\",round(q,1)\n",
-    "print\"\\t Check between ts and t1, since delt/R = deltc/Rc \"\n",
-    "t1=300-(((103)*((1)*(log(3.375/2.375))))/((2)*(3.14)*(.033))); # using eq 2.31,F\n",
-    "print\"\\t t1 is : F \",round(t1,1)\n",
-    "# end \n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation.ipynb
deleted file mode 100755
index 71f8ec94..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation.ipynb
+++ /dev/null
@@ -1,208 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 4: Radiation"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.1 pgno:75"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  3500.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\";\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "#solution\n",
-    "Q=((0.173)*((14.6)**4-(12.6)**4)); # using eq.4.24,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.2 pgno:76"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  1826.0\n",
-      "\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "e1=0.6; # emissivity of hotter wall\n",
-    "e2=0.8; # emissivity of colder wall\n",
-    "#solution\n",
-    "Q=(((0.173)/((1/0.6)+(1/0.8)-1))*((14.6)**4-(12.6)**4)); # using eq.4.26,heat loss per unit area,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "print\"\\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.3 pgno:78"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t area is :  ft**2/lin ft  0.88\n",
-      "\t heat loss  is : Btu/(hr)*(lin ft)  52.4\n",
-      "\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F)  1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=125.+460.; # R\n",
-    "T2=70.+460.; # R\n",
-    "e=0.9; # emissivity,using table 4.1B\n",
-    "#solution\n",
-    "from math import pi\n",
-    "A=(pi)*(3.375/12)*(1); # area,ft**2/lin ft\n",
-    "print\"\\t area is :  ft**2/lin ft \",round(A,2)\n",
-    "Q=(0.9)*(0.88)*(0.173)*((T1/100)**4-(T2/100)**4); # heat loss using eq.4.32,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss  is : Btu/(hr)*(lin ft) \",round(Q,1)\n",
-    "hr=(Q)/((A)*(T1-T2)); # fictitious film coefficient,using eq 4.33,Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F) \",round(hr,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.4 pgno:82"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t surface area of pipe is :  ft**2/lin ft  0.62\n",
-      "\t surface area of duct is :  ft**2/lin ft  4\n",
-      "\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\n",
-      "\t Fe is :  0.6\n",
-      "\t heat loss due to radiation is :  Btu/(hr)*(lin ft)  162.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300+460; # R\n",
-    "T2=75+460; #R\n",
-    "A1=0.622; # area from table 11 in the appendix A,ft**2/lin ft\n",
-    "A2=4*(1*1); # surface area of duct,ft**2/lin ft\n",
-    "e1=0.79; # emissivity of oxidized steel from table 4.1\n",
-    "e2=0.276; # emissivity of oxidized zinc from table 4.1\n",
-    "print\"\\t surface area of pipe is :  ft**2/lin ft \",round(A1,2)\n",
-    "print\"\\t surface area of duct is :  ft**2/lin ft \",A2\n",
-    "print\"\\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\"\n",
-    "Fa=1; # from table 4.2\n",
-    "Fe=((1)/((1/e1)+((A1/A2)*((1/e2)-1)))); # from table 4.2\n",
-    "print\"\\t Fe is : \",round(Fe,2)\n",
-    "Q=(0.173*10**-8)*(Fa)*(Fe)*(A1)*((T1)**4-(T2)**4); # heat loss due to radiation,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss due to radiation is :  Btu/(hr)*(lin ft) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_1.ipynb
deleted file mode 100755
index 769fa4d0..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_1.ipynb
+++ /dev/null
@@ -1,199 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 4: Radiation"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.1 pgno:75"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  3500.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\";\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "#solution\n",
-    "Q=((0.173)*((14.6)**4-(12.6)**4)); # using eq.4.24,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.2 pgno:76"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  1826.0\n",
-      "\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "e1=0.6; # emissivity of hotter wall\n",
-    "e2=0.8; # emissivity of colder wall\n",
-    "#solution\n",
-    "Q=(((0.173)/((1/0.6)+(1/0.8)-1))*((14.6)**4-(12.6)**4)); # using eq.4.26,heat loss per unit area,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "print\"\\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.3 pgno:78"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t area is :  ft**2/lin ft  0.88\n",
-      "\t heat loss  is : Btu/(hr)*(lin ft)  52.4\n",
-      "\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F)  1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=125.+460.; # R\n",
-    "T2=70.+460.; # R\n",
-    "e=0.9; # emissivity,using table 4.1B\n",
-    "#solution\n",
-    "from math import pi\n",
-    "A=(pi)*(3.375/12)*(1); # area,ft**2/lin ft\n",
-    "print\"\\t area is :  ft**2/lin ft \",round(A,2)\n",
-    "Q=(0.9)*(0.88)*(0.173)*((T1/100)**4-(T2/100)**4); # heat loss using eq.4.32,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss  is : Btu/(hr)*(lin ft) \",round(Q,1)\n",
-    "hr=(Q)/((A)*(T1-T2)); # fictitious film coefficient,using eq 4.33,Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F) \",round(hr,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.4 pgno:82"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t surface area of pipe is :  ft**2/lin ft  0.62\n",
-      "\t surface area of duct is :  ft**2/lin ft  4\n",
-      "\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\n",
-      "\t Fe is :  0.6\n",
-      "\t heat loss due to radiation is :  Btu/(hr)*(lin ft)  162.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300+460; # R\n",
-    "T2=75+460; #R\n",
-    "A1=0.622; # area from table 11 in the appendix A,ft**2/lin ft\n",
-    "A2=4*(1*1); # surface area of duct,ft**2/lin ft\n",
-    "e1=0.79; # emissivity of oxidized steel from table 4.1\n",
-    "e2=0.276; # emissivity of oxidized zinc from table 4.1\n",
-    "print\"\\t surface area of pipe is :  ft**2/lin ft \",round(A1,2)\n",
-    "print\"\\t surface area of duct is :  ft**2/lin ft \",A2\n",
-    "print\"\\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\"\n",
-    "Fa=1; # from table 4.2\n",
-    "Fe=((1)/((1/e1)+((A1/A2)*((1/e2)-1)))); # from table 4.2\n",
-    "print\"\\t Fe is : \",round(Fe,2)\n",
-    "Q=(0.173*10**-8)*(Fa)*(Fe)*(A1)*((T1)**4-(T2)**4); # heat loss due to radiation,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss due to radiation is :  Btu/(hr)*(lin ft) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_2.ipynb
deleted file mode 100755
index 769fa4d0..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_2.ipynb
+++ /dev/null
@@ -1,199 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 4: Radiation"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.1 pgno:75"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  3500.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\";\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "#solution\n",
-    "Q=((0.173)*((14.6)**4-(12.6)**4)); # using eq.4.24,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.2 pgno:76"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  1826.0\n",
-      "\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "e1=0.6; # emissivity of hotter wall\n",
-    "e2=0.8; # emissivity of colder wall\n",
-    "#solution\n",
-    "Q=(((0.173)/((1/0.6)+(1/0.8)-1))*((14.6)**4-(12.6)**4)); # using eq.4.26,heat loss per unit area,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "print\"\\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.3 pgno:78"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t area is :  ft**2/lin ft  0.88\n",
-      "\t heat loss  is : Btu/(hr)*(lin ft)  52.4\n",
-      "\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F)  1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=125.+460.; # R\n",
-    "T2=70.+460.; # R\n",
-    "e=0.9; # emissivity,using table 4.1B\n",
-    "#solution\n",
-    "from math import pi\n",
-    "A=(pi)*(3.375/12)*(1); # area,ft**2/lin ft\n",
-    "print\"\\t area is :  ft**2/lin ft \",round(A,2)\n",
-    "Q=(0.9)*(0.88)*(0.173)*((T1/100)**4-(T2/100)**4); # heat loss using eq.4.32,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss  is : Btu/(hr)*(lin ft) \",round(Q,1)\n",
-    "hr=(Q)/((A)*(T1-T2)); # fictitious film coefficient,using eq 4.33,Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F) \",round(hr,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.4 pgno:82"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t surface area of pipe is :  ft**2/lin ft  0.62\n",
-      "\t surface area of duct is :  ft**2/lin ft  4\n",
-      "\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\n",
-      "\t Fe is :  0.6\n",
-      "\t heat loss due to radiation is :  Btu/(hr)*(lin ft)  162.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300+460; # R\n",
-    "T2=75+460; #R\n",
-    "A1=0.622; # area from table 11 in the appendix A,ft**2/lin ft\n",
-    "A2=4*(1*1); # surface area of duct,ft**2/lin ft\n",
-    "e1=0.79; # emissivity of oxidized steel from table 4.1\n",
-    "e2=0.276; # emissivity of oxidized zinc from table 4.1\n",
-    "print\"\\t surface area of pipe is :  ft**2/lin ft \",round(A1,2)\n",
-    "print\"\\t surface area of duct is :  ft**2/lin ft \",A2\n",
-    "print\"\\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\"\n",
-    "Fa=1; # from table 4.2\n",
-    "Fe=((1)/((1/e1)+((A1/A2)*((1/e2)-1)))); # from table 4.2\n",
-    "print\"\\t Fe is : \",round(Fe,2)\n",
-    "Q=(0.173*10**-8)*(Fa)*(Fe)*(A1)*((T1)**4-(T2)**4); # heat loss due to radiation,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss due to radiation is :  Btu/(hr)*(lin ft) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_3.ipynb
deleted file mode 100755
index 769fa4d0..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_4_Radiation_3.ipynb
+++ /dev/null
@@ -1,199 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 4: Radiation"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.1 pgno:75"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  3500.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\";\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "#solution\n",
-    "Q=((0.173)*((14.6)**4-(12.6)**4)); # using eq.4.24,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.2 pgno:76"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2)  1826.0\n",
-      "\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=1000+460; # R\n",
-    "T2=800+460; # R\n",
-    "e1=0.6; # emissivity of hotter wall\n",
-    "e2=0.8; # emissivity of colder wall\n",
-    "#solution\n",
-    "Q=(((0.173)/((1/0.6)+(1/0.8)-1))*((14.6)**4-(12.6)**4)); # using eq.4.26,heat loss per unit area,Btu/(hr)*(ft**2)\n",
-    "#results\n",
-    "print\"\\t heat removed from colder wall per unit area is : Btu/(hr)*(ft**2) \",round(Q,0)\n",
-    "print\"\\t For perfect black bodies the value was 3500 Btu/(hr)(ft**2) \"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.3 pgno:78"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t area is :  ft**2/lin ft  0.88\n",
-      "\t heat loss  is : Btu/(hr)*(lin ft)  52.4\n",
-      "\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F)  1.08\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=125.+460.; # R\n",
-    "T2=70.+460.; # R\n",
-    "e=0.9; # emissivity,using table 4.1B\n",
-    "#solution\n",
-    "from math import pi\n",
-    "A=(pi)*(3.375/12)*(1); # area,ft**2/lin ft\n",
-    "print\"\\t area is :  ft**2/lin ft \",round(A,2)\n",
-    "Q=(0.9)*(0.88)*(0.173)*((T1/100)**4-(T2/100)**4); # heat loss using eq.4.32,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss  is : Btu/(hr)*(lin ft) \",round(Q,1)\n",
-    "hr=(Q)/((A)*(T1-T2)); # fictitious film coefficient,using eq 4.33,Btu/(hr)(ft**2)(F)\n",
-    "print\"\\t fictitious film coefficient is :  Btu/(hr)(ft**2)(F) \",round(hr,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 4.4 pgno:82"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t surface area of pipe is :  ft**2/lin ft  0.62\n",
-      "\t surface area of duct is :  ft**2/lin ft  4\n",
-      "\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\n",
-      "\t Fe is :  0.6\n",
-      "\t heat loss due to radiation is :  Btu/(hr)*(lin ft)  162.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300+460; # R\n",
-    "T2=75+460; #R\n",
-    "A1=0.622; # area from table 11 in the appendix A,ft**2/lin ft\n",
-    "A2=4*(1*1); # surface area of duct,ft**2/lin ft\n",
-    "e1=0.79; # emissivity of oxidized steel from table 4.1\n",
-    "e2=0.276; # emissivity of oxidized zinc from table 4.1\n",
-    "print\"\\t surface area of pipe is :  ft**2/lin ft \",round(A1,2)\n",
-    "print\"\\t surface area of duct is :  ft**2/lin ft \",A2\n",
-    "print\"\\t The surface of the pipe is not negligible by comparison with that of the duct, and(f) of Table 4.2 applies most nearly\"\n",
-    "Fa=1; # from table 4.2\n",
-    "Fe=((1)/((1/e1)+((A1/A2)*((1/e2)-1)))); # from table 4.2\n",
-    "print\"\\t Fe is : \",round(Fe,2)\n",
-    "Q=(0.173*10**-8)*(Fa)*(Fe)*(A1)*((T1)**4-(T2)**4); # heat loss due to radiation,Btu/(hr)*(lin ft)\n",
-    "print\"\\t heat loss due to radiation is :  Btu/(hr)*(lin ft) \",round(Q,0)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature.ipynb
deleted file mode 100755
index 8b658273..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature.ipynb
+++ /dev/null
@@ -1,408 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 5: Temperature"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.1 pgno:90"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  100.0\n",
-      "\t LMTDc is : F  123.3\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTDp is : F  108.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=150.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDc=((delt2-delt1)/(log(delt2/delt1)));\n",
-    "print\"\\t LMTDc is : F \",round(LMTDc,1)\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDp=((delt2-delt1)/((log(delt2/delt1))));\n",
-    "print\"\\t LMTDp is : F \",round(LMTDp,0)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.2 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTD is : F  72.1347520444\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  0.0\n",
-      "\t denominator becomes infinity so LMTD becomes Zero \n",
-      "\n",
-      "\t LMTD is Zero \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=150.; # cold fluid inlet temperature,F\n",
-    "t2=200.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.3 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delth is :  F  25.0\n",
-      "\t deltc is :  F  100.0\n",
-      "\t LMTD is : F  54.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "LMTD=((delth-deltc)/((1)*(log(delth/deltc))))\n",
-    "print\"\\t LMTD is : F \",round(LMTD,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.4 pgno:92"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.4 \n",
-      "\n",
-      "\t process is isothermal with hot fluid so temperature of hot fluid remains constant \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delt1 is :  F  25.0\n",
-      "\t delt2 is :  F  200.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t for parallel flow \n",
-      "\n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  25.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t these are identical \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.4 \\n\"\n",
-    "print\"\\t process is isothermal with hot fluid so temperature of hot fluid remains constant \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=300.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \\n\"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "print\"\\t these are identical \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.5 pgno:93"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 7,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for inlet \t\n",
-      "\t Re is : \t2589.0\n",
-      "\t Pr is : \t3.52\n",
-      "\t nusselt number is :  \t105.0\n",
-      "\t heat transfer coefficient is : 158.0\n",
-      "\t for outlet \t\n",
-      "\t Re is :  \t3372.0\n",
-      "\t Pr is :  \t3.23\n",
-      "\t nusselt number is :  \t125.0\n",
-      "\t heat transfer coefficient is : 189.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t for inlet \\t\"\n",
-    "t1=99.1; # temperature of inlet,F\n",
-    "t2=129.2; # temperature of outlet,F\n",
-    "c=.478; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=7.139; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(0.9);\n",
-    "print\"\\t Re is : \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is : \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "print\"\\t for outlet \\t\"\n",
-    "c=.495; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=2.20*2.42; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(.9); # reynolds number raised to poer 0.9, calculation mistake in book\n",
-    "print\"\\t Re is :  \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.6 pgno:97"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.6 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t for counter current flow \n",
-      "\t temperature difference for crude oil is :  F  100\n",
-      "\t temperature difference for gasoline is :  F  40\n",
-      "\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \n",
-      "\t deltc is :  F  120\n",
-      "\t delth is :  F  180\n",
-      "\t ratio of two local temperature difference is :  0.67\n",
-      "\t caloric temperature of hot fluid is :  F  242.5\n",
-      "\t caloric temperature of cold fluid is : F  97.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.6 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "T1=300; # hot fluid inlet temperature,F\n",
-    "T2=200; # hot fluid outlet temperature,F\n",
-    "t1=80; # cold fluid inlet temperature,F\n",
-    "t2=120; # cold fluid outlet temperature,F\n",
-    "print\"\\t for counter current flow \"\n",
-    "delT=T1-T2; # temperature difference for crude oil,F\n",
-    "print\"\\t temperature difference for crude oil is :  F \",delT\n",
-    "Kc=0.68; # from fig.17\n",
-    "delt=t2-t1; # temperature difference for gasoline,F\n",
-    "print\"\\t temperature difference for gasoline is :  F \",delt\n",
-    "Kc<=0.10; # from fig.17\n",
-    "print\"\\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "A=120./180.#((deltc)/(delth));\n",
-    "print\"\\t ratio of two local temperature difference is : \",round(A,2)\n",
-    "Fc=0.425; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : F \",tc\n",
-    "# end\n",
-    "\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_1.ipynb
deleted file mode 100755
index 2fa21473..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_1.ipynb
+++ /dev/null
@@ -1,399 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 5: Temperature"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.1 pgno:90"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  100.0\n",
-      "\t LMTDc is : F  123.3\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTDp is : F  108.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=150.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDc=((delt2-delt1)/(log(delt2/delt1)));\n",
-    "print\"\\t LMTDc is : F \",round(LMTDc,1)\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDp=((delt2-delt1)/((log(delt2/delt1))));\n",
-    "print\"\\t LMTDp is : F \",round(LMTDp,0)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.2 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTD is : F  72.1347520444\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  0.0\n",
-      "\t denominator becomes infinity so LMTD becomes Zero \n",
-      "\n",
-      "\t LMTD is Zero \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=150.; # cold fluid inlet temperature,F\n",
-    "t2=200.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.3 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delth is :  F  25.0\n",
-      "\t deltc is :  F  100.0\n",
-      "\t LMTD is : F  54.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "LMTD=((delth-deltc)/((1)*(log(delth/deltc))))\n",
-    "print\"\\t LMTD is : F \",round(LMTD,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.4 pgno:92"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.4 \n",
-      "\n",
-      "\t process is isothermal with hot fluid so temperature of hot fluid remains constant \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delt1 is :  F  25.0\n",
-      "\t delt2 is :  F  200.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t for parallel flow \n",
-      "\n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  25.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t these are identical \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.4 \\n\"\n",
-    "print\"\\t process is isothermal with hot fluid so temperature of hot fluid remains constant \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=300.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \\n\"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "print\"\\t these are identical \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.5 pgno:93"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 7,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for inlet \t\n",
-      "\t Re is : \t2589.0\n",
-      "\t Pr is : \t3.52\n",
-      "\t nusselt number is :  \t105.0\n",
-      "\t heat transfer coefficient is : 158.0\n",
-      "\t for outlet \t\n",
-      "\t Re is :  \t3372.0\n",
-      "\t Pr is :  \t3.23\n",
-      "\t nusselt number is :  \t125.0\n",
-      "\t heat transfer coefficient is : 189.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t for inlet \\t\"\n",
-    "t1=99.1; # temperature of inlet,F\n",
-    "t2=129.2; # temperature of outlet,F\n",
-    "c=.478; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=7.139; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(0.9);\n",
-    "print\"\\t Re is : \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is : \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "print\"\\t for outlet \\t\"\n",
-    "c=.495; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=2.20*2.42; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(.9); # reynolds number raised to poer 0.9, calculation mistake in book\n",
-    "print\"\\t Re is :  \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.6 pgno:97"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.6 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t for counter current flow \n",
-      "\t temperature difference for crude oil is :  F  100\n",
-      "\t temperature difference for gasoline is :  F  40\n",
-      "\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \n",
-      "\t deltc is :  F  120\n",
-      "\t delth is :  F  180\n",
-      "\t ratio of two local temperature difference is :  0.67\n",
-      "\t caloric temperature of hot fluid is :  F  242.5\n",
-      "\t caloric temperature of cold fluid is : F  97.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.6 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "T1=300; # hot fluid inlet temperature,F\n",
-    "T2=200; # hot fluid outlet temperature,F\n",
-    "t1=80; # cold fluid inlet temperature,F\n",
-    "t2=120; # cold fluid outlet temperature,F\n",
-    "print\"\\t for counter current flow \"\n",
-    "delT=T1-T2; # temperature difference for crude oil,F\n",
-    "print\"\\t temperature difference for crude oil is :  F \",delT\n",
-    "Kc=0.68; # from fig.17\n",
-    "delt=t2-t1; # temperature difference for gasoline,F\n",
-    "print\"\\t temperature difference for gasoline is :  F \",delt\n",
-    "Kc<=0.10; # from fig.17\n",
-    "print\"\\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "A=120./180.#((deltc)/(delth));\n",
-    "print\"\\t ratio of two local temperature difference is : \",round(A,2)\n",
-    "Fc=0.425; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : F \",tc\n",
-    "# end\n",
-    "\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_2.ipynb
deleted file mode 100755
index 2fa21473..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_2.ipynb
+++ /dev/null
@@ -1,399 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 5: Temperature"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.1 pgno:90"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  100.0\n",
-      "\t LMTDc is : F  123.3\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTDp is : F  108.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=150.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDc=((delt2-delt1)/(log(delt2/delt1)));\n",
-    "print\"\\t LMTDc is : F \",round(LMTDc,1)\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDp=((delt2-delt1)/((log(delt2/delt1))));\n",
-    "print\"\\t LMTDp is : F \",round(LMTDp,0)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.2 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTD is : F  72.1347520444\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  0.0\n",
-      "\t denominator becomes infinity so LMTD becomes Zero \n",
-      "\n",
-      "\t LMTD is Zero \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=150.; # cold fluid inlet temperature,F\n",
-    "t2=200.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.3 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delth is :  F  25.0\n",
-      "\t deltc is :  F  100.0\n",
-      "\t LMTD is : F  54.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "LMTD=((delth-deltc)/((1)*(log(delth/deltc))))\n",
-    "print\"\\t LMTD is : F \",round(LMTD,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.4 pgno:92"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.4 \n",
-      "\n",
-      "\t process is isothermal with hot fluid so temperature of hot fluid remains constant \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delt1 is :  F  25.0\n",
-      "\t delt2 is :  F  200.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t for parallel flow \n",
-      "\n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  25.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t these are identical \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.4 \\n\"\n",
-    "print\"\\t process is isothermal with hot fluid so temperature of hot fluid remains constant \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=300.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \\n\"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "print\"\\t these are identical \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.5 pgno:93"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 7,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for inlet \t\n",
-      "\t Re is : \t2589.0\n",
-      "\t Pr is : \t3.52\n",
-      "\t nusselt number is :  \t105.0\n",
-      "\t heat transfer coefficient is : 158.0\n",
-      "\t for outlet \t\n",
-      "\t Re is :  \t3372.0\n",
-      "\t Pr is :  \t3.23\n",
-      "\t nusselt number is :  \t125.0\n",
-      "\t heat transfer coefficient is : 189.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t for inlet \\t\"\n",
-    "t1=99.1; # temperature of inlet,F\n",
-    "t2=129.2; # temperature of outlet,F\n",
-    "c=.478; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=7.139; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(0.9);\n",
-    "print\"\\t Re is : \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is : \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "print\"\\t for outlet \\t\"\n",
-    "c=.495; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=2.20*2.42; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(.9); # reynolds number raised to poer 0.9, calculation mistake in book\n",
-    "print\"\\t Re is :  \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.6 pgno:97"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.6 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t for counter current flow \n",
-      "\t temperature difference for crude oil is :  F  100\n",
-      "\t temperature difference for gasoline is :  F  40\n",
-      "\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \n",
-      "\t deltc is :  F  120\n",
-      "\t delth is :  F  180\n",
-      "\t ratio of two local temperature difference is :  0.67\n",
-      "\t caloric temperature of hot fluid is :  F  242.5\n",
-      "\t caloric temperature of cold fluid is : F  97.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.6 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "T1=300; # hot fluid inlet temperature,F\n",
-    "T2=200; # hot fluid outlet temperature,F\n",
-    "t1=80; # cold fluid inlet temperature,F\n",
-    "t2=120; # cold fluid outlet temperature,F\n",
-    "print\"\\t for counter current flow \"\n",
-    "delT=T1-T2; # temperature difference for crude oil,F\n",
-    "print\"\\t temperature difference for crude oil is :  F \",delT\n",
-    "Kc=0.68; # from fig.17\n",
-    "delt=t2-t1; # temperature difference for gasoline,F\n",
-    "print\"\\t temperature difference for gasoline is :  F \",delt\n",
-    "Kc<=0.10; # from fig.17\n",
-    "print\"\\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "A=120./180.#((deltc)/(delth));\n",
-    "print\"\\t ratio of two local temperature difference is : \",round(A,2)\n",
-    "Fc=0.425; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : F \",tc\n",
-    "# end\n",
-    "\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_3.ipynb
deleted file mode 100755
index 2fa21473..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_5_Temperature_3.ipynb
+++ /dev/null
@@ -1,399 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 5: Temperature"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.1 pgno:90"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 1,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  100.0\n",
-      "\t LMTDc is : F  123.3\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTDp is : F  108.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=150.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDc=((delt2-delt1)/(log(delt2/delt1)));\n",
-    "print\"\\t LMTDc is : F \",round(LMTDc,1)\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTDp=((delt2-delt1)/((log(delt2/delt1))));\n",
-    "print\"\\t LMTDp is : F \",round(LMTDp,0)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.2 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 2,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  50.0\n",
-      "\t LMTD is : F  72.1347520444\n",
-      "\t for parallel flow \n",
-      "\t delt1 is :  F  150.0\n",
-      "\t delt2 is :  F  0.0\n",
-      "\t denominator becomes infinity so LMTD becomes Zero \n",
-      "\n",
-      "\t LMTD is Zero \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=150.; # cold fluid inlet temperature,F\n",
-    "t2=200.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.3 pgno:91"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delth is :  F  25.0\n",
-      "\t deltc is :  F  100.0\n",
-      "\t LMTD is : F  54.1\n"
-     ]
-    }
-   ],
-   "source": [
-    "\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=200.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "LMTD=((delth-deltc)/((1)*(log(delth/deltc))))\n",
-    "print\"\\t LMTD is : F \",round(LMTD,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.4 pgno:92"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.4 \n",
-      "\n",
-      "\t process is isothermal with hot fluid so temperature of hot fluid remains constant \n",
-      "\n",
-      "\t for counter current flow \n",
-      "\n",
-      "\t delt1 is :  F  25.0\n",
-      "\t delt2 is :  F  200.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t for parallel flow \n",
-      "\n",
-      "\t delt1 is :  F  200.0\n",
-      "\t delt2 is :  F  25.0\n",
-      "\t LMTD is : F  84.1572107185\n",
-      "\t these are identical \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.4 \\n\"\n",
-    "print\"\\t process is isothermal with hot fluid so temperature of hot fluid remains constant \\n\"\n",
-    "#given\n",
-    "T1=300.; # hot fluid inlet temperature,F\n",
-    "T2=300.; # hot fluid outlet temperature,F\n",
-    "t1=100.; # cold fluid inlet temperature,F\n",
-    "t2=275.; # cold fluid outlet temperature,F\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t for counter current flow \\n\"\n",
-    "delt1=T1-t2; #F\n",
-    "delt2=T2-t1; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))))\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "print\"\\t for parallel flow \\n\"\n",
-    "delt1=T1-t1; # F\n",
-    "delt2=T2-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "if delt2 == 0:\n",
-    "    print\"\\t denominator becomes infinity so LMTD becomes Zero \\n\"\n",
-    "    print\"\\t LMTD is Zero \\n\"\n",
-    "else:\n",
-    "    LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "    print\"\\t LMTD is : F \",LMTD\n",
-    "    \n",
-    "print\"\\t these are identical \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.5 pgno:93"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 7,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.5 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t for inlet \t\n",
-      "\t Re is : \t2589.0\n",
-      "\t Pr is : \t3.52\n",
-      "\t nusselt number is :  \t105.0\n",
-      "\t heat transfer coefficient is : 158.0\n",
-      "\t for outlet \t\n",
-      "\t Re is :  \t3372.0\n",
-      "\t Pr is :  \t3.23\n",
-      "\t nusselt number is :  \t125.0\n",
-      "\t heat transfer coefficient is : 189.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.5 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "print\"\\t for inlet \\t\"\n",
-    "t1=99.1; # temperature of inlet,F\n",
-    "t2=129.2; # temperature of outlet,F\n",
-    "c=.478; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=7.139; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(0.9);\n",
-    "print\"\\t Re is : \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is : \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "print\"\\t for outlet \\t\"\n",
-    "c=.495; # Btu/(hr)*(ft)*(F/ft)\n",
-    "mu=2.20*2.42; # lb/(ft)(hr)\n",
-    "k=0.078; # Btu/(hr)*(ft)*(F/ft)\n",
-    "G=854000; # mass velocity,lb/(ft**2)(hr)\n",
-    "D=0.622/12; # diameter,ft\n",
-    "Re=((D)*((G)/(mu)))**(.9); # reynolds number raised to poer 0.9, calculation mistake in book\n",
-    "print\"\\t Re is :  \\t\",round(Re)\n",
-    "Pr=((c)*(mu)/k)**(1./3.); # prandtl number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",round(Pr,2)\n",
-    "Nu=0.0115*(Re)*(Pr); # formula for nusselt number\n",
-    "print\"\\t nusselt number is :  \\t\",round(Nu)\n",
-    "hi=((k)*(Nu)/(D)); # heat transfer coefficient\n",
-    "print\"\\t heat transfer coefficient is :\",round(hi) # caculation mistake in book\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 5.6 pgno:97"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 11,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 5.6 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t for counter current flow \n",
-      "\t temperature difference for crude oil is :  F  100\n",
-      "\t temperature difference for gasoline is :  F  40\n",
-      "\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \n",
-      "\t deltc is :  F  120\n",
-      "\t delth is :  F  180\n",
-      "\t ratio of two local temperature difference is :  0.67\n",
-      "\t caloric temperature of hot fluid is :  F  242.5\n",
-      "\t caloric temperature of cold fluid is : F  97.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 5.6 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "T1=300; # hot fluid inlet temperature,F\n",
-    "T2=200; # hot fluid outlet temperature,F\n",
-    "t1=80; # cold fluid inlet temperature,F\n",
-    "t2=120; # cold fluid outlet temperature,F\n",
-    "print\"\\t for counter current flow \"\n",
-    "delT=T1-T2; # temperature difference for crude oil,F\n",
-    "print\"\\t temperature difference for crude oil is :  F \",delT\n",
-    "Kc=0.68; # from fig.17\n",
-    "delt=t2-t1; # temperature difference for gasoline,F\n",
-    "print\"\\t temperature difference for gasoline is :  F \",delt\n",
-    "Kc<=0.10; # from fig.17\n",
-    "print\"\\t The larger value of K. correspQnds to the controlling heat transfer coefficient which is assumed to establish the variation of U with temperature \"\n",
-    "deltc=T2-t1; #F\n",
-    "delth=T1-t2; # F\n",
-    "print\"\\t deltc is :  F \",deltc\n",
-    "print\"\\t delth is :  F \",delth\n",
-    "A=120./180.#((deltc)/(delth));\n",
-    "print\"\\t ratio of two local temperature difference is : \",round(A,2)\n",
-    "Fc=0.425; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is : F \",tc\n",
-    "# end\n",
-    "\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers.ipynb
deleted file mode 100755
index 49162c0d..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers.ipynb
+++ /dev/null
@@ -1,507 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 6 Counterflow : Double Pipe Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.1 pgno:113"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.1 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for benzene \n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t total heat required for benzene is :  Btu/hr  166940.0\n",
-      "\t for toulene \n",
-      "\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t W is : lb/hr  6323.48484848\n",
-      "\t 2.LMTD \n",
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  20\n",
-      "\t delt2 is :  F  40\n",
-      "\t LMTD is : F \t28.8539008178\n",
-      "\t 3.caloric temperatures \n",
-      "\n",
-      "\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \n",
-      "\n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t hot fluid:annulus,toulene \n",
-      "\t flow area is :  ft**2  0.00841338147585\n",
-      "\t equiv diameter is :  ft  0.077625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  751598.494212\n",
-      "\t reynolds number is :   58801.4846938\n",
-      "\t Pr is :   1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  182.866344605\n",
-      "\t cold fluid:inner pipe,benzene \n",
-      "\t flow area is :  ft**2  0.0103868907109\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  945422.482367\n",
-      "\t reynolds number is :   89854.2028696\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  186.747826087\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  155.248192771\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  83.9646521529\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  71.891896062\n",
-      "\t required surface is :  ft**2  80.4777705563\n",
-      "\t required length is :  lin ft  185.006369095\n",
-      "\t This may be fulfilled by connecting three 20-ft hairpins in series \n",
-      "\n",
-      "\t actual surface supplied is :  ft**2  52.2\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  110.837155481\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.00288752837534\n",
-      "\t pressure drop  for annulus \n",
-      "\t De1 is :  ft  0.0345\n",
-      "\t reynolds number is : 26133.9931973\n",
-      "\t friction factor is :  0.00718449101601\n",
-      "\t delFa is :  ft  35.2200986001\n",
-      "\t V is :  fps  3.83958362305\n",
-      "\t Fl is :  ft  0.686757875702\n",
-      "\t delPa is :  psi  13.5585786172\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t friction factor is :   0.00569339980566\n",
-      "\t delFp is : ft  12.9491334918\n",
-      "\t delPp is :  psi  4.94584959755\n",
-      "\t allowable delPp is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.1 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=160; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=120; # outlet cold fluid,F\n",
-    "w=9820; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "from math import pi\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for benzene \"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "c=0.425; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for benzene is :  Btu/hr \",Q\n",
-    "print\"\\t for toulene \\n\"\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "c=0.44; # Btu/(lb)*(F)\n",
-    "W=((Q)/((c)*(T1-T2))); # lb/hr\n",
-    "print\"\\t W is : lb/hr \",round(W)\n",
-    "print\"\\t 2.LMTD \"\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD,1)\n",
-    "print\"\\t 3.caloric temperatures \\n\"\n",
-    "print\"\\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \\n\"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "print\"\\t hot fluid:annulus,toulene \"\n",
-    "D1=0.138; # ft\n",
-    "D2=0.1725; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Ga\n",
-    "mu1=0.41*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rea\n",
-    "jH=167; # from fig.24\n",
-    "c=0.44; # Btu/(lb)*(F),at 130F\n",
-    "k=0.085; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*(1**0.14)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner pipe,benzene \"\n",
-    "D=0.115; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",ap\n",
-    "Gp=(w/ap); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gp\n",
-    "mu2=0.5*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rep\n",
-    "jH=236; # from fig.24\n",
-    "c=0.425; # Btu/(lb)*(F),at 130F\n",
-    "k=0.091; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=1.38; # ft\n",
-    "OD=1.66; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "Rd=0.002; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \",A\n",
-    "A1=0.435; # From Table 11 for 1(1/4)in IPS standard pipe there are 0.435 ft2 of external surface per foot length,ft**2\n",
-    "L=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \",L\n",
-    "print\"\\t This may be fulfilled by connecting three 20-ft hairpins in series \\n\"\n",
-    "A2=120*0.435; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "De1=(D2-D1); #ft\n",
-    "print\"\\t De1 is :  ft \",De1\n",
-    "Rea1=((De1)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :\",Rea1\n",
-    "f=(0.0035)+((0.264)/(Rea1**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is : \",f\n",
-    "s=0.87;\n",
-    "row=62.5*0.87; # from table 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "Fl=((3*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t Fl is :  ft \",Fl\n",
-    "delPa=((delFa+Fl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \",f\n",
-    "s=0.88;\n",
-    "row=62.5*0.88; # from table 6\n",
-    "delFp=((4*f*(Gp**2)*L)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is : ft \",delFp\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \",delPp\n",
-    "print\"\\t allowable delPp is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.2 pgno:120"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.2 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t P is :  0.091\n",
-      "\t R is :  0.556\n",
-      "\t gama is : 0.242\n",
-      " true temperature difference is :  F  26.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.2 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=190.; # inlet cold fluid,F\n",
-    "t2=220.; # outlet cold fluid,F\n",
-    "n=6; # number of parallel streams\n",
-    "#solution\n",
-    "from math import log\n",
-    "P=((T2-t1)/(T1-t1));\n",
-    "print\"\\t P is : \",round(P,3)\n",
-    "R=((T1-T2)/((n)*(t2-t1)));\n",
-    "print\"\\t R is : \",round(R,3)\n",
-    "gama=0.242#((1-P)/((1)*((n*R)/(R-1))*log(((R-1)/R)*(1/P)**(1/n)+(1/R)))); # using eq.6.35a\n",
-    "print\"\\t gama is :\",gama\n",
-    "delt=(gama*(T1-t1)); # true temperature difference,F\n",
-    "print\" true temperature difference is :  F \",round(delt,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.3 pgno:121"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lube oil \t\n",
-      "\t total heat required for lube oil is :  Btu/hr \t427800.0\n",
-      "\t for crude oil \t\n",
-      "\t total heat required for crude oil is :  Btu/hr \t424125.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t140\n",
-      "\t LMTD is : F \t129.84255368\n",
-      "\t ratio of two local temperature difference is :  \t0\n",
-      "\t caloric temperature of hot fluid is :  F \t389.5\n",
-      "\t caloric temperature of cold fluid is :  F \t303.95\n",
-      "\t hot fluid:annulus,lube oil \t\n",
-      "\t flow area is :  ft**2 \t0.0203693013677\n",
-      "\t equiv diameter is :  ft \t0.130326633166\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t338745.049496\n",
-      "\t reynolds number is :  \t6080.92311327\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t10.5389049547\n",
-      "\t cold fluid:inner pipe,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.023235219266\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1560131.60819\n",
-      "\t reynolds number is :  \t133596.851841\n",
-      "\t Pr is :  \t1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t135.813953488\n",
-      "\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t phyp is :  \t1.01056029649\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t tw is :  F \t310.966826293\n",
-      "\t phya is :  \t0.89549017376\n",
-      "\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t9.43748582912\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.73832573656\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.30299983373\n",
-      "\t required surface is :  ft**2 \t396.815568378\n",
-      "\t required length is :  lin ft \t637.967151733\n",
-      "\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \t\n",
-      "\t actual surface supplied is :  ft**2 \t199.04\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.5532536086\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0540273138235\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 is :  ft \t0.058\n",
-      "\t reynolds number is :  \t2709.96039597\n",
-      "\t friction factor is :  \t0.0130893090019\n",
-      "\t delFa is :  ft \t16.8995403857\n",
-      "\t V is :  fps \t1.94262393976\n",
-      "\t delFl is :  ft \t0.468793511967\n",
-      "\t delPa is :  psi \t5.84221300811\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t friction factor is :  \t0.0053568\n",
-      "\t delFp is :  ft \t25.7\n",
-      "\t delPp is :  psi \t8.5\n",
-      "\t allowable delPp is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450; # inlet hot fluid,F\n",
-    "T2=350; # outlet hot fluid,F\n",
-    "t1=300; # inlet cold fluid,F\n",
-    "t2=310; # outlet cold fluid,F\n",
-    "W=6900; # lb/hr\n",
-    "w=72500; # lb/hr\n",
-    "from math import log,pi\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lube oil \\t\"\n",
-    "c=0.62; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lube oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for crude oil \\t\"\n",
-    "c=0.585; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude oil is :  Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "A=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",A\n",
-    "Fc=0.395; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:annulus,lube oil \\t\"\n",
-    "D1=0.199; # ft\n",
-    "D2=0.256; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=3*2.42; # at 389.5F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jH=20.5; # from fig.24\n",
-    "c=0.615; # Btu/(lb)*(F),at 130F\n",
-    "k=0.067; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "print\"\\t cold fluid:inner pipe,crude oil \\t\"\n",
-    "D=0.172; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",ap\n",
-    "Gp=(w/(2*ap)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gp\n",
-    "mu2=0.83*2.42; # at 304 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rep\n",
-    "jH=320; # from fig.24\n",
-    "c=0.585; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.073; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=2.067; # ft\n",
-    "OD=2.38; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=0.77*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyp=(mu2/muw)**0.14;\n",
-    "print\"\\t phyp is :  \\t\",phyp # from fig.24\n",
-    "hio=(Hio)*(1); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=6.6*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phya=(mu1/muw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "ho=(Ho)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.006; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \\t\",A\n",
-    "A1=0.622; # From Table 11,ft**2\n",
-    "Lr=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \\t\",Lr\n",
-    "print\"\\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \\t\"\n",
-    "L=320;\n",
-    "A2=320*0.622; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=.058; #ft\n",
-    "print\"\\t De1 is :  ft \\t\",De1\n",
-    "Rea1=((De1)*(Ga)/7.25); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea1\n",
-    "f=(0.0035)+((0.264)/(2680**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",f\n",
-    "s=0.775;\n",
-    "row=62.5*0.775; # from fig 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \\t\",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "delFl=((8*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t delFl is :  ft \\t\",delFl\n",
-    "delPa=((delFa+delFl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \\t\",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",round(f,7)\n",
-    "s=0.76;\n",
-    "row=62.5*0.76; # from table 6\n",
-    "Lp=160;\n",
-    "delFp=((4*f*(Gp**2)*Lp)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is :  ft \\t\",round(delFp,1)\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \\t\",round(delPp,1)\n",
-    "print\"\\t allowable delPp is 10 psi \\t\"\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_1.ipynb
deleted file mode 100755
index d1205d31..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_1.ipynb
+++ /dev/null
@@ -1,498 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 6 Counterflow : Double Pipe Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.1 pgno:113"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.1 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for benzene \n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t total heat required for benzene is :  Btu/hr  166940.0\n",
-      "\t for toulene \n",
-      "\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t W is : lb/hr  6323.48484848\n",
-      "\t 2.LMTD \n",
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  20\n",
-      "\t delt2 is :  F  40\n",
-      "\t LMTD is : F \t28.8539008178\n",
-      "\t 3.caloric temperatures \n",
-      "\n",
-      "\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \n",
-      "\n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t hot fluid:annulus,toulene \n",
-      "\t flow area is :  ft**2  0.00841338147585\n",
-      "\t equiv diameter is :  ft  0.077625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  751598.494212\n",
-      "\t reynolds number is :   58801.4846938\n",
-      "\t Pr is :   1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  182.866344605\n",
-      "\t cold fluid:inner pipe,benzene \n",
-      "\t flow area is :  ft**2  0.0103868907109\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  945422.482367\n",
-      "\t reynolds number is :   89854.2028696\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  186.747826087\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  155.248192771\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  83.9646521529\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  71.891896062\n",
-      "\t required surface is :  ft**2  80.4777705563\n",
-      "\t required length is :  lin ft  185.006369095\n",
-      "\t This may be fulfilled by connecting three 20-ft hairpins in series \n",
-      "\n",
-      "\t actual surface supplied is :  ft**2  52.2\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  110.837155481\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.00288752837534\n",
-      "\t pressure drop  for annulus \n",
-      "\t De1 is :  ft  0.0345\n",
-      "\t reynolds number is : 26133.9931973\n",
-      "\t friction factor is :  0.00718449101601\n",
-      "\t delFa is :  ft  35.2200986001\n",
-      "\t V is :  fps  3.83958362305\n",
-      "\t Fl is :  ft  0.686757875702\n",
-      "\t delPa is :  psi  13.5585786172\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t friction factor is :   0.00569339980566\n",
-      "\t delFp is : ft  12.9491334918\n",
-      "\t delPp is :  psi  4.94584959755\n",
-      "\t allowable delPp is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.1 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=160; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=120; # outlet cold fluid,F\n",
-    "w=9820; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "from math import pi\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for benzene \"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "c=0.425; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for benzene is :  Btu/hr \",Q\n",
-    "print\"\\t for toulene \\n\"\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "c=0.44; # Btu/(lb)*(F)\n",
-    "W=((Q)/((c)*(T1-T2))); # lb/hr\n",
-    "print\"\\t W is : lb/hr \",round(W)\n",
-    "print\"\\t 2.LMTD \"\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD,1)\n",
-    "print\"\\t 3.caloric temperatures \\n\"\n",
-    "print\"\\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \\n\"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "print\"\\t hot fluid:annulus,toulene \"\n",
-    "D1=0.138; # ft\n",
-    "D2=0.1725; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Ga\n",
-    "mu1=0.41*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rea\n",
-    "jH=167; # from fig.24\n",
-    "c=0.44; # Btu/(lb)*(F),at 130F\n",
-    "k=0.085; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*(1**0.14)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner pipe,benzene \"\n",
-    "D=0.115; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",ap\n",
-    "Gp=(w/ap); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gp\n",
-    "mu2=0.5*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rep\n",
-    "jH=236; # from fig.24\n",
-    "c=0.425; # Btu/(lb)*(F),at 130F\n",
-    "k=0.091; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=1.38; # ft\n",
-    "OD=1.66; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "Rd=0.002; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \",A\n",
-    "A1=0.435; # From Table 11 for 1(1/4)in IPS standard pipe there are 0.435 ft2 of external surface per foot length,ft**2\n",
-    "L=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \",L\n",
-    "print\"\\t This may be fulfilled by connecting three 20-ft hairpins in series \\n\"\n",
-    "A2=120*0.435; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "De1=(D2-D1); #ft\n",
-    "print\"\\t De1 is :  ft \",De1\n",
-    "Rea1=((De1)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :\",Rea1\n",
-    "f=(0.0035)+((0.264)/(Rea1**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is : \",f\n",
-    "s=0.87;\n",
-    "row=62.5*0.87; # from table 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "Fl=((3*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t Fl is :  ft \",Fl\n",
-    "delPa=((delFa+Fl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \",f\n",
-    "s=0.88;\n",
-    "row=62.5*0.88; # from table 6\n",
-    "delFp=((4*f*(Gp**2)*L)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is : ft \",delFp\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \",delPp\n",
-    "print\"\\t allowable delPp is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.2 pgno:120"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.2 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t P is :  0.091\n",
-      "\t R is :  0.556\n",
-      "\t gama is : 0.242\n",
-      " true temperature difference is :  F  26.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.2 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=190.; # inlet cold fluid,F\n",
-    "t2=220.; # outlet cold fluid,F\n",
-    "n=6; # number of parallel streams\n",
-    "#solution\n",
-    "from math import log\n",
-    "P=((T2-t1)/(T1-t1));\n",
-    "print\"\\t P is : \",round(P,3)\n",
-    "R=((T1-T2)/((n)*(t2-t1)));\n",
-    "print\"\\t R is : \",round(R,3)\n",
-    "gama=0.242#((1-P)/((1)*((n*R)/(R-1))*log(((R-1)/R)*(1/P)**(1/n)+(1/R)))); # using eq.6.35a\n",
-    "print\"\\t gama is :\",gama\n",
-    "delt=(gama*(T1-t1)); # true temperature difference,F\n",
-    "print\" true temperature difference is :  F \",round(delt,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.3 pgno:121"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lube oil \t\n",
-      "\t total heat required for lube oil is :  Btu/hr \t427800.0\n",
-      "\t for crude oil \t\n",
-      "\t total heat required for crude oil is :  Btu/hr \t424125.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t140\n",
-      "\t LMTD is : F \t129.84255368\n",
-      "\t ratio of two local temperature difference is :  \t0\n",
-      "\t caloric temperature of hot fluid is :  F \t389.5\n",
-      "\t caloric temperature of cold fluid is :  F \t303.95\n",
-      "\t hot fluid:annulus,lube oil \t\n",
-      "\t flow area is :  ft**2 \t0.0203693013677\n",
-      "\t equiv diameter is :  ft \t0.130326633166\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t338745.049496\n",
-      "\t reynolds number is :  \t6080.92311327\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t10.5389049547\n",
-      "\t cold fluid:inner pipe,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.023235219266\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1560131.60819\n",
-      "\t reynolds number is :  \t133596.851841\n",
-      "\t Pr is :  \t1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t135.813953488\n",
-      "\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t phyp is :  \t1.01056029649\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t tw is :  F \t310.966826293\n",
-      "\t phya is :  \t0.89549017376\n",
-      "\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t9.43748582912\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.73832573656\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.30299983373\n",
-      "\t required surface is :  ft**2 \t396.815568378\n",
-      "\t required length is :  lin ft \t637.967151733\n",
-      "\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \t\n",
-      "\t actual surface supplied is :  ft**2 \t199.04\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.5532536086\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0540273138235\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 is :  ft \t0.058\n",
-      "\t reynolds number is :  \t2709.96039597\n",
-      "\t friction factor is :  \t0.0130893090019\n",
-      "\t delFa is :  ft \t16.8995403857\n",
-      "\t V is :  fps \t1.94262393976\n",
-      "\t delFl is :  ft \t0.468793511967\n",
-      "\t delPa is :  psi \t5.84221300811\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t friction factor is :  \t0.0053568\n",
-      "\t delFp is :  ft \t25.7\n",
-      "\t delPp is :  psi \t8.5\n",
-      "\t allowable delPp is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450; # inlet hot fluid,F\n",
-    "T2=350; # outlet hot fluid,F\n",
-    "t1=300; # inlet cold fluid,F\n",
-    "t2=310; # outlet cold fluid,F\n",
-    "W=6900; # lb/hr\n",
-    "w=72500; # lb/hr\n",
-    "from math import log,pi\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lube oil \\t\"\n",
-    "c=0.62; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lube oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for crude oil \\t\"\n",
-    "c=0.585; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude oil is :  Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "A=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",A\n",
-    "Fc=0.395; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:annulus,lube oil \\t\"\n",
-    "D1=0.199; # ft\n",
-    "D2=0.256; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=3*2.42; # at 389.5F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jH=20.5; # from fig.24\n",
-    "c=0.615; # Btu/(lb)*(F),at 130F\n",
-    "k=0.067; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "print\"\\t cold fluid:inner pipe,crude oil \\t\"\n",
-    "D=0.172; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",ap\n",
-    "Gp=(w/(2*ap)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gp\n",
-    "mu2=0.83*2.42; # at 304 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rep\n",
-    "jH=320; # from fig.24\n",
-    "c=0.585; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.073; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=2.067; # ft\n",
-    "OD=2.38; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=0.77*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyp=(mu2/muw)**0.14;\n",
-    "print\"\\t phyp is :  \\t\",phyp # from fig.24\n",
-    "hio=(Hio)*(1); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=6.6*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phya=(mu1/muw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "ho=(Ho)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.006; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \\t\",A\n",
-    "A1=0.622; # From Table 11,ft**2\n",
-    "Lr=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \\t\",Lr\n",
-    "print\"\\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \\t\"\n",
-    "L=320;\n",
-    "A2=320*0.622; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=.058; #ft\n",
-    "print\"\\t De1 is :  ft \\t\",De1\n",
-    "Rea1=((De1)*(Ga)/7.25); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea1\n",
-    "f=(0.0035)+((0.264)/(2680**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",f\n",
-    "s=0.775;\n",
-    "row=62.5*0.775; # from fig 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \\t\",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "delFl=((8*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t delFl is :  ft \\t\",delFl\n",
-    "delPa=((delFa+delFl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \\t\",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",round(f,7)\n",
-    "s=0.76;\n",
-    "row=62.5*0.76; # from table 6\n",
-    "Lp=160;\n",
-    "delFp=((4*f*(Gp**2)*Lp)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is :  ft \\t\",round(delFp,1)\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \\t\",round(delPp,1)\n",
-    "print\"\\t allowable delPp is 10 psi \\t\"\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_2.ipynb
deleted file mode 100755
index d1205d31..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_2.ipynb
+++ /dev/null
@@ -1,498 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 6 Counterflow : Double Pipe Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.1 pgno:113"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.1 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for benzene \n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t total heat required for benzene is :  Btu/hr  166940.0\n",
-      "\t for toulene \n",
-      "\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t W is : lb/hr  6323.48484848\n",
-      "\t 2.LMTD \n",
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  20\n",
-      "\t delt2 is :  F  40\n",
-      "\t LMTD is : F \t28.8539008178\n",
-      "\t 3.caloric temperatures \n",
-      "\n",
-      "\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \n",
-      "\n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t hot fluid:annulus,toulene \n",
-      "\t flow area is :  ft**2  0.00841338147585\n",
-      "\t equiv diameter is :  ft  0.077625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  751598.494212\n",
-      "\t reynolds number is :   58801.4846938\n",
-      "\t Pr is :   1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  182.866344605\n",
-      "\t cold fluid:inner pipe,benzene \n",
-      "\t flow area is :  ft**2  0.0103868907109\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  945422.482367\n",
-      "\t reynolds number is :   89854.2028696\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  186.747826087\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  155.248192771\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  83.9646521529\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  71.891896062\n",
-      "\t required surface is :  ft**2  80.4777705563\n",
-      "\t required length is :  lin ft  185.006369095\n",
-      "\t This may be fulfilled by connecting three 20-ft hairpins in series \n",
-      "\n",
-      "\t actual surface supplied is :  ft**2  52.2\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  110.837155481\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.00288752837534\n",
-      "\t pressure drop  for annulus \n",
-      "\t De1 is :  ft  0.0345\n",
-      "\t reynolds number is : 26133.9931973\n",
-      "\t friction factor is :  0.00718449101601\n",
-      "\t delFa is :  ft  35.2200986001\n",
-      "\t V is :  fps  3.83958362305\n",
-      "\t Fl is :  ft  0.686757875702\n",
-      "\t delPa is :  psi  13.5585786172\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t friction factor is :   0.00569339980566\n",
-      "\t delFp is : ft  12.9491334918\n",
-      "\t delPp is :  psi  4.94584959755\n",
-      "\t allowable delPp is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.1 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=160; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=120; # outlet cold fluid,F\n",
-    "w=9820; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "from math import pi\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for benzene \"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "c=0.425; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for benzene is :  Btu/hr \",Q\n",
-    "print\"\\t for toulene \\n\"\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "c=0.44; # Btu/(lb)*(F)\n",
-    "W=((Q)/((c)*(T1-T2))); # lb/hr\n",
-    "print\"\\t W is : lb/hr \",round(W)\n",
-    "print\"\\t 2.LMTD \"\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD,1)\n",
-    "print\"\\t 3.caloric temperatures \\n\"\n",
-    "print\"\\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \\n\"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "print\"\\t hot fluid:annulus,toulene \"\n",
-    "D1=0.138; # ft\n",
-    "D2=0.1725; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Ga\n",
-    "mu1=0.41*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rea\n",
-    "jH=167; # from fig.24\n",
-    "c=0.44; # Btu/(lb)*(F),at 130F\n",
-    "k=0.085; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*(1**0.14)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner pipe,benzene \"\n",
-    "D=0.115; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",ap\n",
-    "Gp=(w/ap); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gp\n",
-    "mu2=0.5*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rep\n",
-    "jH=236; # from fig.24\n",
-    "c=0.425; # Btu/(lb)*(F),at 130F\n",
-    "k=0.091; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=1.38; # ft\n",
-    "OD=1.66; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "Rd=0.002; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \",A\n",
-    "A1=0.435; # From Table 11 for 1(1/4)in IPS standard pipe there are 0.435 ft2 of external surface per foot length,ft**2\n",
-    "L=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \",L\n",
-    "print\"\\t This may be fulfilled by connecting three 20-ft hairpins in series \\n\"\n",
-    "A2=120*0.435; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "De1=(D2-D1); #ft\n",
-    "print\"\\t De1 is :  ft \",De1\n",
-    "Rea1=((De1)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :\",Rea1\n",
-    "f=(0.0035)+((0.264)/(Rea1**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is : \",f\n",
-    "s=0.87;\n",
-    "row=62.5*0.87; # from table 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "Fl=((3*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t Fl is :  ft \",Fl\n",
-    "delPa=((delFa+Fl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \",f\n",
-    "s=0.88;\n",
-    "row=62.5*0.88; # from table 6\n",
-    "delFp=((4*f*(Gp**2)*L)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is : ft \",delFp\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \",delPp\n",
-    "print\"\\t allowable delPp is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.2 pgno:120"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.2 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t P is :  0.091\n",
-      "\t R is :  0.556\n",
-      "\t gama is : 0.242\n",
-      " true temperature difference is :  F  26.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.2 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=190.; # inlet cold fluid,F\n",
-    "t2=220.; # outlet cold fluid,F\n",
-    "n=6; # number of parallel streams\n",
-    "#solution\n",
-    "from math import log\n",
-    "P=((T2-t1)/(T1-t1));\n",
-    "print\"\\t P is : \",round(P,3)\n",
-    "R=((T1-T2)/((n)*(t2-t1)));\n",
-    "print\"\\t R is : \",round(R,3)\n",
-    "gama=0.242#((1-P)/((1)*((n*R)/(R-1))*log(((R-1)/R)*(1/P)**(1/n)+(1/R)))); # using eq.6.35a\n",
-    "print\"\\t gama is :\",gama\n",
-    "delt=(gama*(T1-t1)); # true temperature difference,F\n",
-    "print\" true temperature difference is :  F \",round(delt,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.3 pgno:121"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lube oil \t\n",
-      "\t total heat required for lube oil is :  Btu/hr \t427800.0\n",
-      "\t for crude oil \t\n",
-      "\t total heat required for crude oil is :  Btu/hr \t424125.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t140\n",
-      "\t LMTD is : F \t129.84255368\n",
-      "\t ratio of two local temperature difference is :  \t0\n",
-      "\t caloric temperature of hot fluid is :  F \t389.5\n",
-      "\t caloric temperature of cold fluid is :  F \t303.95\n",
-      "\t hot fluid:annulus,lube oil \t\n",
-      "\t flow area is :  ft**2 \t0.0203693013677\n",
-      "\t equiv diameter is :  ft \t0.130326633166\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t338745.049496\n",
-      "\t reynolds number is :  \t6080.92311327\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t10.5389049547\n",
-      "\t cold fluid:inner pipe,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.023235219266\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1560131.60819\n",
-      "\t reynolds number is :  \t133596.851841\n",
-      "\t Pr is :  \t1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t135.813953488\n",
-      "\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t phyp is :  \t1.01056029649\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t tw is :  F \t310.966826293\n",
-      "\t phya is :  \t0.89549017376\n",
-      "\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t9.43748582912\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.73832573656\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.30299983373\n",
-      "\t required surface is :  ft**2 \t396.815568378\n",
-      "\t required length is :  lin ft \t637.967151733\n",
-      "\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \t\n",
-      "\t actual surface supplied is :  ft**2 \t199.04\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.5532536086\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0540273138235\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 is :  ft \t0.058\n",
-      "\t reynolds number is :  \t2709.96039597\n",
-      "\t friction factor is :  \t0.0130893090019\n",
-      "\t delFa is :  ft \t16.8995403857\n",
-      "\t V is :  fps \t1.94262393976\n",
-      "\t delFl is :  ft \t0.468793511967\n",
-      "\t delPa is :  psi \t5.84221300811\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t friction factor is :  \t0.0053568\n",
-      "\t delFp is :  ft \t25.7\n",
-      "\t delPp is :  psi \t8.5\n",
-      "\t allowable delPp is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450; # inlet hot fluid,F\n",
-    "T2=350; # outlet hot fluid,F\n",
-    "t1=300; # inlet cold fluid,F\n",
-    "t2=310; # outlet cold fluid,F\n",
-    "W=6900; # lb/hr\n",
-    "w=72500; # lb/hr\n",
-    "from math import log,pi\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lube oil \\t\"\n",
-    "c=0.62; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lube oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for crude oil \\t\"\n",
-    "c=0.585; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude oil is :  Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "A=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",A\n",
-    "Fc=0.395; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:annulus,lube oil \\t\"\n",
-    "D1=0.199; # ft\n",
-    "D2=0.256; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=3*2.42; # at 389.5F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jH=20.5; # from fig.24\n",
-    "c=0.615; # Btu/(lb)*(F),at 130F\n",
-    "k=0.067; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "print\"\\t cold fluid:inner pipe,crude oil \\t\"\n",
-    "D=0.172; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",ap\n",
-    "Gp=(w/(2*ap)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gp\n",
-    "mu2=0.83*2.42; # at 304 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rep\n",
-    "jH=320; # from fig.24\n",
-    "c=0.585; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.073; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=2.067; # ft\n",
-    "OD=2.38; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=0.77*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyp=(mu2/muw)**0.14;\n",
-    "print\"\\t phyp is :  \\t\",phyp # from fig.24\n",
-    "hio=(Hio)*(1); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=6.6*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phya=(mu1/muw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "ho=(Ho)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.006; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \\t\",A\n",
-    "A1=0.622; # From Table 11,ft**2\n",
-    "Lr=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \\t\",Lr\n",
-    "print\"\\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \\t\"\n",
-    "L=320;\n",
-    "A2=320*0.622; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=.058; #ft\n",
-    "print\"\\t De1 is :  ft \\t\",De1\n",
-    "Rea1=((De1)*(Ga)/7.25); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea1\n",
-    "f=(0.0035)+((0.264)/(2680**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",f\n",
-    "s=0.775;\n",
-    "row=62.5*0.775; # from fig 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \\t\",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "delFl=((8*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t delFl is :  ft \\t\",delFl\n",
-    "delPa=((delFa+delFl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \\t\",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",round(f,7)\n",
-    "s=0.76;\n",
-    "row=62.5*0.76; # from table 6\n",
-    "Lp=160;\n",
-    "delFp=((4*f*(Gp**2)*Lp)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is :  ft \\t\",round(delFp,1)\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \\t\",round(delPp,1)\n",
-    "print\"\\t allowable delPp is 10 psi \\t\"\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_3.ipynb
deleted file mode 100755
index d1205d31..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_6_Counterflow_Double_Pipe_Exchangers_3.ipynb
+++ /dev/null
@@ -1,498 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 6 Counterflow : Double Pipe Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.1 pgno:113"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 4,
-   "metadata": {
-    "collapsed": false,
-    "scrolled": true
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.1 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for benzene \n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t total heat required for benzene is :  Btu/hr  166940.0\n",
-      "\t for toulene \n",
-      "\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t W is : lb/hr  6323.48484848\n",
-      "\t 2.LMTD \n",
-      "\t for counter current flow \n",
-      "\t delt1 is :  F  20\n",
-      "\t delt2 is :  F  40\n",
-      "\t LMTD is : F \t28.8539008178\n",
-      "\t 3.caloric temperatures \n",
-      "\n",
-      "\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \n",
-      "\n",
-      "\t average temperature of benzene is :  F  100\n",
-      "\t average temperature of toulene is :  F  130\n",
-      "\t hot fluid:annulus,toulene \n",
-      "\t flow area is :  ft**2  0.00841338147585\n",
-      "\t equiv diameter is :  ft  0.077625\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  751598.494212\n",
-      "\t reynolds number is :   58801.4846938\n",
-      "\t Pr is :   1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  182.866344605\n",
-      "\t cold fluid:inner pipe,benzene \n",
-      "\t flow area is :  ft**2  0.0103868907109\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  945422.482367\n",
-      "\t reynolds number is :   89854.2028696\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  186.747826087\n",
-      "\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  155.248192771\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  83.9646521529\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  71.891896062\n",
-      "\t required surface is :  ft**2  80.4777705563\n",
-      "\t required length is :  lin ft  185.006369095\n",
-      "\t This may be fulfilled by connecting three 20-ft hairpins in series \n",
-      "\n",
-      "\t actual surface supplied is :  ft**2  52.2\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  110.837155481\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.00288752837534\n",
-      "\t pressure drop  for annulus \n",
-      "\t De1 is :  ft  0.0345\n",
-      "\t reynolds number is : 26133.9931973\n",
-      "\t friction factor is :  0.00718449101601\n",
-      "\t delFa is :  ft  35.2200986001\n",
-      "\t V is :  fps  3.83958362305\n",
-      "\t Fl is :  ft  0.686757875702\n",
-      "\t delPa is :  psi  13.5585786172\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t friction factor is :   0.00569339980566\n",
-      "\t delFp is : ft  12.9491334918\n",
-      "\t delPp is :  psi  4.94584959755\n",
-      "\t allowable delPp is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.1 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=160; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=80; # inlet cold fluid,F\n",
-    "t2=120; # outlet cold fluid,F\n",
-    "w=9820; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "from math import pi\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for benzene \"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "c=0.425; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for benzene is :  Btu/hr \",Q\n",
-    "print\"\\t for toulene \\n\"\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "c=0.44; # Btu/(lb)*(F)\n",
-    "W=((Q)/((c)*(T1-T2))); # lb/hr\n",
-    "print\"\\t W is : lb/hr \",round(W)\n",
-    "print\"\\t 2.LMTD \"\n",
-    "print\"\\t for counter current flow \"\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",round(LMTD,1)\n",
-    "print\"\\t 3.caloric temperatures \\n\"\n",
-    "print\"\\t both streams will show that neither is viscous at the cold terminal (the viscosities less than 1 centipoise) and the temperature ranges and temperature difference are moderate. The coefficients may accordingly be evaluated from properties at the arithmetic mean, and the value of (mu/muw)**0.14 may be assumed equal to 1.0 \\n\"\n",
-    "tav=((t1+t2)/2); # F\n",
-    "print\"\\t average temperature of benzene is :  F \",tav\n",
-    "Tav=((T1+T2)/2); #F\n",
-    "print\"\\t average temperature of toulene is :  F \",Tav\n",
-    "print\"\\t hot fluid:annulus,toulene \"\n",
-    "D1=0.138; # ft\n",
-    "D2=0.1725; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Ga\n",
-    "mu1=0.41*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rea\n",
-    "jH=167; # from fig.24\n",
-    "c=0.44; # Btu/(lb)*(F),at 130F\n",
-    "k=0.085; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*(1**0.14)); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner pipe,benzene \"\n",
-    "D=0.115; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",ap\n",
-    "Gp=(w/ap); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gp\n",
-    "mu2=0.5*2.42; # at 130 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Rep\n",
-    "jH=236; # from fig.24\n",
-    "c=0.425; # Btu/(lb)*(F),at 130F\n",
-    "k=0.091; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=1.38; # ft\n",
-    "OD=1.66; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "Rd=0.002; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \",A\n",
-    "A1=0.435; # From Table 11 for 1(1/4)in IPS standard pipe there are 0.435 ft2 of external surface per foot length,ft**2\n",
-    "L=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \",L\n",
-    "print\"\\t This may be fulfilled by connecting three 20-ft hairpins in series \\n\"\n",
-    "A2=120*0.435; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "De1=(D2-D1); #ft\n",
-    "print\"\\t De1 is :  ft \",De1\n",
-    "Rea1=((De1)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :\",Rea1\n",
-    "f=(0.0035)+((0.264)/(Rea1**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is : \",f\n",
-    "s=0.87;\n",
-    "row=62.5*0.87; # from table 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "Fl=((3*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t Fl is :  ft \",Fl\n",
-    "delPa=((delFa+Fl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \",f\n",
-    "s=0.88;\n",
-    "row=62.5*0.88; # from table 6\n",
-    "delFp=((4*f*(Gp**2)*L)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is : ft \",delFp\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \",delPp\n",
-    "print\"\\t allowable delPp is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.2 pgno:120"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.2 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t P is :  0.091\n",
-      "\t R is :  0.556\n",
-      "\t gama is : 0.242\n",
-      " true temperature difference is :  F  26.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.2 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=300.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=190.; # inlet cold fluid,F\n",
-    "t2=220.; # outlet cold fluid,F\n",
-    "n=6; # number of parallel streams\n",
-    "#solution\n",
-    "from math import log\n",
-    "P=((T2-t1)/(T1-t1));\n",
-    "print\"\\t P is : \",round(P,3)\n",
-    "R=((T1-T2)/((n)*(t2-t1)));\n",
-    "print\"\\t R is : \",round(R,3)\n",
-    "gama=0.242#((1-P)/((1)*((n*R)/(R-1))*log(((R-1)/R)*(1/P)**(1/n)+(1/R)))); # using eq.6.35a\n",
-    "print\"\\t gama is :\",gama\n",
-    "delt=(gama*(T1-t1)); # true temperature difference,F\n",
-    "print\" true temperature difference is :  F \",round(delt,1)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 6.3 pgno:121"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 10,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 6.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for lube oil \t\n",
-      "\t total heat required for lube oil is :  Btu/hr \t427800.0\n",
-      "\t for crude oil \t\n",
-      "\t total heat required for crude oil is :  Btu/hr \t424125.0\n",
-      "\t delt1 is :  F \t50\n",
-      "\t delt2 is :  F \t140\n",
-      "\t LMTD is : F \t129.84255368\n",
-      "\t ratio of two local temperature difference is :  \t0\n",
-      "\t caloric temperature of hot fluid is :  F \t389.5\n",
-      "\t caloric temperature of cold fluid is :  F \t303.95\n",
-      "\t hot fluid:annulus,lube oil \t\n",
-      "\t flow area is :  ft**2 \t0.0203693013677\n",
-      "\t equiv diameter is :  ft \t0.130326633166\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t338745.049496\n",
-      "\t reynolds number is :  \t6080.92311327\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t10.5389049547\n",
-      "\t cold fluid:inner pipe,crude oil \t\n",
-      "\t flow area is :  ft**2 \t0.023235219266\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t1560131.60819\n",
-      "\t reynolds number is :  \t133596.851841\n",
-      "\t Pr is :  \t1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F) \t135.813953488\n",
-      "\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t phyp is :  \t1.01056029649\n",
-      "\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F)  117.952706664\n",
-      "\t tw is :  F \t310.966826293\n",
-      "\t phya is :  \t0.89549017376\n",
-      "\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \t9.43748582912\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.73832573656\n",
-      "\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t8.30299983373\n",
-      "\t required surface is :  ft**2 \t396.815568378\n",
-      "\t required length is :  lin ft \t637.967151733\n",
-      "\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \t\n",
-      "\t actual surface supplied is :  ft**2 \t199.04\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t16.5532536086\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0540273138235\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t De1 is :  ft \t0.058\n",
-      "\t reynolds number is :  \t2709.96039597\n",
-      "\t friction factor is :  \t0.0130893090019\n",
-      "\t delFa is :  ft \t16.8995403857\n",
-      "\t V is :  fps \t1.94262393976\n",
-      "\t delFl is :  ft \t0.468793511967\n",
-      "\t delPa is :  psi \t5.84221300811\n",
-      "\t allowable delPa is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t friction factor is :  \t0.0053568\n",
-      "\t delFp is :  ft \t25.7\n",
-      "\t delPp is :  psi \t8.5\n",
-      "\t allowable delPp is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 6.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "T1=450; # inlet hot fluid,F\n",
-    "T2=350; # outlet hot fluid,F\n",
-    "t1=300; # inlet cold fluid,F\n",
-    "t2=310; # outlet cold fluid,F\n",
-    "W=6900; # lb/hr\n",
-    "w=72500; # lb/hr\n",
-    "from math import log,pi\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for lube oil \\t\"\n",
-    "c=0.62; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for lube oil is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for crude oil \\t\"\n",
-    "c=0.585; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for crude oil is :  Btu/hr \\t\",Q1 # calculation mistake in book\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "A=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is :  \\t\",A\n",
-    "Fc=0.395; # from fig.17\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:annulus,lube oil \\t\"\n",
-    "D1=0.199; # ft\n",
-    "D2=0.256; # ft\n",
-    "aa=((pi)*(D2**2-D1**2)/4); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",aa\n",
-    "De=(D2**2-D1**2)/D1; # equiv diameter,ft\n",
-    "print\"\\t equiv diameter is :  ft \\t\",De\n",
-    "Ga=(W/aa); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Ga\n",
-    "mu1=3*2.42; # at 389.5F,lb/(ft)*(hr), from fig.14\n",
-    "Rea=((De)*(Ga)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea\n",
-    "jH=20.5; # from fig.24\n",
-    "c=0.615; # Btu/(lb)*(F),at 130F\n",
-    "k=0.067; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Ho\n",
-    "print\"\\t cold fluid:inner pipe,crude oil \\t\"\n",
-    "D=0.172; # ft\n",
-    "ap=((pi)*(D**2)/4); # flow area, ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",ap\n",
-    "Gp=(w/(2*ap)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gp\n",
-    "mu2=0.83*2.42; # at 304 F,lb/(ft)*(hr)\n",
-    "Rep=((D)*(Gp)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rep\n",
-    "jH=320; # from fig.24\n",
-    "c=0.585; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.073; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \\t\",Hi\n",
-    "ID=2.067; # ft\n",
-    "OD=2.38; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=0.77*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyp=(mu2/muw)**0.14;\n",
-    "print\"\\t phyp is :  \\t\",phyp # from fig.24\n",
-    "hio=(Hio)*(1); # from eq.6.37\n",
-    "print\"\\t Correct hio to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\t\",tw\n",
-    "muw=6.6*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phya=(mu1/muw)**0.14;\n",
-    "print\"\\t phya is :  \\t\",phya # from fig.24\n",
-    "ho=(Ho)*(phya); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is : Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "Rd=0.006; # required by problem,(hr)*(ft**2)*(F)/Btu\n",
-    "UD=((Uc)/((1)+(Uc*Rd))); # design overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "A=((Q)/((UD)*(LMTD))); # required surface,ft**2\n",
-    "print\"\\t required surface is :  ft**2 \\t\",A\n",
-    "A1=0.622; # From Table 11,ft**2\n",
-    "Lr=(A/A1); # required length;lin ft\n",
-    "print\"\\t required length is :  lin ft \\t\",Lr\n",
-    "print\"\\t Since two parallel streams are employed, use eight 20 ft hairpins or 320 lin. feet \\t\"\n",
-    "L=320;\n",
-    "A2=320*0.622; # actual surface supplied,ft**2\n",
-    "print\"\\t actual surface supplied is :  ft**2 \\t\",A2\n",
-    "UD=((Q)/((A2)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "De1=.058; #ft\n",
-    "print\"\\t De1 is :  ft \\t\",De1\n",
-    "Rea1=((De1)*(Ga)/7.25); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Rea1\n",
-    "f=(0.0035)+((0.264)/(2680**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",f\n",
-    "s=0.775;\n",
-    "row=62.5*0.775; # from fig 6\n",
-    "delFa=((4*f*(Ga**2)*L)/(2*4.18*(10**8)*(row**2)*(De1))); # ft\n",
-    "print\"\\t delFa is :  ft \\t\",delFa\n",
-    "V=((Ga)/(3600*row)); #fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "delFl=((8*(V**2))/(2*32.2)); #ft\n",
-    "print\"\\t delFl is :  ft \\t\",delFl\n",
-    "delPa=((delFa+delFl)*(row)/144); # psi\n",
-    "print\"\\t delPa is :  psi \\t\",delPa\n",
-    "print\"\\t allowable delPa is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=(0.0035)+((0.264)/(Rep**0.42)); # friction factor, using eq.3.47b\n",
-    "print\"\\t friction factor is :  \\t\",round(f,7)\n",
-    "s=0.76;\n",
-    "row=62.5*0.76; # from table 6\n",
-    "Lp=160;\n",
-    "delFp=((4*f*(Gp**2)*Lp)/(2*4.18*(10**8)*(row**2)*(D))); # ft\n",
-    "print\"\\t delFp is :  ft \\t\",round(delFp,1)\n",
-    "delPp=((delFp)*(row)/144); # psi\n",
-    "print\"\\t delPp is :  psi \\t\",round(delPp,1)\n",
-    "print\"\\t allowable delPp is 10 psi \\t\"\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers.ipynb
deleted file mode 100755
index 2593280d..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers.ipynb
+++ /dev/null
@@ -1,1093 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 7 Parallel-Counter flow:Shell and Tube Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.1 pgno:139"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.1 \n",
-      "\n",
-      "\t equivalent diameter is :  in  0.95\n",
-      "\t De is :  in  0.079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.1 \\n\"\n",
-    "#given\n",
-    "PT=1; # square pitch,in\n",
-    "do=0.75; # outer diameter,in\n",
-    "#solution\n",
-    "de=((4*(PT**2-(3.14*do**2/4)))/(3.14*do));\n",
-    "print\"\\t equivalent diameter is :  in \",round(de,2)\n",
-    "De=(de/12); # ft\n",
-    "print\"\\t De is :  in \",round(De,3)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.2 pgno:147"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.2 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t considering 50F approach \n",
-      "\t t2 is :  F  200.0\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100.0\n",
-      "\t R is :  1.0\n",
-      "\t S is :  0.4\n",
-      "\t FT is 0.925 \n",
-      "\t considering 0F approach \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.80 \n",
-      "\t considering 20F cross \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.64 \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.2 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "print\"\\t considering 50F approach \"\n",
-    "#given\n",
-    "T1=350.; #F\n",
-    "T2=250.; #F\n",
-    "t2=T2-50.; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "t2=200.;\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2);# F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=100.;\n",
-    "#solution\n",
-    "\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.925 \" # from fig 18\n",
-    "print\"\\t considering 0F approach \"\n",
-    "T1=300; #F\n",
-    "T2=200; #F\n",
-    "t2=T2-0; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.80 \" # from fig 18\n",
-    "print\"\\t considering 20F cross \"\n",
-    "T1=280; #F\n",
-    "T2=180; #F\n",
-    "t2=T2+20; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \\n\"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.64 \" # from fig 18\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.3 pgno:151"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\t for kerosene \n",
-      "\t total heat required for kerosene is :  Btu/hr  5034810.0\n",
-      "\t for crude oil \n",
-      "\t total heat required for mid continent crude is :  Btu/hr  5110700.0\n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  220.0\n",
-      "\t LMTD is : F  152.195928445\n",
-      "\t R is :  2.71428571429\n",
-      "\t S is :  0.241379310345\n",
-      "\t FT is 0.905 \n",
-      "\t delt is :  F  137.737315243\n",
-      "\t ratio of two local temperature difference is :  0.454545454545\n",
-      "\t caloric temperature of hot fluid is :  F  279.8\n",
-      "\t caloric temperature of cold fluid is :  F  129.4\n",
-      "\t hot fluid:shell side,kerosene \n",
-      "\t flow area is :  ft**2  0.147569444444\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  296809.411765\n",
-      "\t reynolds number is :  25296.2566845\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  86.2363636364\n",
-      "\t cold fluid:inner tube side,crude oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.141267361111\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1054737.61829\n",
-      "\t reynolds number is :  8172.03733177\n",
-      "\t Pr is :  1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F)  35.362962963\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  28.644\n",
-      "\t phyt is :  1.1303932977\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  32.3789856193\n",
-      "\t tw is :  F  242.299617309\n",
-      "\t phys is :  0.953986161765\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  82.26829755\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  23.2344278003\n",
-      "\t total surface area is :  ft**2  661.8304\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  56.0637396161\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.0252027385623\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are : 38\n",
-      "\t delPs is :  psi  3.45911725247\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  6.13806896405\n",
-      "\t delPr is :  psi  2.89156626506\n",
-      "\t delPT is :  psi  9.03\n",
-      "\t allowable delPs is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=170.; # outlet cold fluid,F\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for kerosene \"\n",
-    "c=0.605; # Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \",Q1 # calculation mistake in problem\n",
-    "print\"\\t for crude oil \"\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for mid continent crude is :  Btu/hr \",Q # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.905 \" # from fig 18\n",
-    "delt=(0.905*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X \n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,kerosene \"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.40*2.42; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=93; # from fig.28\n",
-    "c=0.59; # Btu/(lb)*(F),at 280F,from fig.4\n",
-    "k=0.0765; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\n\"\n",
-    "D=0.0675; # ft\n",
-    "Nt=158;\n",
-    "n=4; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.515; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=3.6*2.42; # at 129F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "jH=31; # from fig.24\n",
-    "c=0.49; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \",Hi\n",
-    "ID=0.81; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=1.5*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is : \",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "muw=0.56*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.00175; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.73; # for reynolds number 25300,using fig.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.000285; # friction factor for reynolds number 8220, using fig.26\n",
-    "s=0.83;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.15; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,2)\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.4 pgno:155"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.4 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for distilled water \n",
-      "\t total heat required for distilled water is : Btu/hr  1400000.0\n",
-      "\t for raw water \n",
-      "\t total heat required for raw water is :  Btu/hr  1400000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  13.0\n",
-      "\t LMTD is : F  11.4344840601\n",
-      "\t R is :   1.6\n",
-      "\t S is :  0.277777777778\n",
-      "\t FT is 0.945 \n",
-      "\t delt is :  F  10.8055874368\n",
-      "\t ratio of two local temperature difference is :  0.769230769231\n",
-      "\t caloric temperature of hot fluid is :  F  89.0\n",
-      "\t caloric temperature of cold fluid is :  F  77.5\n",
-      "\t hot fluid:shell side,distilled water \n",
-      "\t flow area is :  ft**2  0.254166666667\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  688524.590164\n",
-      "\t reynolds number is :  16099.0598149\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  573.381818182\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.185555555556\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1508982.03593\n",
-      "\t V is  fps  6.70658682635\n",
-      "\t reynolds number is :  36712.4177803\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1158.3\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  383.527824238\n",
-      "\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \n",
-      "\t total surface area is :  ft**2  502.528\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  257.821653196\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00127127741812\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  16\n",
-      "\t delPs is :  psi  7.65506963359\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  4.9\n",
-      "\t delPr is :  psi  2.6\n",
-      "\t delPT is :  psi  7.6\n",
-      "\t allowable delPT is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.4 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=93.; # inlet hot fluid,F\n",
-    "T2=85.; # outlet hot fluid,F\n",
-    "t1=75.; # inlet cold fluid,F\n",
-    "t2=80.; # outlet cold fluid,F\n",
-    "W=175000.; # lb/hr\n",
-    "w=280000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for distilled water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for distilled water is : Btu/hr \",Q\n",
-    "print\"\\t for raw water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for raw water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.945 \" # from fig 18\n",
-    "delt=(0.945*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X\n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,distilled water \"\n",
-    "ID=15.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.9375;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.81*2.42; # at 89F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=73; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 89F,from fig.table 4\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=160;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.334; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.92*2.42; # at 77.5F,lb/(ft)*(hr)\n",
-    "D=0.65/12; #ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=1350*0.99; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.65; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "print\"\\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \"\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 16200, using fig.29\n",
-    "s=1; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00019; # friction factor for reynolds number 36400, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.054; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "X1=0.33; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Exxample 7.5 pgno:159"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.5 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t delt1 is :  F  65.0\n",
-      "\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \n",
-      "\n",
-      "\t X is :  0.120481927711\n",
-      "\t Y is :  0.384615384615\n",
-      "\t delt2 is :  F  62.4\n",
-      "\t t2 is :  F  112.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.5 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=175.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "#solution\n",
-    "delt1=T2-t1; #F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "U=15; # assumption,Btu/(hr)*(ft^2)*(F)\n",
-    "theta=8000; # operating hours,hr\n",
-    "CW=(0.01/8300); # water cost,$/lb\n",
-    "print\"\\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \\n\"\n",
-    "CF=(0.3*4); # annual fixed charges/ft^2\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "X=((U)*(theta)*(CW)/(CF*c));\n",
-    "print\"\\t X is : \",X\n",
-    "Y=((T1-T2)/delt1);\n",
-    "print\"\\t Y is : \",Y\n",
-    "A=0.96; # A=(delt2/delt1), from fig 7.24\n",
-    "delt2=0.96*delt1;\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "t2=T1-delt2; # F\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.6 pgno:161"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.6 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  915667.2\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  915200.0\n",
-      "\t delt1 is :  F  22.0\n",
-      "\t delt2 is :  F  60.0\n",
-      "\t LMTD is : F  37.8749328485\n",
-      "\t R is :  2.72727272727\n",
-      "\t S is :  0.268292682927\n",
-      "\t FT is 0.81 \n",
-      "\t delt is :  F  30.6786956073\n",
-      "\t caloric temperature of hot fluid is : F 120.0\n",
-      "\t caloric temperature of cold fluid is :  F  79.0\n",
-      "\t hot fluid:shell side,phosphate solution \n",
-      "\t flow area is :  ft**2  0.0347916666667\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  579449.101796\n",
-      "\t reynolds number is :  15796.5061612\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  295.957894737\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.0545277777778\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  762913.907285\n",
-      "\t V is  fps  3.39072847682\n",
-      "\t reynolds number is :  17899.0185011\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  204.459014471\n",
-      "\t total surface area is :  ft**2  163.3216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  182.656652912\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000583796892885\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  96\n",
-      "\t delPs is :  psi  9.51887629626\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  1.58733222032\n",
-      "\t delPr is :  psi  0.6\n",
-      "\t delPT is :  psi  2.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.6 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=150.; # inlet hot fluid,F\n",
-    "T2=90.; # outlet hot fluid,F\n",
-    "t1=68.; # inlet cold fluid,F\n",
-    "t2=90.; # outlet cold fluid,F\n",
-    "W=20160.; # lb/hr\n",
-    "w=41600.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.3*0.19)+(0.7*1); # Btu/(lb)*(F), bcoz of 30 percent of solution\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.81 \" # from fig 18\n",
-    "delt=(0.81*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,phosphate solution \"\n",
-    "ID=10.02; # in\n",
-    "C=0.25; # clearance\n",
-    "B=2; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.20*2.42; # at 120F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=71; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 120F,from fig.table 4\n",
-    "k=0.33; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((0.757)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=52;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.91*2.42; # at 79F,lb/(ft)*(hr),from table 14\n",
-    "D=(0.62/12); # from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=800*1; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 15750, using fig.29\n",
-    "s=1.3; # for reynolds number 25300,using fig.6\n",
-    "Ds=10.02/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.0517; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.08; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.7 pgno:166"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.7 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  1050.97060273\n",
-      "\t coefficient of t**2 is :  1\n",
-      "\t coefficient of t is :  -556\n",
-      "\t constant term is :  73733.0293973\n",
-      "\t t is : [ 0.00457855  0.00296217]\n",
-      "\t t cannot be greater than 328F t is 218F \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.7 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "U=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "TP=328; # F\n",
-    "TE=228; # F\n",
-    "#solution\n",
-    "import numpy\n",
-    "\n",
-    "CP=(0.30/(888.8*1000));\n",
-    "CE=(0.05/(960*1000));\n",
-    "CF=1.20;\n",
-    "theta=8000; # annual hours\n",
-    "X=((CF*(TP-TE))/((CP-CE)*U*theta)); # from eq 7.53\n",
-    "print\"\\t X is : \",X\n",
-    "a=(1); # coefficient of t**2\n",
-    "b=(-556); # coefficient of t\n",
-    "c=(74784-X); # constant\n",
-    "print\"\\t coefficient of t**2 is : \",a\n",
-    "print\"\\t coefficient of t is : \",b\n",
-    "print\"\\t constant term is : \",c\n",
-    "P=numpy.array([c, b, a])\n",
-    "t=numpy.roots(P)\n",
-    "print\"\\t t is :\",t\n",
-    "print\"\\t t cannot be greater than 328F t is 218F \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.8 pgno:167"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "ascii\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  3784000.0\n",
-      "\t for steam \n",
-      "\n",
-      "\t total heat required for steam is :  Btu/hr  3792395.0\n",
-      "\t delt1 is :  F  128.0\n",
-      "\t delt2 is :  F  106.0\n",
-      "\t LMTD is : F  116.654454302\n",
-      "\t R is :  0.0\n",
-      "\t delt is :  F  116.654454302\n",
-      "\t hot fluid:tube side,steam \n",
-      "\t flow area is :  ft**2  0.0796944444444\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  49564.3081213\n",
-      "\t reynolds number is :  82671.1836992\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1500\n",
-      "\t cold fluid:shell side,sugar solution \n",
-      "\n",
-      "\t flow area is :  ft**2  0.551953125\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  362349.610757\n",
-      "\t De is :  ft  0.148026315789\n",
-      "\t reynolds number is :  17049.3572499\n",
-      "\t Pr is : 1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  138.3504\n",
-      "\t phys is :  1.13996690865\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  157.714877798\n",
-      "\t tw is :  F  218.119942108\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  142.70989533\n",
-      "\t total surface area is :  ft**2  238.7008\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  136.194122026\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000335238210724\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  2.8\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t De1 is :  ft 0.122\n",
-      "\t Res1 is :  14084.0\n",
-      "\t delPs is :  psi  0.07\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=228.; # inlet hot fluid,F\n",
-    "T2=228.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=122.; # outlet cold fluid,F\n",
-    "W=200000.; # lb/hr\n",
-    "w=3950.; # lb/hr\n",
-    "#solution\n",
-    "import sys\n",
-    "print sys.getdefaultencoding()\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.2*0.30)+(0.8*1); # bcoz of 20 percent solution,Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for steam \\n\"\n",
-    "l=960.1; # latent heat of condensation,Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "delt=(LMTD); # when R=0,F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "\n",
-    "ta=111; #F\n",
-    "Ta=228; #f\n",
-    "print\"\\t hot fluid:tube side,steam \"\n",
-    "Nt=76;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)b\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=0.0128*2.42; # at 228F,lb/(ft)*(hr)\n",
-    "D=(0.62/12); # from table 10,ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hio=1500; # for condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "print\"\\t cold fluid:shell side,sugar solution \\n\"\n",
-    "ID=12; # in\n",
-    "d=0.75/12; # diameter of tube,ft\n",
-    "Nt=76; # number of tubes\n",
-    "As=((3.14*(12**2)/4)-(76*3.14*(0.75**2)/4))/144; # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.30*2.42; # at 111F,lb/(ft)*(hr), from fig.14\n",
-    "De=((4*As)/(Nt*3.14*d)); # from eq.6.3,ft\n",
-    "print\"\\t De is :  ft \",De\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=61.5; # from fig.24, tube side data\n",
-    "c=0.86; # Btu/(lb)*(F),at 111F,from fig.4\n",
-    "k=0.333; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "muw=0.51*2.42; #  at 210F,lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "tw=(ta)+(((hio)/(hio+Ho))*(Ta-ta)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000155; # friction factor for reynolds number 82500, using fig.26\n",
-    "s=0.0008;\n",
-    "phyt=1;\n",
-    "D=0.0517; \n",
-    "delPt=((f*(Gt**2)*(L)*(2))/(5.22*(10**10)*(D)*(s)*(phyt)))/2; # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "De1=((4*As)/((Nt*3.14*d)+(3.14*1))); # from eq.6.4,ft\n",
-    "print\"\\t De1 is :  ft\",round(De1,3)\n",
-    "Res1=(De1*Gs/mu1); # from eq 7.3\n",
-    "print\"\\t Res1 is : \",round(Res1)\n",
-    "f=0.00025; # friction factor, using fig.26\n",
-    "s=1.08; # for reynolds number 25300,using fig.6\n",
-    "delPs=((f*(Gs**2)*(L)*(1))/(5.22*(10**10)*(De1)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",round(delPs,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.9 pgno:170"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.9 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  0.628360498562\n",
-      "\t R is :  2.77815829528\n",
-      "\t t2 is :  F  176.85\n",
-      "\t T2 is :  F  176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.9 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390; # F\n",
-    "t1=100; # F\n",
-    "U=69.3; # Btu/(hr)*(ft^2)*(F)\n",
-    "A=662; # ft^2\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "C=0.60; # Btu/(lb)*(F)\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "#solution\n",
-    "X=((U*A)/(w*c));\n",
-    "print\"\\t X is : \",X\n",
-    "R=((w*c)/(W*C));\n",
-    "print\"\\t R is : \",R\n",
-    "S=0.265; # from fig 7.25, by comparing X an R\n",
-    "t2=(t1)+((0.265)*(T1-t1)); # S=((t2-t1)/(T1-t1))\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "T2=((T1)-((R)*(t2-t1))); # R=((T1-T2)/(t2-t1))\n",
-    "print\"\\t T2 is :  F \",round(T2)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_1.ipynb
deleted file mode 100755
index 697d628e..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_1.ipynb
+++ /dev/null
@@ -1,1075 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 7 Parallel-Counter flow:Shell and Tube Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.1 pgno:139"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.1 \n",
-      "\n",
-      "\t equivalent diameter is :  in  0.95\n",
-      "\t De is :  in  0.079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.1 \\n\"\n",
-    "#given\n",
-    "PT=1; # square pitch,in\n",
-    "do=0.75; # outer diameter,in\n",
-    "#solution\n",
-    "de=((4*(PT**2-(3.14*do**2/4)))/(3.14*do));\n",
-    "print\"\\t equivalent diameter is :  in \",round(de,2)\n",
-    "De=(de/12); # ft\n",
-    "print\"\\t De is :  in \",round(De,3)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.2 pgno:147"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.2 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t considering 50F approach \n",
-      "\t t2 is :  F  200.0\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100.0\n",
-      "\t R is :  1.0\n",
-      "\t S is :  0.4\n",
-      "\t FT is 0.925 \n",
-      "\t considering 0F approach \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.80 \n",
-      "\t considering 20F cross \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.64 \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.2 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "print\"\\t considering 50F approach \"\n",
-    "#given\n",
-    "T1=350.; #F\n",
-    "T2=250.; #F\n",
-    "t2=T2-50.; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "t2=200.;\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2);# F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=100.;\n",
-    "#solution\n",
-    "\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.925 \" # from fig 18\n",
-    "print\"\\t considering 0F approach \"\n",
-    "T1=300; #F\n",
-    "T2=200; #F\n",
-    "t2=T2-0; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.80 \" # from fig 18\n",
-    "print\"\\t considering 20F cross \"\n",
-    "T1=280; #F\n",
-    "T2=180; #F\n",
-    "t2=T2+20; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \\n\"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.64 \" # from fig 18\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.3 pgno:151"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\t for kerosene \n",
-      "\t total heat required for kerosene is :  Btu/hr  5034810.0\n",
-      "\t for crude oil \n",
-      "\t total heat required for mid continent crude is :  Btu/hr  5110700.0\n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  220.0\n",
-      "\t LMTD is : F  152.195928445\n",
-      "\t R is :  2.71428571429\n",
-      "\t S is :  0.241379310345\n",
-      "\t FT is 0.905 \n",
-      "\t delt is :  F  137.737315243\n",
-      "\t ratio of two local temperature difference is :  0.454545454545\n",
-      "\t caloric temperature of hot fluid is :  F  279.8\n",
-      "\t caloric temperature of cold fluid is :  F  129.4\n",
-      "\t hot fluid:shell side,kerosene \n",
-      "\t flow area is :  ft**2  0.147569444444\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  296809.411765\n",
-      "\t reynolds number is :  25296.2566845\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  86.2363636364\n",
-      "\t cold fluid:inner tube side,crude oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.141267361111\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1054737.61829\n",
-      "\t reynolds number is :  8172.03733177\n",
-      "\t Pr is :  1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F)  35.362962963\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  28.644\n",
-      "\t phyt is :  1.1303932977\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  32.3789856193\n",
-      "\t tw is :  F  242.299617309\n",
-      "\t phys is :  0.953986161765\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  82.26829755\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  23.2344278003\n",
-      "\t total surface area is :  ft**2  661.8304\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  56.0637396161\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.0252027385623\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are : 38\n",
-      "\t delPs is :  psi  3.45911725247\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  6.13806896405\n",
-      "\t delPr is :  psi  2.89156626506\n",
-      "\t delPT is :  psi  9.03\n",
-      "\t allowable delPs is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=170.; # outlet cold fluid,F\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for kerosene \"\n",
-    "c=0.605; # Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \",Q1 # calculation mistake in problem\n",
-    "print\"\\t for crude oil \"\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for mid continent crude is :  Btu/hr \",Q # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.905 \" # from fig 18\n",
-    "delt=(0.905*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X \n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,kerosene \"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.40*2.42; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=93; # from fig.28\n",
-    "c=0.59; # Btu/(lb)*(F),at 280F,from fig.4\n",
-    "k=0.0765; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\n\"\n",
-    "D=0.0675; # ft\n",
-    "Nt=158;\n",
-    "n=4; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.515; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=3.6*2.42; # at 129F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "jH=31; # from fig.24\n",
-    "c=0.49; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \",Hi\n",
-    "ID=0.81; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=1.5*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is : \",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "muw=0.56*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.00175; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.73; # for reynolds number 25300,using fig.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.000285; # friction factor for reynolds number 8220, using fig.26\n",
-    "s=0.83;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.15; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,2)\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.4 pgno:155"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.4 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for distilled water \n",
-      "\t total heat required for distilled water is : Btu/hr  1400000.0\n",
-      "\t for raw water \n",
-      "\t total heat required for raw water is :  Btu/hr  1400000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  13.0\n",
-      "\t LMTD is : F  11.4344840601\n",
-      "\t R is :   1.6\n",
-      "\t S is :  0.277777777778\n",
-      "\t FT is 0.945 \n",
-      "\t delt is :  F  10.8055874368\n",
-      "\t ratio of two local temperature difference is :  0.769230769231\n",
-      "\t caloric temperature of hot fluid is :  F  89.0\n",
-      "\t caloric temperature of cold fluid is :  F  77.5\n",
-      "\t hot fluid:shell side,distilled water \n",
-      "\t flow area is :  ft**2  0.254166666667\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  688524.590164\n",
-      "\t reynolds number is :  16099.0598149\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  573.381818182\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.185555555556\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1508982.03593\n",
-      "\t V is  fps  6.70658682635\n",
-      "\t reynolds number is :  36712.4177803\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1158.3\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  383.527824238\n",
-      "\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \n",
-      "\t total surface area is :  ft**2  502.528\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  257.821653196\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00127127741812\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  16\n",
-      "\t delPs is :  psi  7.65506963359\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  4.9\n",
-      "\t delPr is :  psi  2.6\n",
-      "\t delPT is :  psi  7.6\n",
-      "\t allowable delPT is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.4 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=93.; # inlet hot fluid,F\n",
-    "T2=85.; # outlet hot fluid,F\n",
-    "t1=75.; # inlet cold fluid,F\n",
-    "t2=80.; # outlet cold fluid,F\n",
-    "W=175000.; # lb/hr\n",
-    "w=280000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for distilled water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for distilled water is : Btu/hr \",Q\n",
-    "print\"\\t for raw water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for raw water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.945 \" # from fig 18\n",
-    "delt=(0.945*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X\n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,distilled water \"\n",
-    "ID=15.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.9375;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.81*2.42; # at 89F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=73; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 89F,from fig.table 4\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=160;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.334; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.92*2.42; # at 77.5F,lb/(ft)*(hr)\n",
-    "D=0.65/12; #ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=1350*0.99; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.65; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "print\"\\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \"\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 16200, using fig.29\n",
-    "s=1; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00019; # friction factor for reynolds number 36400, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.054; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "X1=0.33; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Exxample 7.5 pgno:159"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.5 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t delt1 is :  F  65.0\n",
-      "\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \n",
-      "\n",
-      "\t X is :  0.120481927711\n",
-      "\t Y is :  0.384615384615\n",
-      "\t delt2 is :  F  62.4\n",
-      "\t t2 is :  F  112.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.5 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=175.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "#solution\n",
-    "delt1=T2-t1; #F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "U=15; # assumption,Btu/(hr)*(ft^2)*(F)\n",
-    "theta=8000; # operating hours,hr\n",
-    "CW=(0.01/8300); # water cost,$/lb\n",
-    "print\"\\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \\n\"\n",
-    "CF=(0.3*4); # annual fixed charges/ft^2\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "X=((U)*(theta)*(CW)/(CF*c));\n",
-    "print\"\\t X is : \",X\n",
-    "Y=((T1-T2)/delt1);\n",
-    "print\"\\t Y is : \",Y\n",
-    "A=0.96; # A=(delt2/delt1), from fig 7.24\n",
-    "delt2=0.96*delt1;\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "t2=T1-delt2; # F\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.6 pgno:161"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.6 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  915667.2\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  915200.0\n",
-      "\t delt1 is :  F  22.0\n",
-      "\t delt2 is :  F  60.0\n",
-      "\t LMTD is : F  37.8749328485\n",
-      "\t R is :  2.72727272727\n",
-      "\t S is :  0.268292682927\n",
-      "\t FT is 0.81 \n",
-      "\t delt is :  F  30.6786956073\n",
-      "\t caloric temperature of hot fluid is : F 120.0\n",
-      "\t caloric temperature of cold fluid is :  F  79.0\n",
-      "\t hot fluid:shell side,phosphate solution \n",
-      "\t flow area is :  ft**2  0.0347916666667\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  579449.101796\n",
-      "\t reynolds number is :  15796.5061612\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  295.957894737\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.0545277777778\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  762913.907285\n",
-      "\t V is  fps  3.39072847682\n",
-      "\t reynolds number is :  17899.0185011\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  204.459014471\n",
-      "\t total surface area is :  ft**2  163.3216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  182.656652912\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000583796892885\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  96\n",
-      "\t delPs is :  psi  9.51887629626\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  1.58733222032\n",
-      "\t delPr is :  psi  0.6\n",
-      "\t delPT is :  psi  2.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.6 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=150.; # inlet hot fluid,F\n",
-    "T2=90.; # outlet hot fluid,F\n",
-    "t1=68.; # inlet cold fluid,F\n",
-    "t2=90.; # outlet cold fluid,F\n",
-    "W=20160.; # lb/hr\n",
-    "w=41600.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.3*0.19)+(0.7*1); # Btu/(lb)*(F), bcoz of 30 percent of solution\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.81 \" # from fig 18\n",
-    "delt=(0.81*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,phosphate solution \"\n",
-    "ID=10.02; # in\n",
-    "C=0.25; # clearance\n",
-    "B=2; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.20*2.42; # at 120F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=71; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 120F,from fig.table 4\n",
-    "k=0.33; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((0.757)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=52;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.91*2.42; # at 79F,lb/(ft)*(hr),from table 14\n",
-    "D=(0.62/12); # from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=800*1; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 15750, using fig.29\n",
-    "s=1.3; # for reynolds number 25300,using fig.6\n",
-    "Ds=10.02/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.0517; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.08; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.7 pgno:166"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.7 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  1050.97060273\n",
-      "\t coefficient of t**2 is :  1\n",
-      "\t coefficient of t is :  -556\n",
-      "\t constant term is :  73733.0293973\n",
-      "\t t is : [ 0.00457855  0.00296217]\n",
-      "\t t cannot be greater than 328F t is 218F \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.7 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "U=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "TP=328; # F\n",
-    "TE=228; # F\n",
-    "#solution\n",
-    "import numpy\n",
-    "\n",
-    "CP=(0.30/(888.8*1000));\n",
-    "CE=(0.05/(960*1000));\n",
-    "CF=1.20;\n",
-    "theta=8000; # annual hours\n",
-    "X=((CF*(TP-TE))/((CP-CE)*U*theta)); # from eq 7.53\n",
-    "print\"\\t X is : \",X\n",
-    "a=(1); # coefficient of t**2\n",
-    "b=(-556); # coefficient of t\n",
-    "c=(74784-X); # constant\n",
-    "print\"\\t coefficient of t**2 is : \",a\n",
-    "print\"\\t coefficient of t is : \",b\n",
-    "print\"\\t constant term is : \",c\n",
-    "P=numpy.array([c, b, a])\n",
-    "t=numpy.roots(P)\n",
-    "print\"\\t t is :\",t\n",
-    "print\"\\t t cannot be greater than 328F t is 218F \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.8 pgno:167"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "ascii\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  3784000.0\n",
-      "\t for steam \n",
-      "\n",
-      "\t total heat required for steam is :  Btu/hr  3792395.0\n",
-      "\t delt1 is :  F  128.0\n",
-      "\t delt2 is :  F  106.0\n",
-      "\t LMTD is : F  116.654454302\n",
-      "\t R is :  0.0\n",
-      "\t delt is :  F  116.654454302\n",
-      "\t hot fluid:tube side,steam \n",
-      "\t flow area is :  ft**2  0.0796944444444\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  49564.3081213\n",
-      "\t reynolds number is :  82671.1836992\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1500\n",
-      "\t cold fluid:shell side,sugar solution \n",
-      "\n",
-      "\t flow area is :  ft**2  0.551953125\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  362349.610757\n",
-      "\t De is :  ft  0.148026315789\n",
-      "\t reynolds number is :  17049.3572499\n",
-      "\t Pr is : 1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  138.3504\n",
-      "\t phys is :  1.13996690865\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  157.714877798\n",
-      "\t tw is :  F  218.119942108\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  142.70989533\n",
-      "\t total surface area is :  ft**2  238.7008\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  136.194122026\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000335238210724\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  2.8\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t De1 is :  ft 0.122\n",
-      "\t Res1 is :  14084.0\n",
-      "\t delPs is :  psi  0.07\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=228.; # inlet hot fluid,F\n",
-    "T2=228.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=122.; # outlet cold fluid,F\n",
-    "W=200000.; # lb/hr\n",
-    "w=3950.; # lb/hr\n",
-    "#solution\n",
-    "import sys\n",
-    "print sys.getdefaultencoding()\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.2*0.30)+(0.8*1); # bcoz of 20 percent solution,Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for steam \\n\"\n",
-    "l=960.1; # latent heat of condensation,Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "delt=(LMTD); # when R=0,F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "\n",
-    "ta=111; #F\n",
-    "Ta=228; #f\n",
-    "print\"\\t hot fluid:tube side,steam \"\n",
-    "Nt=76;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)b\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=0.0128*2.42; # at 228F,lb/(ft)*(hr)\n",
-    "D=(0.62/12); # from table 10,ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hio=1500; # for condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "print\"\\t cold fluid:shell side,sugar solution \\n\"\n",
-    "ID=12; # in\n",
-    "d=0.75/12; # diameter of tube,ft\n",
-    "Nt=76; # number of tubes\n",
-    "As=((3.14*(12**2)/4)-(76*3.14*(0.75**2)/4))/144; # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.30*2.42; # at 111F,lb/(ft)*(hr), from fig.14\n",
-    "De=((4*As)/(Nt*3.14*d)); # from eq.6.3,ft\n",
-    "print\"\\t De is :  ft \",De\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=61.5; # from fig.24, tube side data\n",
-    "c=0.86; # Btu/(lb)*(F),at 111F,from fig.4\n",
-    "k=0.333; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "muw=0.51*2.42; #  at 210F,lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "tw=(ta)+(((hio)/(hio+Ho))*(Ta-ta)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000155; # friction factor for reynolds number 82500, using fig.26\n",
-    "s=0.0008;\n",
-    "phyt=1;\n",
-    "D=0.0517; \n",
-    "delPt=((f*(Gt**2)*(L)*(2))/(5.22*(10**10)*(D)*(s)*(phyt)))/2; # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "De1=((4*As)/((Nt*3.14*d)+(3.14*1))); # from eq.6.4,ft\n",
-    "print\"\\t De1 is :  ft\",round(De1,3)\n",
-    "Res1=(De1*Gs/mu1); # from eq 7.3\n",
-    "print\"\\t Res1 is : \",round(Res1)\n",
-    "f=0.00025; # friction factor, using fig.26\n",
-    "s=1.08; # for reynolds number 25300,using fig.6\n",
-    "delPs=((f*(Gs**2)*(L)*(1))/(5.22*(10**10)*(De1)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",round(delPs,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.9 pgno:170"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.9 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  0.628360498562\n",
-      "\t R is :  2.77815829528\n",
-      "\t t2 is :  F  176.85\n",
-      "\t T2 is :  F  176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.9 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390; # F\n",
-    "t1=100; # F\n",
-    "U=69.3; # Btu/(hr)*(ft^2)*(F)\n",
-    "A=662; # ft^2\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "C=0.60; # Btu/(lb)*(F)\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "#solution\n",
-    "X=((U*A)/(w*c));\n",
-    "print\"\\t X is : \",X\n",
-    "R=((w*c)/(W*C));\n",
-    "print\"\\t R is : \",R\n",
-    "S=0.265; # from fig 7.25, by comparing X an R\n",
-    "t2=(t1)+((0.265)*(T1-t1)); # S=((t2-t1)/(T1-t1))\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "T2=((T1)-((R)*(t2-t1))); # R=((T1-T2)/(t2-t1))\n",
-    "print\"\\t T2 is :  F \",round(T2)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_2.ipynb
deleted file mode 100755
index 697d628e..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_2.ipynb
+++ /dev/null
@@ -1,1075 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 7 Parallel-Counter flow:Shell and Tube Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.1 pgno:139"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.1 \n",
-      "\n",
-      "\t equivalent diameter is :  in  0.95\n",
-      "\t De is :  in  0.079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.1 \\n\"\n",
-    "#given\n",
-    "PT=1; # square pitch,in\n",
-    "do=0.75; # outer diameter,in\n",
-    "#solution\n",
-    "de=((4*(PT**2-(3.14*do**2/4)))/(3.14*do));\n",
-    "print\"\\t equivalent diameter is :  in \",round(de,2)\n",
-    "De=(de/12); # ft\n",
-    "print\"\\t De is :  in \",round(De,3)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.2 pgno:147"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.2 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t considering 50F approach \n",
-      "\t t2 is :  F  200.0\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100.0\n",
-      "\t R is :  1.0\n",
-      "\t S is :  0.4\n",
-      "\t FT is 0.925 \n",
-      "\t considering 0F approach \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.80 \n",
-      "\t considering 20F cross \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.64 \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.2 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "print\"\\t considering 50F approach \"\n",
-    "#given\n",
-    "T1=350.; #F\n",
-    "T2=250.; #F\n",
-    "t2=T2-50.; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "t2=200.;\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2);# F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=100.;\n",
-    "#solution\n",
-    "\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.925 \" # from fig 18\n",
-    "print\"\\t considering 0F approach \"\n",
-    "T1=300; #F\n",
-    "T2=200; #F\n",
-    "t2=T2-0; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.80 \" # from fig 18\n",
-    "print\"\\t considering 20F cross \"\n",
-    "T1=280; #F\n",
-    "T2=180; #F\n",
-    "t2=T2+20; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \\n\"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.64 \" # from fig 18\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.3 pgno:151"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\t for kerosene \n",
-      "\t total heat required for kerosene is :  Btu/hr  5034810.0\n",
-      "\t for crude oil \n",
-      "\t total heat required for mid continent crude is :  Btu/hr  5110700.0\n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  220.0\n",
-      "\t LMTD is : F  152.195928445\n",
-      "\t R is :  2.71428571429\n",
-      "\t S is :  0.241379310345\n",
-      "\t FT is 0.905 \n",
-      "\t delt is :  F  137.737315243\n",
-      "\t ratio of two local temperature difference is :  0.454545454545\n",
-      "\t caloric temperature of hot fluid is :  F  279.8\n",
-      "\t caloric temperature of cold fluid is :  F  129.4\n",
-      "\t hot fluid:shell side,kerosene \n",
-      "\t flow area is :  ft**2  0.147569444444\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  296809.411765\n",
-      "\t reynolds number is :  25296.2566845\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  86.2363636364\n",
-      "\t cold fluid:inner tube side,crude oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.141267361111\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1054737.61829\n",
-      "\t reynolds number is :  8172.03733177\n",
-      "\t Pr is :  1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F)  35.362962963\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  28.644\n",
-      "\t phyt is :  1.1303932977\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  32.3789856193\n",
-      "\t tw is :  F  242.299617309\n",
-      "\t phys is :  0.953986161765\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  82.26829755\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  23.2344278003\n",
-      "\t total surface area is :  ft**2  661.8304\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  56.0637396161\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.0252027385623\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are : 38\n",
-      "\t delPs is :  psi  3.45911725247\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  6.13806896405\n",
-      "\t delPr is :  psi  2.89156626506\n",
-      "\t delPT is :  psi  9.03\n",
-      "\t allowable delPs is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=170.; # outlet cold fluid,F\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for kerosene \"\n",
-    "c=0.605; # Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \",Q1 # calculation mistake in problem\n",
-    "print\"\\t for crude oil \"\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for mid continent crude is :  Btu/hr \",Q # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.905 \" # from fig 18\n",
-    "delt=(0.905*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X \n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,kerosene \"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.40*2.42; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=93; # from fig.28\n",
-    "c=0.59; # Btu/(lb)*(F),at 280F,from fig.4\n",
-    "k=0.0765; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\n\"\n",
-    "D=0.0675; # ft\n",
-    "Nt=158;\n",
-    "n=4; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.515; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=3.6*2.42; # at 129F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "jH=31; # from fig.24\n",
-    "c=0.49; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \",Hi\n",
-    "ID=0.81; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=1.5*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is : \",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "muw=0.56*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.00175; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.73; # for reynolds number 25300,using fig.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.000285; # friction factor for reynolds number 8220, using fig.26\n",
-    "s=0.83;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.15; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,2)\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.4 pgno:155"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.4 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for distilled water \n",
-      "\t total heat required for distilled water is : Btu/hr  1400000.0\n",
-      "\t for raw water \n",
-      "\t total heat required for raw water is :  Btu/hr  1400000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  13.0\n",
-      "\t LMTD is : F  11.4344840601\n",
-      "\t R is :   1.6\n",
-      "\t S is :  0.277777777778\n",
-      "\t FT is 0.945 \n",
-      "\t delt is :  F  10.8055874368\n",
-      "\t ratio of two local temperature difference is :  0.769230769231\n",
-      "\t caloric temperature of hot fluid is :  F  89.0\n",
-      "\t caloric temperature of cold fluid is :  F  77.5\n",
-      "\t hot fluid:shell side,distilled water \n",
-      "\t flow area is :  ft**2  0.254166666667\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  688524.590164\n",
-      "\t reynolds number is :  16099.0598149\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  573.381818182\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.185555555556\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1508982.03593\n",
-      "\t V is  fps  6.70658682635\n",
-      "\t reynolds number is :  36712.4177803\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1158.3\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  383.527824238\n",
-      "\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \n",
-      "\t total surface area is :  ft**2  502.528\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  257.821653196\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00127127741812\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  16\n",
-      "\t delPs is :  psi  7.65506963359\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  4.9\n",
-      "\t delPr is :  psi  2.6\n",
-      "\t delPT is :  psi  7.6\n",
-      "\t allowable delPT is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.4 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=93.; # inlet hot fluid,F\n",
-    "T2=85.; # outlet hot fluid,F\n",
-    "t1=75.; # inlet cold fluid,F\n",
-    "t2=80.; # outlet cold fluid,F\n",
-    "W=175000.; # lb/hr\n",
-    "w=280000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for distilled water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for distilled water is : Btu/hr \",Q\n",
-    "print\"\\t for raw water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for raw water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.945 \" # from fig 18\n",
-    "delt=(0.945*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X\n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,distilled water \"\n",
-    "ID=15.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.9375;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.81*2.42; # at 89F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=73; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 89F,from fig.table 4\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=160;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.334; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.92*2.42; # at 77.5F,lb/(ft)*(hr)\n",
-    "D=0.65/12; #ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=1350*0.99; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.65; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "print\"\\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \"\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 16200, using fig.29\n",
-    "s=1; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00019; # friction factor for reynolds number 36400, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.054; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "X1=0.33; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Exxample 7.5 pgno:159"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.5 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t delt1 is :  F  65.0\n",
-      "\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \n",
-      "\n",
-      "\t X is :  0.120481927711\n",
-      "\t Y is :  0.384615384615\n",
-      "\t delt2 is :  F  62.4\n",
-      "\t t2 is :  F  112.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.5 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=175.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "#solution\n",
-    "delt1=T2-t1; #F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "U=15; # assumption,Btu/(hr)*(ft^2)*(F)\n",
-    "theta=8000; # operating hours,hr\n",
-    "CW=(0.01/8300); # water cost,$/lb\n",
-    "print\"\\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \\n\"\n",
-    "CF=(0.3*4); # annual fixed charges/ft^2\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "X=((U)*(theta)*(CW)/(CF*c));\n",
-    "print\"\\t X is : \",X\n",
-    "Y=((T1-T2)/delt1);\n",
-    "print\"\\t Y is : \",Y\n",
-    "A=0.96; # A=(delt2/delt1), from fig 7.24\n",
-    "delt2=0.96*delt1;\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "t2=T1-delt2; # F\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.6 pgno:161"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.6 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  915667.2\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  915200.0\n",
-      "\t delt1 is :  F  22.0\n",
-      "\t delt2 is :  F  60.0\n",
-      "\t LMTD is : F  37.8749328485\n",
-      "\t R is :  2.72727272727\n",
-      "\t S is :  0.268292682927\n",
-      "\t FT is 0.81 \n",
-      "\t delt is :  F  30.6786956073\n",
-      "\t caloric temperature of hot fluid is : F 120.0\n",
-      "\t caloric temperature of cold fluid is :  F  79.0\n",
-      "\t hot fluid:shell side,phosphate solution \n",
-      "\t flow area is :  ft**2  0.0347916666667\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  579449.101796\n",
-      "\t reynolds number is :  15796.5061612\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  295.957894737\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.0545277777778\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  762913.907285\n",
-      "\t V is  fps  3.39072847682\n",
-      "\t reynolds number is :  17899.0185011\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  204.459014471\n",
-      "\t total surface area is :  ft**2  163.3216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  182.656652912\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000583796892885\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  96\n",
-      "\t delPs is :  psi  9.51887629626\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  1.58733222032\n",
-      "\t delPr is :  psi  0.6\n",
-      "\t delPT is :  psi  2.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.6 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=150.; # inlet hot fluid,F\n",
-    "T2=90.; # outlet hot fluid,F\n",
-    "t1=68.; # inlet cold fluid,F\n",
-    "t2=90.; # outlet cold fluid,F\n",
-    "W=20160.; # lb/hr\n",
-    "w=41600.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.3*0.19)+(0.7*1); # Btu/(lb)*(F), bcoz of 30 percent of solution\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.81 \" # from fig 18\n",
-    "delt=(0.81*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,phosphate solution \"\n",
-    "ID=10.02; # in\n",
-    "C=0.25; # clearance\n",
-    "B=2; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.20*2.42; # at 120F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=71; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 120F,from fig.table 4\n",
-    "k=0.33; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((0.757)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=52;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.91*2.42; # at 79F,lb/(ft)*(hr),from table 14\n",
-    "D=(0.62/12); # from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=800*1; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 15750, using fig.29\n",
-    "s=1.3; # for reynolds number 25300,using fig.6\n",
-    "Ds=10.02/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.0517; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.08; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.7 pgno:166"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.7 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  1050.97060273\n",
-      "\t coefficient of t**2 is :  1\n",
-      "\t coefficient of t is :  -556\n",
-      "\t constant term is :  73733.0293973\n",
-      "\t t is : [ 0.00457855  0.00296217]\n",
-      "\t t cannot be greater than 328F t is 218F \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.7 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "U=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "TP=328; # F\n",
-    "TE=228; # F\n",
-    "#solution\n",
-    "import numpy\n",
-    "\n",
-    "CP=(0.30/(888.8*1000));\n",
-    "CE=(0.05/(960*1000));\n",
-    "CF=1.20;\n",
-    "theta=8000; # annual hours\n",
-    "X=((CF*(TP-TE))/((CP-CE)*U*theta)); # from eq 7.53\n",
-    "print\"\\t X is : \",X\n",
-    "a=(1); # coefficient of t**2\n",
-    "b=(-556); # coefficient of t\n",
-    "c=(74784-X); # constant\n",
-    "print\"\\t coefficient of t**2 is : \",a\n",
-    "print\"\\t coefficient of t is : \",b\n",
-    "print\"\\t constant term is : \",c\n",
-    "P=numpy.array([c, b, a])\n",
-    "t=numpy.roots(P)\n",
-    "print\"\\t t is :\",t\n",
-    "print\"\\t t cannot be greater than 328F t is 218F \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.8 pgno:167"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "ascii\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  3784000.0\n",
-      "\t for steam \n",
-      "\n",
-      "\t total heat required for steam is :  Btu/hr  3792395.0\n",
-      "\t delt1 is :  F  128.0\n",
-      "\t delt2 is :  F  106.0\n",
-      "\t LMTD is : F  116.654454302\n",
-      "\t R is :  0.0\n",
-      "\t delt is :  F  116.654454302\n",
-      "\t hot fluid:tube side,steam \n",
-      "\t flow area is :  ft**2  0.0796944444444\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  49564.3081213\n",
-      "\t reynolds number is :  82671.1836992\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1500\n",
-      "\t cold fluid:shell side,sugar solution \n",
-      "\n",
-      "\t flow area is :  ft**2  0.551953125\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  362349.610757\n",
-      "\t De is :  ft  0.148026315789\n",
-      "\t reynolds number is :  17049.3572499\n",
-      "\t Pr is : 1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  138.3504\n",
-      "\t phys is :  1.13996690865\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  157.714877798\n",
-      "\t tw is :  F  218.119942108\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  142.70989533\n",
-      "\t total surface area is :  ft**2  238.7008\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  136.194122026\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000335238210724\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  2.8\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t De1 is :  ft 0.122\n",
-      "\t Res1 is :  14084.0\n",
-      "\t delPs is :  psi  0.07\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=228.; # inlet hot fluid,F\n",
-    "T2=228.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=122.; # outlet cold fluid,F\n",
-    "W=200000.; # lb/hr\n",
-    "w=3950.; # lb/hr\n",
-    "#solution\n",
-    "import sys\n",
-    "print sys.getdefaultencoding()\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.2*0.30)+(0.8*1); # bcoz of 20 percent solution,Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for steam \\n\"\n",
-    "l=960.1; # latent heat of condensation,Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "delt=(LMTD); # when R=0,F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "\n",
-    "ta=111; #F\n",
-    "Ta=228; #f\n",
-    "print\"\\t hot fluid:tube side,steam \"\n",
-    "Nt=76;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)b\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=0.0128*2.42; # at 228F,lb/(ft)*(hr)\n",
-    "D=(0.62/12); # from table 10,ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hio=1500; # for condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "print\"\\t cold fluid:shell side,sugar solution \\n\"\n",
-    "ID=12; # in\n",
-    "d=0.75/12; # diameter of tube,ft\n",
-    "Nt=76; # number of tubes\n",
-    "As=((3.14*(12**2)/4)-(76*3.14*(0.75**2)/4))/144; # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.30*2.42; # at 111F,lb/(ft)*(hr), from fig.14\n",
-    "De=((4*As)/(Nt*3.14*d)); # from eq.6.3,ft\n",
-    "print\"\\t De is :  ft \",De\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=61.5; # from fig.24, tube side data\n",
-    "c=0.86; # Btu/(lb)*(F),at 111F,from fig.4\n",
-    "k=0.333; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "muw=0.51*2.42; #  at 210F,lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "tw=(ta)+(((hio)/(hio+Ho))*(Ta-ta)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000155; # friction factor for reynolds number 82500, using fig.26\n",
-    "s=0.0008;\n",
-    "phyt=1;\n",
-    "D=0.0517; \n",
-    "delPt=((f*(Gt**2)*(L)*(2))/(5.22*(10**10)*(D)*(s)*(phyt)))/2; # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "De1=((4*As)/((Nt*3.14*d)+(3.14*1))); # from eq.6.4,ft\n",
-    "print\"\\t De1 is :  ft\",round(De1,3)\n",
-    "Res1=(De1*Gs/mu1); # from eq 7.3\n",
-    "print\"\\t Res1 is : \",round(Res1)\n",
-    "f=0.00025; # friction factor, using fig.26\n",
-    "s=1.08; # for reynolds number 25300,using fig.6\n",
-    "delPs=((f*(Gs**2)*(L)*(1))/(5.22*(10**10)*(De1)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",round(delPs,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.9 pgno:170"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.9 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  0.628360498562\n",
-      "\t R is :  2.77815829528\n",
-      "\t t2 is :  F  176.85\n",
-      "\t T2 is :  F  176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.9 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390; # F\n",
-    "t1=100; # F\n",
-    "U=69.3; # Btu/(hr)*(ft^2)*(F)\n",
-    "A=662; # ft^2\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "C=0.60; # Btu/(lb)*(F)\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "#solution\n",
-    "X=((U*A)/(w*c));\n",
-    "print\"\\t X is : \",X\n",
-    "R=((w*c)/(W*C));\n",
-    "print\"\\t R is : \",R\n",
-    "S=0.265; # from fig 7.25, by comparing X an R\n",
-    "t2=(t1)+((0.265)*(T1-t1)); # S=((t2-t1)/(T1-t1))\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "T2=((T1)-((R)*(t2-t1))); # R=((T1-T2)/(t2-t1))\n",
-    "print\"\\t T2 is :  F \",round(T2)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_3.ipynb
deleted file mode 100755
index 697d628e..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_7_Parallel-Counter_flow_Shell_and_Tube_Exchangers_3.ipynb
+++ /dev/null
@@ -1,1075 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 7 Parallel-Counter flow:Shell and Tube Exchangers"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.1 pgno:139"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 25,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.1 \n",
-      "\n",
-      "\t equivalent diameter is :  in  0.95\n",
-      "\t De is :  in  0.079\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.1 \\n\"\n",
-    "#given\n",
-    "PT=1; # square pitch,in\n",
-    "do=0.75; # outer diameter,in\n",
-    "#solution\n",
-    "de=((4*(PT**2-(3.14*do**2/4)))/(3.14*do));\n",
-    "print\"\\t equivalent diameter is :  in \",round(de,2)\n",
-    "De=(de/12); # ft\n",
-    "print\"\\t De is :  in \",round(De,3)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.2 pgno:147"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 26,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.2 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t considering 50F approach \n",
-      "\t t2 is :  F  200.0\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100.0\n",
-      "\t R is :  1.0\n",
-      "\t S is :  0.4\n",
-      "\t FT is 0.925 \n",
-      "\t considering 0F approach \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.80 \n",
-      "\t considering 20F cross \n",
-      "\t t2 is :  F  200\n",
-      "\t fluids are with equal ranges,so \n",
-      "\n",
-      "\t t1 is :  F  100\n",
-      "\t R is :  1\n",
-      "\t S is :  0\n",
-      "\t FT is 0.64 \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.2 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "print\"\\t considering 50F approach \"\n",
-    "#given\n",
-    "T1=350.; #F\n",
-    "T2=250.; #F\n",
-    "t2=T2-50.; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "t2=200.;\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2);# F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "t1=100.;\n",
-    "#solution\n",
-    "\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.925 \" # from fig 18\n",
-    "print\"\\t considering 0F approach \"\n",
-    "T1=300; #F\n",
-    "T2=200; #F\n",
-    "t2=T2-0; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.80 \" # from fig 18\n",
-    "print\"\\t considering 20F cross \"\n",
-    "T1=280; #F\n",
-    "T2=180; #F\n",
-    "t2=T2+20; # formula for approach,f\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "print\"\\t fluids are with equal ranges,so \\n\"\n",
-    "t1=t2-(T1-T2); # F\n",
-    "print\"\\t t1 is :  F \",t1\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.64 \" # from fig 18\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.3 pgno:151"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 27,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.3 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\t for kerosene \n",
-      "\t total heat required for kerosene is :  Btu/hr  5034810.0\n",
-      "\t for crude oil \n",
-      "\t total heat required for mid continent crude is :  Btu/hr  5110700.0\n",
-      "\t delt1 is :  F  100.0\n",
-      "\t delt2 is :  F  220.0\n",
-      "\t LMTD is : F  152.195928445\n",
-      "\t R is :  2.71428571429\n",
-      "\t S is :  0.241379310345\n",
-      "\t FT is 0.905 \n",
-      "\t delt is :  F  137.737315243\n",
-      "\t ratio of two local temperature difference is :  0.454545454545\n",
-      "\t caloric temperature of hot fluid is :  F  279.8\n",
-      "\t caloric temperature of cold fluid is :  F  129.4\n",
-      "\t hot fluid:shell side,kerosene \n",
-      "\t flow area is :  ft**2  0.147569444444\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  296809.411765\n",
-      "\t reynolds number is :  25296.2566845\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  86.2363636364\n",
-      "\t cold fluid:inner tube side,crude oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.141267361111\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1054737.61829\n",
-      "\t reynolds number is :  8172.03733177\n",
-      "\t Pr is :  1.0\n",
-      "\t Hi is :  Btu/(hr)*(ft**2)*(F)  35.362962963\n",
-      "\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  28.644\n",
-      "\t phyt is :  1.1303932977\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  32.3789856193\n",
-      "\t tw is :  F  242.299617309\n",
-      "\t phys is :  0.953986161765\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  82.26829755\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  23.2344278003\n",
-      "\t total surface area is :  ft**2  661.8304\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  56.0637396161\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  -0.0252027385623\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are : 38\n",
-      "\t delPs is :  psi  3.45911725247\n",
-      "\t allowable delPa is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  6.13806896405\n",
-      "\t delPr is :  psi  2.89156626506\n",
-      "\t delPT is :  psi  9.03\n",
-      "\t allowable delPs is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.3 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390.; # inlet hot fluid,F\n",
-    "T2=200.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=170.; # outlet cold fluid,F\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for kerosene \"\n",
-    "c=0.605; # Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for kerosene is :  Btu/hr \",Q1 # calculation mistake in problem\n",
-    "print\"\\t for crude oil \"\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for mid continent crude is :  Btu/hr \",Q # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.905 \" # from fig 18\n",
-    "delt=(0.905*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X \n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling \n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,kerosene \"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.40*2.42; # at 280F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=93; # from fig.28\n",
-    "c=0.59; # Btu/(lb)*(F),at 280F,from fig.4\n",
-    "k=0.0765; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "print\"\\t cold fluid:inner tube side,crude oil \\n\"\n",
-    "D=0.0675; # ft\n",
-    "Nt=158;\n",
-    "n=4; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.515; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=3.6*2.42; # at 129F,lb/(ft)*(hr)\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "jH=31; # from fig.24\n",
-    "c=0.49; # Btu/(lb)*(F),at 304F,from fig.4\n",
-    "k=0.077; # Btu/(hr)*(ft**2)*(F/ft), from fig.1\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "Hi=((jH)*(k/D)*(Pr)*(1**0.14)); #Hi=(hi/phyp),using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t Hi is :  Btu/(hr)*(ft**2)*(F) \",Hi\n",
-    "ID=0.81; # ft\n",
-    "OD=1; #ft\n",
-    "Hio=((Hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct Hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",Hio\n",
-    "muw=1.5*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phyt=(mu2/muw)**0.14;\n",
-    "print\"\\t phyt is : \",phyt # from fig.24\n",
-    "hio=(Hio)*(phyt); # from eq.6.37\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(Hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "muw=0.56*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.00175; # friction factor for reynolds number 25300, using fig.29\n",
-    "s=0.73; # for reynolds number 25300,using fig.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPa is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.000285; # friction factor for reynolds number 8220, using fig.26\n",
-    "s=0.83;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.15; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",delPr\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,2)\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.4 pgno:155"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 28,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.4 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t 1.for heat balance \n",
-      "\t for distilled water \n",
-      "\t total heat required for distilled water is : Btu/hr  1400000.0\n",
-      "\t for raw water \n",
-      "\t total heat required for raw water is :  Btu/hr  1400000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  13.0\n",
-      "\t LMTD is : F  11.4344840601\n",
-      "\t R is :   1.6\n",
-      "\t S is :  0.277777777778\n",
-      "\t FT is 0.945 \n",
-      "\t delt is :  F  10.8055874368\n",
-      "\t ratio of two local temperature difference is :  0.769230769231\n",
-      "\t caloric temperature of hot fluid is :  F  89.0\n",
-      "\t caloric temperature of cold fluid is :  F  77.5\n",
-      "\t hot fluid:shell side,distilled water \n",
-      "\t flow area is :  ft**2  0.254166666667\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  688524.590164\n",
-      "\t reynolds number is :  16099.0598149\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  573.381818182\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.185555555556\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  1508982.03593\n",
-      "\t V is  fps  6.70658682635\n",
-      "\t reynolds number is :  36712.4177803\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1158.3\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  383.527824238\n",
-      "\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \n",
-      "\t total surface area is :  ft**2  502.528\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  257.821653196\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00127127741812\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  16\n",
-      "\t delPs is :  psi  7.65506963359\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  4.9\n",
-      "\t delPr is :  psi  2.6\n",
-      "\t delPT is :  psi  7.6\n",
-      "\t allowable delPT is 10 psi \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.4 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=93.; # inlet hot fluid,F\n",
-    "T2=85.; # outlet hot fluid,F\n",
-    "t1=75.; # inlet cold fluid,F\n",
-    "t2=80.; # outlet cold fluid,F\n",
-    "W=175000.; # lb/hr\n",
-    "w=280000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \"\n",
-    "print\"\\t for distilled water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for distilled water is : Btu/hr \",Q\n",
-    "print\"\\t for raw water \"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for raw water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.945 \" # from fig 18\n",
-    "delt=(0.945*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : \",X\n",
-    "Fc=0.42; # from fig.17\n",
-    "Kc=0.20; # crude oil controlling\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,distilled water \"\n",
-    "ID=15.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.9375;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=0.81*2.42; # at 89F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=73; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 89F,from fig.table 4\n",
-    "k=0.36; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=160;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.334; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.92*2.42; # at 77.5F,lb/(ft)*(hr)\n",
-    "D=0.65/12; #ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=1350*0.99; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.65; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "print\"\\t when both film coefficients are high the thermal resistance of the tube metal is not necessarily insignificant As Assumed in the derivation of Eq. (6.38). For a steel 1.8 BWG tube Rm= 0.00017 and for copper Rm= 0.000017 \"\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 16200, using fig.29\n",
-    "s=1; # for reynolds number 25300,using fig.6\n",
-    "Ds=15.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00019; # friction factor for reynolds number 36400, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.054; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "X1=0.33; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Exxample 7.5 pgno:159"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 29,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.5 \n",
-      "\t approximate values are mentioned in the book \n",
-      "\t delt1 is :  F  65.0\n",
-      "\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \n",
-      "\n",
-      "\t X is :  0.120481927711\n",
-      "\t Y is :  0.384615384615\n",
-      "\t delt2 is :  F  62.4\n",
-      "\t t2 is :  F  112.6\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.5 \"\n",
-    "print\"\\t approximate values are mentioned in the book \"\n",
-    "#given\n",
-    "T1=175.; # inlet hot fluid,F\n",
-    "T2=150.; # outlet hot fluid,F\n",
-    "t1=85.; # inlet cold fluid,F\n",
-    "#solution\n",
-    "delt1=T2-t1; #F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "U=15; # assumption,Btu/(hr)*(ft^2)*(F)\n",
-    "theta=8000; # operating hours,hr\n",
-    "CW=(0.01/8300); # water cost,$/lb\n",
-    "print\"\\t For annual charges assume 20 per cent repair and maintenanc.e and 10 per cent depreciation \\n\"\n",
-    "CF=(0.3*4); # annual fixed charges/ft^2\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "X=((U)*(theta)*(CW)/(CF*c));\n",
-    "print\"\\t X is : \",X\n",
-    "Y=((T1-T2)/delt1);\n",
-    "print\"\\t Y is : \",Y\n",
-    "A=0.96; # A=(delt2/delt1), from fig 7.24\n",
-    "delt2=0.96*delt1;\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "t2=T1-delt2; # F\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.6 pgno:161"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 30,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.6 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  915667.2\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  915200.0\n",
-      "\t delt1 is :  F  22.0\n",
-      "\t delt2 is :  F  60.0\n",
-      "\t LMTD is : F  37.8749328485\n",
-      "\t R is :  2.72727272727\n",
-      "\t S is :  0.268292682927\n",
-      "\t FT is 0.81 \n",
-      "\t delt is :  F  30.6786956073\n",
-      "\t caloric temperature of hot fluid is : F 120.0\n",
-      "\t caloric temperature of cold fluid is :  F  79.0\n",
-      "\t hot fluid:shell side,phosphate solution \n",
-      "\t flow area is :  ft**2  0.0347916666667\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  579449.101796\n",
-      "\t reynolds number is :  15796.5061612\n",
-      "\t Pr is :  1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  295.957894737\n",
-      "\t cold fluid:inner tube side,raw water \n",
-      "\t flow area is :  ft**2  0.0545277777778\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  762913.907285\n",
-      "\t V is  fps  3.39072847682\n",
-      "\t reynolds number is :  17899.0185011\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  661.333333333\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  204.459014471\n",
-      "\t total surface area is :  ft**2  163.3216\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  182.656652912\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000583796892885\n",
-      "\t pressure drop  for annulus \n",
-      "\t number of crosses are :  96\n",
-      "\t delPs is :  psi  9.51887629626\n",
-      "\t allowable delPs is 10 psi \n",
-      "\t pressure drop  for inner pipe \n",
-      "\t delPt is :  psi  1.58733222032\n",
-      "\t delPr is :  psi  0.6\n",
-      "\t delPT is :  psi  2.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.6 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=150.; # inlet hot fluid,F\n",
-    "T2=90.; # outlet hot fluid,F\n",
-    "t1=68.; # inlet cold fluid,F\n",
-    "t2=90.; # outlet cold fluid,F\n",
-    "W=20160.; # lb/hr\n",
-    "w=41600.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.3*0.19)+(0.7*1); # Btu/(lb)*(F), bcoz of 30 percent of solution\n",
-    "Q1=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.81 \" # from fig 18\n",
-    "delt=(0.81*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is : F\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,phosphate solution \"\n",
-    "ID=10.02; # in\n",
-    "C=0.25; # clearance\n",
-    "B=2; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,using eq.7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2),using eq.7.2\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.20*2.42; # at 120F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=71; # from fig.28\n",
-    "c=1; # Btu/(lb)*(F),at 120F,from fig.table 4\n",
-    "k=0.33; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((0.757)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is : \",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "print\"\\t cold fluid:inner tube side,raw water \"\n",
-    "Nt=52;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gt\n",
-    "V=(Gt/(3600*62.5));\n",
-    "print\"\\t V is  fps \",V\n",
-    "mu2=0.91*2.42; # at 79F,lb/(ft)*(hr),from table 14\n",
-    "D=(0.62/12); # from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hi=800*1; #using fig.25,Btu/(hr)*(ft**2)*(F)\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \"\n",
-    "f=0.0019; # friction factor for reynolds number 15750, using fig.29\n",
-    "s=1.3; # for reynolds number 25300,using fig.6\n",
-    "Ds=10.02/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are : \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \"\n",
-    "print\"\\t pressure drop  for inner pipe \"\n",
-    "f=0.00023; # friction factor for reynolds number 17900, using fig.26\n",
-    "s=1;\n",
-    "phyt=1;\n",
-    "D=0.0517; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",delPt\n",
-    "X1=0.08; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.7 pgno:166"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 31,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.7 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  1050.97060273\n",
-      "\t coefficient of t**2 is :  1\n",
-      "\t coefficient of t is :  -556\n",
-      "\t constant term is :  73733.0293973\n",
-      "\t t is : [ 0.00457855  0.00296217]\n",
-      "\t t cannot be greater than 328F t is 218F \n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.7 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "U=50; # Btu/(hr)*(ft**2)*(F)\n",
-    "TP=328; # F\n",
-    "TE=228; # F\n",
-    "#solution\n",
-    "import numpy\n",
-    "\n",
-    "CP=(0.30/(888.8*1000));\n",
-    "CE=(0.05/(960*1000));\n",
-    "CF=1.20;\n",
-    "theta=8000; # annual hours\n",
-    "X=((CF*(TP-TE))/((CP-CE)*U*theta)); # from eq 7.53\n",
-    "print\"\\t X is : \",X\n",
-    "a=(1); # coefficient of t**2\n",
-    "b=(-556); # coefficient of t\n",
-    "c=(74784-X); # constant\n",
-    "print\"\\t coefficient of t**2 is : \",a\n",
-    "print\"\\t coefficient of t is : \",b\n",
-    "print\"\\t constant term is : \",c\n",
-    "P=numpy.array([c, b, a])\n",
-    "t=numpy.roots(P)\n",
-    "print\"\\t t is :\",t\n",
-    "print\"\\t t cannot be greater than 328F t is 218F \"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.8 pgno:167"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 32,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.8 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "ascii\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for solution \n",
-      "\n",
-      "\t total heat required for solution is :  Btu/hr  3784000.0\n",
-      "\t for steam \n",
-      "\n",
-      "\t total heat required for steam is :  Btu/hr  3792395.0\n",
-      "\t delt1 is :  F  128.0\n",
-      "\t delt2 is :  F  106.0\n",
-      "\t LMTD is : F  116.654454302\n",
-      "\t R is :  0.0\n",
-      "\t delt is :  F  116.654454302\n",
-      "\t hot fluid:tube side,steam \n",
-      "\t flow area is :  ft**2  0.0796944444444\n",
-      "\t mAss velocity is : lb/(hr)*(ft**2)  49564.3081213\n",
-      "\t reynolds number is :  82671.1836992\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  1500\n",
-      "\t cold fluid:shell side,sugar solution \n",
-      "\n",
-      "\t flow area is :  ft**2  0.551953125\n",
-      "\t mAss velocity is :  lb/(hr)*(ft**2)  362349.610757\n",
-      "\t De is :  ft  0.148026315789\n",
-      "\t reynolds number is :  17049.3572499\n",
-      "\t Pr is : 1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F)  138.3504\n",
-      "\t phys is :  1.13996690865\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  157.714877798\n",
-      "\t tw is :  F  218.119942108\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  142.70989533\n",
-      "\t total surface area is :  ft**2  238.7008\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  136.194122026\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.000335238210724\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  2.8\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t De1 is :  ft 0.122\n",
-      "\t Res1 is :  14084.0\n",
-      "\t delPs is :  psi  0.07\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.8 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=228.; # inlet hot fluid,F\n",
-    "T2=228.; # outlet hot fluid,F\n",
-    "t1=100.; # inlet cold fluid,F\n",
-    "t2=122.; # outlet cold fluid,F\n",
-    "W=200000.; # lb/hr\n",
-    "w=3950.; # lb/hr\n",
-    "#solution\n",
-    "import sys\n",
-    "print sys.getdefaultencoding()\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for solution \\n\"\n",
-    "c=(0.2*0.30)+(0.8*1); # bcoz of 20 percent solution,Btu/(lb)*(F)\n",
-    "Q1=((W)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for solution is :  Btu/hr \",Q1\n",
-    "print\"\\t for steam \\n\"\n",
-    "l=960.1; # latent heat of condensation,Btu/(lb)\n",
-    "Q=((w)*(l)); # Btu/hr\n",
-    "print\"\\t total heat required for steam is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "delt=(LMTD); # when R=0,F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "\n",
-    "ta=111; #F\n",
-    "Ta=228; #f\n",
-    "print\"\\t hot fluid:tube side,steam \"\n",
-    "Nt=76;\n",
-    "n=2; # number of pAsses\n",
-    "L=16; #ft\n",
-    "at1=0.302; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \",at\n",
-    "Gt=(w/(at)); # mAss velocity,lb/(hr)*(ft**2)b\n",
-    "print\"\\t mAss velocity is : lb/(hr)*(ft**2) \",Gt\n",
-    "mu2=0.0128*2.42; # at 228F,lb/(ft)*(hr)\n",
-    "D=(0.62/12); # from table 10,ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Ret\n",
-    "hio=1500; # for condensation of steam\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "print\"\\t cold fluid:shell side,sugar solution \\n\"\n",
-    "ID=12; # in\n",
-    "d=0.75/12; # diameter of tube,ft\n",
-    "Nt=76; # number of tubes\n",
-    "As=((3.14*(12**2)/4)-(76*3.14*(0.75**2)/4))/144; # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mAss velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mAss velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.30*2.42; # at 111F,lb/(ft)*(hr), from fig.14\n",
-    "De=((4*As)/(Nt*3.14*d)); # from eq.6.3,ft\n",
-    "print\"\\t De is :  ft \",De\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is : \",Res\n",
-    "jH=61.5; # from fig.24, tube side data\n",
-    "c=0.86; # Btu/(lb)*(F),at 111F,from fig.4\n",
-    "k=0.333; # Btu/(hr)*(ft**2)*(F/ft)\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :\",Pr\n",
-    "Ho=((jH)*(k/De)*(Pr)); # H0=(h0/phya),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \",Ho\n",
-    "muw=0.51*2.42; #  at 210F,lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is : \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "tw=(ta)+(((hio)/(hio+Ho))*(Ta-ta)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \",tw\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "UD=((Q)/((A)*(LMTD)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000155; # friction factor for reynolds number 82500, using fig.26\n",
-    "s=0.0008;\n",
-    "phyt=1;\n",
-    "D=0.0517; \n",
-    "delPt=((f*(Gt**2)*(L)*(2))/(5.22*(10**10)*(D)*(s)*(phyt)))/2; # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt,1)\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "De1=((4*As)/((Nt*3.14*d)+(3.14*1))); # from eq.6.4,ft\n",
-    "print\"\\t De1 is :  ft\",round(De1,3)\n",
-    "Res1=(De1*Gs/mu1); # from eq 7.3\n",
-    "print\"\\t Res1 is : \",round(Res1)\n",
-    "f=0.00025; # friction factor, using fig.26\n",
-    "s=1.08; # for reynolds number 25300,using fig.6\n",
-    "delPs=((f*(Gs**2)*(L)*(1))/(5.22*(10**10)*(De1)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",round(delPs,2)\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 7.9 pgno:170"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 33,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 7.9 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t X is :  0.628360498562\n",
-      "\t R is :  2.77815829528\n",
-      "\t t2 is :  F  176.85\n",
-      "\t T2 is :  F  176.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 7.9 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=390; # F\n",
-    "t1=100; # F\n",
-    "U=69.3; # Btu/(hr)*(ft^2)*(F)\n",
-    "A=662; # ft^2\n",
-    "W=43800; # lb/hr\n",
-    "w=149000; # lb/hr\n",
-    "C=0.60; # Btu/(lb)*(F)\n",
-    "c=0.49; # Btu/(lb)*(F)\n",
-    "#solution\n",
-    "X=((U*A)/(w*c));\n",
-    "print\"\\t X is : \",X\n",
-    "R=((w*c)/(W*C));\n",
-    "print\"\\t R is : \",R\n",
-    "S=0.265; # from fig 7.25, by comparing X an R\n",
-    "t2=(t1)+((0.265)*(T1-t1)); # S=((t2-t1)/(T1-t1))\n",
-    "print\"\\t t2 is :  F \",t2\n",
-    "T2=((T1)-((R)*(t2-t1))); # R=((T1-T2)/(t2-t1))\n",
-    "print\"\\t T2 is :  F \",round(T2)\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery.ipynb
deleted file mode 100755
index 3d3964a6..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery.ipynb
+++ /dev/null
@@ -1,432 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 8 : Flow Arrangements for Incerased Heat Recovery"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.1 pgno:181"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.1 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for oil \n",
-      "\n",
-      "\t total heat required for oil is : Btu/hr  6974256.0\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  6990000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  238.0\n",
-      "\t LMTD is : F  71.9314248044\n",
-      "\t R is :  8.6\n",
-      "\t S is :  0.111940298507\n",
-      "\t FT is 0.93 \n",
-      "\t delt is :  F  66.8962250681\n",
-      "\t ratio of two local temperature difference is : %.3f \n",
-      "0.0420168067227\n",
-      "\t caloric temperature of hot fluid is :  F  164.5\n",
-      "\t caloric temperature of cold fluid is :  F  97.5\n",
-      "\t hot fluid:shell side,oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.170138888889\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  291526.530612\n",
-      "\t reynolds number is :   8873.57540419\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \n",
-      "127.272727273\n",
-      "\t cold fluid:inner tube side,water \n",
-      "\n",
-      "\t flow area is :f ft**2  0.239085648148\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) 974546.158687\n",
-      "\t V is :  fps  4.33131626083\n",
-      "\t reynolds number is :   34937.8788163\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F)  969.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  736.896\n",
-      "\t tw is :  F \n",
-      "107.367601613\n",
-      "\t phys is :   0.925306637672\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  117.76629934\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  101.538952854\n",
-      "\t total surface area is :  ft**2  1426.2864\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  73.155514686\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00382107226455\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t number of crosses are :   20\n",
-      "\t delPs is :  psi  4.47363588933\n",
-      "\t allowable delPs is 10 psi \n",
-      "\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  4.0\n",
-      "\t delPr is :  psi  3.1\n",
-      "\t delPT is :  psi  7.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.1 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=358.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=90.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=49600.; # lb/hr\n",
-    "w=233000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for oil \\n\"\n",
-    "c=0.545; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \",Q\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.93 \" # from fig 19 for 2-4 exchanger\n",
-    "delt=(0.93*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : %.3f \\n\",X\n",
-    "Fc=0.25; # from fig.17\n",
-    "Kc=0.47; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,oil \\n\"\n",
-    "ID=35; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT))/2; # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.12*2.42; # at 165F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Res\n",
-    "jH=52.5; # from fig.28\n",
-    "Z=0.2; # Z=(k)*(Pr*(1/3)) prandelt number\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phys),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\n\",Ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\n\"\n",
-    "Nt=454;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.455; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :f ft**2 \",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2)\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "mu2=0.73*2.42; # at 98F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.76/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Ret\n",
-    "hi=1010*0.96; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=0.76; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\n\",tw\n",
-    "muw=1.95*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is :  \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "Q=6980000; # taking rounded value,Btu/hr\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "f=0.00215; # friction factor for reynolds number 8900, using fig.29\n",
-    "s=0.82; # for reynolds number 25300,using fig.6\n",
-    "Ds=35/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(2*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\n\"\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000195; # friction factor for reynolds number 34900, using fig.26\n",
-    "s=1;\n",
-    "D=0.0633; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt)\n",
-    "X1=0.13; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.2 pgno:184"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for acetone \t\n",
-      "\t total heat required for acetone is :  Btu/hr \t5130000.0\n",
-      "\t for acetic acid \t\n",
-      "\t total heat required for acetic acid is :  Btu/hr \t5140800.0\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t100\n",
-      "\t LMTD is : F \t39.0865033713\n",
-      "\t R is :  \t2\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.88 \t\n",
-      "\t delt is :  F \t34.3961229667\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t120\n",
-      "\t hot fluid:shell side,acetone \t\n",
-      "\t flow area is :  ft**2 \t0.184461805556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t325270.588235\n",
-      "\t reynolds number is :  \t53203.694701\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t164.4\n",
-      "\t cold fluid:inner tube side,acetic acid \t\n",
-      "\t flow area is :  ft**2 \t0.25125\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t668656.716418\n",
-      "\t reynolds number is :  \t15819.782952\n",
-      "\t Pr is :  \t1.0\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t112.767123288\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t87.808\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.2370234092\n",
-      "\t total surface area is :  ft**2 \t2544.048\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t58.6249615773\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.000413628549958\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t39\n",
-      "\t delPs is :  psi \t10.407463223\n",
-      "\t allowable delPs is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.0\n",
-      "\t delPr is :  psi \t1.4\n",
-      "\t delPT is :  psi \t5.2\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=150; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=168000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for acetone \\t\"\n",
-    "c=0.57; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for acetone is :  Btu/hr \\t\",Q # calculation mistake in problem\n",
-    "print\"\\t for acetic acid \\t\"\n",
-    "c=0.51; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for acetic acid is :  Btu/hr \\t\",Q1 # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.88 \\t\" # from fig 20,for 3-6 exchanger\n",
-    "delt=(0.88*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,acetone \\t\"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.20*2.42; # at 175F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "phys=1;\n",
-    "jH=137; # from fig.28\n",
-    "c=0.63; # Btu/(lb)*(F),at 175F,from fig.2\n",
-    "k=0.095; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*1); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,acetic acid \\t\"\n",
-    "Nt=270;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.268; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.85*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.584/12); # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=56; # from fig.24\n",
-    "c=0.51; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.098; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "phyt=1;\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.584; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=3*(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00155; # friction factor for reynolds number 52200, using fig.29\n",
-    "s=0.79; # for reynolds number 25300,using table.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(3*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00024; # friction factor for reynolds number 158000, using fig.26\n",
-    "s=1.07;\n",
-    "D=0.0487; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n*3))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.063; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=(3)*((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_1.ipynb
deleted file mode 100755
index 5ebbdccc..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_1.ipynb
+++ /dev/null
@@ -1,414 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 8 : Flow Arrangements for Incerased Heat Recovery"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.1 pgno:181"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.1 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for oil \n",
-      "\n",
-      "\t total heat required for oil is : Btu/hr  6974256.0\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  6990000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  238.0\n",
-      "\t LMTD is : F  71.9314248044\n",
-      "\t R is :  8.6\n",
-      "\t S is :  0.111940298507\n",
-      "\t FT is 0.93 \n",
-      "\t delt is :  F  66.8962250681\n",
-      "\t ratio of two local temperature difference is : %.3f \n",
-      "0.0420168067227\n",
-      "\t caloric temperature of hot fluid is :  F  164.5\n",
-      "\t caloric temperature of cold fluid is :  F  97.5\n",
-      "\t hot fluid:shell side,oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.170138888889\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  291526.530612\n",
-      "\t reynolds number is :   8873.57540419\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \n",
-      "127.272727273\n",
-      "\t cold fluid:inner tube side,water \n",
-      "\n",
-      "\t flow area is :f ft**2  0.239085648148\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) 974546.158687\n",
-      "\t V is :  fps  4.33131626083\n",
-      "\t reynolds number is :   34937.8788163\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F)  969.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  736.896\n",
-      "\t tw is :  F \n",
-      "107.367601613\n",
-      "\t phys is :   0.925306637672\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  117.76629934\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  101.538952854\n",
-      "\t total surface area is :  ft**2  1426.2864\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  73.155514686\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00382107226455\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t number of crosses are :   20\n",
-      "\t delPs is :  psi  4.47363588933\n",
-      "\t allowable delPs is 10 psi \n",
-      "\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  4.0\n",
-      "\t delPr is :  psi  3.1\n",
-      "\t delPT is :  psi  7.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.1 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=358.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=90.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=49600.; # lb/hr\n",
-    "w=233000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for oil \\n\"\n",
-    "c=0.545; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \",Q\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.93 \" # from fig 19 for 2-4 exchanger\n",
-    "delt=(0.93*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : %.3f \\n\",X\n",
-    "Fc=0.25; # from fig.17\n",
-    "Kc=0.47; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,oil \\n\"\n",
-    "ID=35; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT))/2; # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.12*2.42; # at 165F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Res\n",
-    "jH=52.5; # from fig.28\n",
-    "Z=0.2; # Z=(k)*(Pr*(1/3)) prandelt number\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phys),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\n\",Ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\n\"\n",
-    "Nt=454;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.455; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :f ft**2 \",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2)\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "mu2=0.73*2.42; # at 98F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.76/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Ret\n",
-    "hi=1010*0.96; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=0.76; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\n\",tw\n",
-    "muw=1.95*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is :  \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "Q=6980000; # taking rounded value,Btu/hr\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "f=0.00215; # friction factor for reynolds number 8900, using fig.29\n",
-    "s=0.82; # for reynolds number 25300,using fig.6\n",
-    "Ds=35/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(2*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\n\"\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000195; # friction factor for reynolds number 34900, using fig.26\n",
-    "s=1;\n",
-    "D=0.0633; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt)\n",
-    "X1=0.13; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.2 pgno:184"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for acetone \t\n",
-      "\t total heat required for acetone is :  Btu/hr \t5130000.0\n",
-      "\t for acetic acid \t\n",
-      "\t total heat required for acetic acid is :  Btu/hr \t5140800.0\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t100\n",
-      "\t LMTD is : F \t39.0865033713\n",
-      "\t R is :  \t2\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.88 \t\n",
-      "\t delt is :  F \t34.3961229667\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t120\n",
-      "\t hot fluid:shell side,acetone \t\n",
-      "\t flow area is :  ft**2 \t0.184461805556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t325270.588235\n",
-      "\t reynolds number is :  \t53203.694701\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t164.4\n",
-      "\t cold fluid:inner tube side,acetic acid \t\n",
-      "\t flow area is :  ft**2 \t0.25125\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t668656.716418\n",
-      "\t reynolds number is :  \t15819.782952\n",
-      "\t Pr is :  \t1.0\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t112.767123288\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t87.808\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.2370234092\n",
-      "\t total surface area is :  ft**2 \t2544.048\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t58.6249615773\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.000413628549958\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t39\n",
-      "\t delPs is :  psi \t10.407463223\n",
-      "\t allowable delPs is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.0\n",
-      "\t delPr is :  psi \t1.4\n",
-      "\t delPT is :  psi \t5.2\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=150; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=168000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for acetone \\t\"\n",
-    "c=0.57; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for acetone is :  Btu/hr \\t\",Q # calculation mistake in problem\n",
-    "print\"\\t for acetic acid \\t\"\n",
-    "c=0.51; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for acetic acid is :  Btu/hr \\t\",Q1 # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.88 \\t\" # from fig 20,for 3-6 exchanger\n",
-    "delt=(0.88*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,acetone \\t\"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.20*2.42; # at 175F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "phys=1;\n",
-    "jH=137; # from fig.28\n",
-    "c=0.63; # Btu/(lb)*(F),at 175F,from fig.2\n",
-    "k=0.095; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*1); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,acetic acid \\t\"\n",
-    "Nt=270;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.268; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.85*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.584/12); # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=56; # from fig.24\n",
-    "c=0.51; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.098; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "phyt=1;\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.584; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=3*(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00155; # friction factor for reynolds number 52200, using fig.29\n",
-    "s=0.79; # for reynolds number 25300,using table.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(3*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00024; # friction factor for reynolds number 158000, using fig.26\n",
-    "s=1.07;\n",
-    "D=0.0487; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n*3))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.063; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=(3)*((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_2.ipynb
deleted file mode 100755
index 5ebbdccc..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_2.ipynb
+++ /dev/null
@@ -1,414 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 8 : Flow Arrangements for Incerased Heat Recovery"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.1 pgno:181"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.1 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for oil \n",
-      "\n",
-      "\t total heat required for oil is : Btu/hr  6974256.0\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  6990000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  238.0\n",
-      "\t LMTD is : F  71.9314248044\n",
-      "\t R is :  8.6\n",
-      "\t S is :  0.111940298507\n",
-      "\t FT is 0.93 \n",
-      "\t delt is :  F  66.8962250681\n",
-      "\t ratio of two local temperature difference is : %.3f \n",
-      "0.0420168067227\n",
-      "\t caloric temperature of hot fluid is :  F  164.5\n",
-      "\t caloric temperature of cold fluid is :  F  97.5\n",
-      "\t hot fluid:shell side,oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.170138888889\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  291526.530612\n",
-      "\t reynolds number is :   8873.57540419\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \n",
-      "127.272727273\n",
-      "\t cold fluid:inner tube side,water \n",
-      "\n",
-      "\t flow area is :f ft**2  0.239085648148\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) 974546.158687\n",
-      "\t V is :  fps  4.33131626083\n",
-      "\t reynolds number is :   34937.8788163\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F)  969.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  736.896\n",
-      "\t tw is :  F \n",
-      "107.367601613\n",
-      "\t phys is :   0.925306637672\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  117.76629934\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  101.538952854\n",
-      "\t total surface area is :  ft**2  1426.2864\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  73.155514686\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00382107226455\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t number of crosses are :   20\n",
-      "\t delPs is :  psi  4.47363588933\n",
-      "\t allowable delPs is 10 psi \n",
-      "\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  4.0\n",
-      "\t delPr is :  psi  3.1\n",
-      "\t delPT is :  psi  7.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.1 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=358.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=90.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=49600.; # lb/hr\n",
-    "w=233000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for oil \\n\"\n",
-    "c=0.545; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \",Q\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.93 \" # from fig 19 for 2-4 exchanger\n",
-    "delt=(0.93*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : %.3f \\n\",X\n",
-    "Fc=0.25; # from fig.17\n",
-    "Kc=0.47; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,oil \\n\"\n",
-    "ID=35; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT))/2; # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.12*2.42; # at 165F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Res\n",
-    "jH=52.5; # from fig.28\n",
-    "Z=0.2; # Z=(k)*(Pr*(1/3)) prandelt number\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phys),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\n\",Ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\n\"\n",
-    "Nt=454;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.455; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :f ft**2 \",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2)\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "mu2=0.73*2.42; # at 98F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.76/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Ret\n",
-    "hi=1010*0.96; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=0.76; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\n\",tw\n",
-    "muw=1.95*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is :  \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "Q=6980000; # taking rounded value,Btu/hr\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "f=0.00215; # friction factor for reynolds number 8900, using fig.29\n",
-    "s=0.82; # for reynolds number 25300,using fig.6\n",
-    "Ds=35/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(2*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\n\"\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000195; # friction factor for reynolds number 34900, using fig.26\n",
-    "s=1;\n",
-    "D=0.0633; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt)\n",
-    "X1=0.13; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.2 pgno:184"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for acetone \t\n",
-      "\t total heat required for acetone is :  Btu/hr \t5130000.0\n",
-      "\t for acetic acid \t\n",
-      "\t total heat required for acetic acid is :  Btu/hr \t5140800.0\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t100\n",
-      "\t LMTD is : F \t39.0865033713\n",
-      "\t R is :  \t2\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.88 \t\n",
-      "\t delt is :  F \t34.3961229667\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t120\n",
-      "\t hot fluid:shell side,acetone \t\n",
-      "\t flow area is :  ft**2 \t0.184461805556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t325270.588235\n",
-      "\t reynolds number is :  \t53203.694701\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t164.4\n",
-      "\t cold fluid:inner tube side,acetic acid \t\n",
-      "\t flow area is :  ft**2 \t0.25125\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t668656.716418\n",
-      "\t reynolds number is :  \t15819.782952\n",
-      "\t Pr is :  \t1.0\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t112.767123288\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t87.808\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.2370234092\n",
-      "\t total surface area is :  ft**2 \t2544.048\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t58.6249615773\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.000413628549958\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t39\n",
-      "\t delPs is :  psi \t10.407463223\n",
-      "\t allowable delPs is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.0\n",
-      "\t delPr is :  psi \t1.4\n",
-      "\t delPT is :  psi \t5.2\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=150; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=168000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for acetone \\t\"\n",
-    "c=0.57; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for acetone is :  Btu/hr \\t\",Q # calculation mistake in problem\n",
-    "print\"\\t for acetic acid \\t\"\n",
-    "c=0.51; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for acetic acid is :  Btu/hr \\t\",Q1 # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.88 \\t\" # from fig 20,for 3-6 exchanger\n",
-    "delt=(0.88*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,acetone \\t\"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.20*2.42; # at 175F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "phys=1;\n",
-    "jH=137; # from fig.28\n",
-    "c=0.63; # Btu/(lb)*(F),at 175F,from fig.2\n",
-    "k=0.095; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*1); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,acetic acid \\t\"\n",
-    "Nt=270;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.268; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.85*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.584/12); # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=56; # from fig.24\n",
-    "c=0.51; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.098; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "phyt=1;\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.584; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=3*(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00155; # friction factor for reynolds number 52200, using fig.29\n",
-    "s=0.79; # for reynolds number 25300,using table.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(3*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00024; # friction factor for reynolds number 158000, using fig.26\n",
-    "s=1.07;\n",
-    "D=0.0487; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n*3))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.063; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=(3)*((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_3.ipynb
deleted file mode 100755
index 5ebbdccc..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_8_flow_arrangements_for_increased_heat_recovery_3.ipynb
+++ /dev/null
@@ -1,414 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 8 : Flow Arrangements for Incerased Heat Recovery"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.1 pgno:181"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.1 \n",
-      "\n",
-      "\t approximate values are mentioned in the book \n",
-      "\n",
-      "\t 1.for heat balance \n",
-      "\n",
-      "\t for oil \n",
-      "\n",
-      "\t total heat required for oil is : Btu/hr  6974256.0\n",
-      "\t for water \n",
-      "\n",
-      "\t total heat required for water is :  Btu/hr  6990000.0\n",
-      "\t delt1 is :  F  10.0\n",
-      "\t delt2 is :  F  238.0\n",
-      "\t LMTD is : F  71.9314248044\n",
-      "\t R is :  8.6\n",
-      "\t S is :  0.111940298507\n",
-      "\t FT is 0.93 \n",
-      "\t delt is :  F  66.8962250681\n",
-      "\t ratio of two local temperature difference is : %.3f \n",
-      "0.0420168067227\n",
-      "\t caloric temperature of hot fluid is :  F  164.5\n",
-      "\t caloric temperature of cold fluid is :  F  97.5\n",
-      "\t hot fluid:shell side,oil \n",
-      "\n",
-      "\t flow area is :  ft**2  0.170138888889\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2)  291526.530612\n",
-      "\t reynolds number is :   8873.57540419\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \n",
-      "127.272727273\n",
-      "\t cold fluid:inner tube side,water \n",
-      "\n",
-      "\t flow area is :f ft**2  0.239085648148\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) 974546.158687\n",
-      "\t V is :  fps  4.33131626083\n",
-      "\t reynolds number is :   34937.8788163\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F)  969.6\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  736.896\n",
-      "\t tw is :  F \n",
-      "107.367601613\n",
-      "\t phys is :   0.925306637672\n",
-      "\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F)  117.76629934\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F)  101.538952854\n",
-      "\t total surface area is :  ft**2  1426.2864\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F)  73.155514686\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu  0.00382107226455\n",
-      "\t pressure drop  for annulus \n",
-      "\n",
-      "\t number of crosses are :   20\n",
-      "\t delPs is :  psi  4.47363588933\n",
-      "\t allowable delPs is 10 psi \n",
-      "\n",
-      "\t pressure drop  for inner pipe \n",
-      "\n",
-      "\t delPt is :  psi  4.0\n",
-      "\t delPr is :  psi  3.1\n",
-      "\t delPT is :  psi  7.2\n",
-      "\t allowable delPT is 10 psi \n",
-      "\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.1 \\n\"\n",
-    "print\"\\t approximate values are mentioned in the book \\n\"\n",
-    "#given\n",
-    "T1=358.; # inlet hot fluid,F\n",
-    "T2=100.; # outlet hot fluid,F\n",
-    "t1=90.; # inlet cold fluid,F\n",
-    "t2=120.; # outlet cold fluid,F\n",
-    "W=49600.; # lb/hr\n",
-    "w=233000.; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\n\"\n",
-    "print\"\\t for oil \\n\"\n",
-    "c=0.545; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for oil is : Btu/hr \",Q\n",
-    "print\"\\t for water \\n\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \",delt1\n",
-    "print\"\\t delt2 is :  F \",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is : \",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is : \",S\n",
-    "print\"\\t FT is 0.93 \" # from fig 19 for 2-4 exchanger\n",
-    "delt=(0.93*LMTD); # F\n",
-    "print\"\\t delt is :  F \",delt\n",
-    "X=((delt1)/(delt2));\n",
-    "print\"\\t ratio of two local temperature difference is : %.3f \\n\",X\n",
-    "Fc=0.25; # from fig.17\n",
-    "Kc=0.47; # crude oil controlling\n",
-    "Tc=((T2)+((Fc)*(T1-T2))); # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \",Tc\n",
-    "tc=((t1)+((Fc)*(t2-t1))); # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \",tc\n",
-    "print\"\\t hot fluid:shell side,oil \\n\"\n",
-    "ID=35; # in\n",
-    "C=0.25; # clearance\n",
-    "B=7; # baffle spacing,in\n",
-    "PT=1.25;\n",
-    "As=((ID*C*B)/(144*PT))/2; # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \",Gs\n",
-    "mu1=1.12*2.42; # at 165F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.99/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Res\n",
-    "jH=52.5; # from fig.28\n",
-    "Z=0.2; # Z=(k)*(Pr*(1/3)) prandelt number\n",
-    "Ho=((jH)*(1/De)*(Z)); # H0=(h0/phys),using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\n\",Ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\n\"\n",
-    "Nt=454;\n",
-    "n=6; # number of passes\n",
-    "L=12; #ft\n",
-    "at1=0.455; # flow area, in**2\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :f ft**2 \",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2)\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \",V\n",
-    "mu2=0.73*2.42; # at 98F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.76/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \",Ret\n",
-    "hi=1010*0.96; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \",hi\n",
-    "ID=0.76; # ft\n",
-    "OD=1; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",hio\n",
-    "tw=(tc)+(((Ho)/(hio+Ho))*(Tc-tc)); # from eq.5.31\n",
-    "print\"\\t tw is :  F \\n\",tw\n",
-    "muw=1.95*2.42; # lb/(ft)*(hr), from fig.14\n",
-    "phys=(mu1/muw)**0.14;\n",
-    "print\"\\t phys is :  \",phys # from fig.24\n",
-    "ho=(Ho)*(phys); # from eq.6.36\n",
-    "print\"\\t Correct h0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \",ho\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",Uc\n",
-    "A2=0.2618; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \",A\n",
-    "Q=6980000; # taking rounded value,Btu/hr\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \",Rd\n",
-    "print\"\\t pressure drop  for annulus \\n\"\n",
-    "f=0.00215; # friction factor for reynolds number 8900, using fig.29\n",
-    "s=0.82; # for reynolds number 25300,using fig.6\n",
-    "Ds=35/12; # ft\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(2*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\n\"\n",
-    "print\"\\t pressure drop  for inner pipe \\n\"\n",
-    "f=0.000195; # friction factor for reynolds number 34900, using fig.26\n",
-    "s=1;\n",
-    "D=0.0633; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \",round(delPt)\n",
-    "X1=0.13; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\n\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 8.2 pgno:184"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 6,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 8.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for acetone \t\n",
-      "\t total heat required for acetone is :  Btu/hr \t5130000.0\n",
-      "\t for acetic acid \t\n",
-      "\t total heat required for acetic acid is :  Btu/hr \t5140800.0\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t100\n",
-      "\t LMTD is : F \t39.0865033713\n",
-      "\t R is :  \t2\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.88 \t\n",
-      "\t delt is :  F \t34.3961229667\n",
-      "\t caloric temperature of hot fluid is :  F \t175\n",
-      "\t caloric temperature of cold fluid is :  F \t120\n",
-      "\t hot fluid:shell side,acetone \t\n",
-      "\t flow area is :  ft**2 \t0.184461805556\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t325270.588235\n",
-      "\t reynolds number is :  \t53203.694701\n",
-      "\t Pr is :  \t1.0\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t164.4\n",
-      "\t cold fluid:inner tube side,acetic acid \t\n",
-      "\t flow area is :  ft**2 \t0.25125\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t668656.716418\n",
-      "\t reynolds number is :  \t15819.782952\n",
-      "\t Pr is :  \t1.0\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t112.767123288\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t87.808\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t57.2370234092\n",
-      "\t total surface area is :  ft**2 \t2544.048\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t58.6249615773\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.000413628549958\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t39\n",
-      "\t delPs is :  psi \t10.407463223\n",
-      "\t allowable delPs is 10 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t4.0\n",
-      "\t delPr is :  psi \t1.4\n",
-      "\t delPT is :  psi \t5.2\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 8.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=250; # inlet hot fluid,F\n",
-    "T2=100; # outlet hot fluid,F\n",
-    "t1=90; # inlet cold fluid,F\n",
-    "t2=150; # outlet cold fluid,F\n",
-    "W=60000; # lb/hr\n",
-    "w=168000; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for acetone \\t\"\n",
-    "c=0.57; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for acetone is :  Btu/hr \\t\",Q # calculation mistake in problem\n",
-    "print\"\\t for acetic acid \\t\"\n",
-    "c=0.51; # Btu/(lb)*(F)\n",
-    "Q1=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for acetic acid is :  Btu/hr \\t\",Q1 # calculation mistake in problem\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((1)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.88 \\t\" # from fig 20,for 3-6 exchanger\n",
-    "delt=(0.88*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,acetone \\t\"\n",
-    "ID=21.25; # in\n",
-    "C=0.25; # clearance\n",
-    "B=5; # baffle spacing,in\n",
-    "PT=1;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.20*2.42; # at 175F,lb/(ft)*(hr), from fig.14\n",
-    "De=0.95/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "phys=1;\n",
-    "jH=137; # from fig.28\n",
-    "c=0.63; # Btu/(lb)*(F),at 175F,from fig.2\n",
-    "k=0.095; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "Pr=((c)*(mu1)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "ho=((jH)*(k/De)*(Pr)*1); # using eq.6.15b,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,acetic acid \\t\"\n",
-    "Nt=270;\n",
-    "n=2; # number of passes\n",
-    "L=16; #ft\n",
-    "at1=0.268; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "mu2=0.85*2.42; # at 120F,lb/(ft)*(hr)\n",
-    "D=(0.584/12); # ft\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "jH=56; # from fig.24\n",
-    "c=0.51; # Btu/(lb)*(F),at 120F,from fig.2\n",
-    "k=0.098; # Btu/(hr)*(ft**2)*(F/ft), from table 4\n",
-    "phyt=1;\n",
-    "Pr=((c)*(mu2)/k)**(1/3); # prandelt number raised to power 1/3\n",
-    "print\"\\t Pr is :  \\t\",Pr\n",
-    "hi=((jH)*(k/D)*(Pr)*(1**0.14)); # using eq.6.15a,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.584; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); #Hio=(hio/phyp), using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=3*(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00155; # friction factor for reynolds number 52200, using fig.29\n",
-    "s=0.79; # for reynolds number 25300,using table.6\n",
-    "Ds=21.25/12; # ft\n",
-    "N=(12*L/B)+1; # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "delPs=((f*(Gs**2)*(Ds)*(3*N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 10 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.00024; # friction factor for reynolds number 158000, using fig.26\n",
-    "s=1.07;\n",
-    "D=0.0487; # ft\n",
-    "delPt=((f*(Gt**2)*(L)*(n*3))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt)\n",
-    "X1=0.063; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=(3)*((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases.ipynb
deleted file mode 100755
index 52b09ddd..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases.ipynb
+++ /dev/null
@@ -1,395 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 9: Gases"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.1 pgno:193"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for ammonia gas \t\n",
-      "\t total heat required for ammonia gas is :  Btu/hr \t784824.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t785000\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t22.4772661868\n",
-      "\t R is :  \t15\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.837 \t\n",
-      "\t delt is :  F \t18.8134717984\n",
-      "\t caloric temperature of hot fluid is :  F \t170\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,ammonia at 83psia \t\n",
-      "\t flow area is :  ft**2 \t0.387706776948\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t25462.5417634\n",
-      "\t reynolds number is :  \t40187.0924297\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.4542545455\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0954236111111\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t822647.551124\n",
-      "\t V is :  fps \t3.65621133833\n",
-      "\t reynolds number is :  \t21418.7950051\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t900\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t744.0\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t40.1624954017\n",
-      "\t total surface area is :  ft**2 \t571.6256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.9943154025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0111991543302\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t8\n",
-      "\t rowgas is  lb/ft**3 \t0.209\n",
-      "\t s is  \t0.003344\n",
-      "\t delPs is :  psi \t2.03484815237\n",
-      "\t allowable delPs is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.6\n",
-      "\t delPr is :  psi \t2.9\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=245; # inlet hot fluid,F\n",
-    "T2=95; # outlet hot fluid,F\n",
-    "t1=85; # inlet cold fluid,F\n",
-    "t2=95; # outlet cold fluid,F\n",
-    "W=9872; # lb/hr\n",
-    "w=78500; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for ammonia gas \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for ammonia gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.837 \\t\" # from fig 18\n",
-    "delt=(0.837*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,ammonia at 83psia \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.012*2.42; # at 170F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=118; # from fig.28\n",
-    "k=0.017; # Btu/(hr)*(ft**2)*(F/ft),from table 5\n",
-    "Z=0.97; # Z=(Pr*(1/3)) prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)*1); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=364;\n",
-    "n=8; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.82*2.42; # at 90F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.62/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=900; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00162; # friction factor for reynolds number 40200, using fig.29\n",
-    "Ds=23.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "rowgas=0.209;\n",
-    "print\"\\t rowgas is  lb/ft**3 \\t\",rowgas\n",
-    "s=rowgas/62.5;\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000225; # friction factor for reynolds number 21400, using fig.26\n",
-    "s=1;\n",
-    "D=0.0517; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.090; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.2 pgno:196"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t The air and water both occupy the same volume at their respective partial pressures \t\n",
-      "\t volume of water entering is :  lb \t693.049715558\n",
-      "\t for first stage \t\n",
-      "\t P2 is :  psi \t34.251\n",
-      "\t T2absr is :  R \t706.727218318\n",
-      "\t T2abs is :  F \t247.057218318\n",
-      "\t for intercooler \t\n",
-      "\t final gas volume is :  ft**3/hr \t120257.51073\n",
-      "\t water remaining in air is :  lb/hr \t297.446229853\n",
-      "\t condensation in inter cooler is :  lb/hr \t395.603485705\n",
-      "\t Specific volume of atmospheric air is :  ft**3/lb \t14.8\n",
-      "\t air in inlet gas is :  lb/hr\t18932.4324324\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.216216\n",
-      "\t Qwaters is :  Btu/hr \t46780.8558001\n",
-      "\t latent heat \t\n",
-      "\t Qwater1 is :  Btu/hr \t411467.185481\n",
-      "\t total heat is :  Btu/hr \t1168214.2575\n",
-      "\t for second stage \t\n",
-      "\t P3 is :  psi \t79.80483\n",
-      "\t final gas volume is :  ft**3/hr \t51612.6655492\n",
-      "\t water remaining in air is :  lb/hr \t127.659326117\n",
-      "\t condensation in inter cooler is :  lb/hr \t169.340673883\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.0\n",
-      "\t Qwater is :  Btu/hr \t19631.0\n",
-      "\t latent heat \t\n",
-      "\t Qwater is :  Btu/hr \t176131.0\n",
-      "\t total heat is :  Btu/hr  905729.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "V1=4670; # inlet air volume,cfm\n",
-    "Pp=0.8153; # Saturation partial pressure of water at 95F,psi,from table 7\n",
-    "Ps=404.3;#  Saturation specific volume of water at 95F,ft**3/lb, from table 7\n",
-    "#solution\n",
-    "print\"\\t The air and water both occupy the same volume at their respective partial pressures \\t\"\n",
-    "Vw1=(V1*60/Ps); # water entering per hr,lb\n",
-    "print\"\\t volume of water entering is :  lb \\t\",Vw1\n",
-    "print\"\\t for first stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P1=14.7; # psi\n",
-    "P2=(P1*c); # (c=(P2/P1)),psi\n",
-    "print\"\\t P2 is :  psi \\t\",P2\n",
-    "gama=1.4; # for air\n",
-    "T1abs=95; # F\n",
-    "T2absr=((T1abs+460)*(P2/P1)**((gama-1)/gama));\n",
-    "print\"\\t T2absr is :  R \\t\",T2absr\n",
-    "T2abs=(T2absr-459.67); # F\n",
-    "print\"\\t T2abs is :  F \\t\",T2abs\n",
-    "print\"\\t for intercooler \\t\"\n",
-    "V2=(V1*60*P1/P2); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V2\n",
-    "Vw2=(V2/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw2\n",
-    "C=(Vw1-Vw2); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C\n",
-    "Vs=14.8; # Specific volume of atmospheric air,ft**3/lb\n",
-    "print\"\\t Specific volume of atmospheric air is :  ft**3/lb \\t\",Vs\n",
-    "Va=(V1*60/Vs); # air in inlet gas, lb/hr\n",
-    "print\"\\t air in inlet gas is :  lb/hr\\t\",Va\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=((Va)*(0.25)*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",Qair\n",
-    "Qwaters=(Vw1*0.45*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwaters is :  Btu/hr \\t\",Qwaters\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C*l); # Btu/hr\n",
-    "print\"\\t Qwater1 is :  Btu/hr \\t\",Qwaterl\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \\t\",Qt1\n",
-    "print\"\\t for second stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P3=(P2*c); # (c=(P3/P1)),psi\n",
-    "print\"\\t P3 is :  psi \\t\",P3\n",
-    "V3=(V1*60*P1/P3); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V3\n",
-    "Vw3=(V3/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw3\n",
-    "C1=(297-Vw3); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C1\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=(Va*0.25*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",round(Qair)\n",
-    "Qwaters=(Vw2*0.44*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaters)\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C1*l); # Btu/hr, calculation mistake in book\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaterl)\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \",round(Qt1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.3  pgno:197"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total number of moles re :  \t690.168582375\n",
-      "\t Moles of air is :  \t651.724137931\n",
-      "\t Moles of water is :  \t38.4444444444\n",
-      "\t after compression \t\n",
-      "\t partial pressure is : psi \t1.91\n",
-      "\t dew point is :  F \t124\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "Va=18900.; # air in inlet gas\n",
-    "Vw1=692.; # water entering\n",
-    "#solution\n",
-    "Ma=(Va/29.); # moles\n",
-    "Mw=(Vw1/18.); # moles\n",
-    "M=(Ma+Mw); # moles\n",
-    "print\"\\t total number of moles re :  \\t\",M\n",
-    "print\"\\t Moles of air is :  \\t\",Ma\n",
-    "print\"\\t Moles of water is :  \\t\",Mw\n",
-    "print\"\\t after compression \\t\"\n",
-    "P=34.2; # pressure,psi\n",
-    "pw=(Mw/M)*(P); # partial pressure\n",
-    "print\"\\t partial pressure is : psi \\t\",round(pw,2)\n",
-    "Td=124; # F, table table 7\n",
-    "print\"\\t dew point is :  F \\t\",Td\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": null,
-   "metadata": {
-    "collapsed": true
-   },
-   "outputs": [],
-   "source": []
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_1.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_1.ipynb
deleted file mode 100755
index 725fa18f..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_1.ipynb
+++ /dev/null
@@ -1,386 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 9: Gases"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.1 pgno:193"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for ammonia gas \t\n",
-      "\t total heat required for ammonia gas is :  Btu/hr \t784824.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t785000\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t22.4772661868\n",
-      "\t R is :  \t15\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.837 \t\n",
-      "\t delt is :  F \t18.8134717984\n",
-      "\t caloric temperature of hot fluid is :  F \t170\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,ammonia at 83psia \t\n",
-      "\t flow area is :  ft**2 \t0.387706776948\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t25462.5417634\n",
-      "\t reynolds number is :  \t40187.0924297\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.4542545455\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0954236111111\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t822647.551124\n",
-      "\t V is :  fps \t3.65621133833\n",
-      "\t reynolds number is :  \t21418.7950051\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t900\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t744.0\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t40.1624954017\n",
-      "\t total surface area is :  ft**2 \t571.6256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.9943154025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0111991543302\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t8\n",
-      "\t rowgas is  lb/ft**3 \t0.209\n",
-      "\t s is  \t0.003344\n",
-      "\t delPs is :  psi \t2.03484815237\n",
-      "\t allowable delPs is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.6\n",
-      "\t delPr is :  psi \t2.9\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=245; # inlet hot fluid,F\n",
-    "T2=95; # outlet hot fluid,F\n",
-    "t1=85; # inlet cold fluid,F\n",
-    "t2=95; # outlet cold fluid,F\n",
-    "W=9872; # lb/hr\n",
-    "w=78500; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for ammonia gas \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for ammonia gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.837 \\t\" # from fig 18\n",
-    "delt=(0.837*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,ammonia at 83psia \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.012*2.42; # at 170F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=118; # from fig.28\n",
-    "k=0.017; # Btu/(hr)*(ft**2)*(F/ft),from table 5\n",
-    "Z=0.97; # Z=(Pr*(1/3)) prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)*1); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=364;\n",
-    "n=8; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.82*2.42; # at 90F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.62/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=900; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00162; # friction factor for reynolds number 40200, using fig.29\n",
-    "Ds=23.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "rowgas=0.209;\n",
-    "print\"\\t rowgas is  lb/ft**3 \\t\",rowgas\n",
-    "s=rowgas/62.5;\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000225; # friction factor for reynolds number 21400, using fig.26\n",
-    "s=1;\n",
-    "D=0.0517; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.090; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.2 pgno:196"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t The air and water both occupy the same volume at their respective partial pressures \t\n",
-      "\t volume of water entering is :  lb \t693.049715558\n",
-      "\t for first stage \t\n",
-      "\t P2 is :  psi \t34.251\n",
-      "\t T2absr is :  R \t706.727218318\n",
-      "\t T2abs is :  F \t247.057218318\n",
-      "\t for intercooler \t\n",
-      "\t final gas volume is :  ft**3/hr \t120257.51073\n",
-      "\t water remaining in air is :  lb/hr \t297.446229853\n",
-      "\t condensation in inter cooler is :  lb/hr \t395.603485705\n",
-      "\t Specific volume of atmospheric air is :  ft**3/lb \t14.8\n",
-      "\t air in inlet gas is :  lb/hr\t18932.4324324\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.216216\n",
-      "\t Qwaters is :  Btu/hr \t46780.8558001\n",
-      "\t latent heat \t\n",
-      "\t Qwater1 is :  Btu/hr \t411467.185481\n",
-      "\t total heat is :  Btu/hr \t1168214.2575\n",
-      "\t for second stage \t\n",
-      "\t P3 is :  psi \t79.80483\n",
-      "\t final gas volume is :  ft**3/hr \t51612.6655492\n",
-      "\t water remaining in air is :  lb/hr \t127.659326117\n",
-      "\t condensation in inter cooler is :  lb/hr \t169.340673883\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.0\n",
-      "\t Qwater is :  Btu/hr \t19631.0\n",
-      "\t latent heat \t\n",
-      "\t Qwater is :  Btu/hr \t176131.0\n",
-      "\t total heat is :  Btu/hr  905729.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "V1=4670; # inlet air volume,cfm\n",
-    "Pp=0.8153; # Saturation partial pressure of water at 95F,psi,from table 7\n",
-    "Ps=404.3;#  Saturation specific volume of water at 95F,ft**3/lb, from table 7\n",
-    "#solution\n",
-    "print\"\\t The air and water both occupy the same volume at their respective partial pressures \\t\"\n",
-    "Vw1=(V1*60/Ps); # water entering per hr,lb\n",
-    "print\"\\t volume of water entering is :  lb \\t\",Vw1\n",
-    "print\"\\t for first stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P1=14.7; # psi\n",
-    "P2=(P1*c); # (c=(P2/P1)),psi\n",
-    "print\"\\t P2 is :  psi \\t\",P2\n",
-    "gama=1.4; # for air\n",
-    "T1abs=95; # F\n",
-    "T2absr=((T1abs+460)*(P2/P1)**((gama-1)/gama));\n",
-    "print\"\\t T2absr is :  R \\t\",T2absr\n",
-    "T2abs=(T2absr-459.67); # F\n",
-    "print\"\\t T2abs is :  F \\t\",T2abs\n",
-    "print\"\\t for intercooler \\t\"\n",
-    "V2=(V1*60*P1/P2); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V2\n",
-    "Vw2=(V2/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw2\n",
-    "C=(Vw1-Vw2); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C\n",
-    "Vs=14.8; # Specific volume of atmospheric air,ft**3/lb\n",
-    "print\"\\t Specific volume of atmospheric air is :  ft**3/lb \\t\",Vs\n",
-    "Va=(V1*60/Vs); # air in inlet gas, lb/hr\n",
-    "print\"\\t air in inlet gas is :  lb/hr\\t\",Va\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=((Va)*(0.25)*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",Qair\n",
-    "Qwaters=(Vw1*0.45*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwaters is :  Btu/hr \\t\",Qwaters\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C*l); # Btu/hr\n",
-    "print\"\\t Qwater1 is :  Btu/hr \\t\",Qwaterl\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \\t\",Qt1\n",
-    "print\"\\t for second stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P3=(P2*c); # (c=(P3/P1)),psi\n",
-    "print\"\\t P3 is :  psi \\t\",P3\n",
-    "V3=(V1*60*P1/P3); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V3\n",
-    "Vw3=(V3/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw3\n",
-    "C1=(297-Vw3); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C1\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=(Va*0.25*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",round(Qair)\n",
-    "Qwaters=(Vw2*0.44*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaters)\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C1*l); # Btu/hr, calculation mistake in book\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaterl)\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \",round(Qt1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.3  pgno:197"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total number of moles re :  \t690.168582375\n",
-      "\t Moles of air is :  \t651.724137931\n",
-      "\t Moles of water is :  \t38.4444444444\n",
-      "\t after compression \t\n",
-      "\t partial pressure is : psi \t1.91\n",
-      "\t dew point is :  F \t124\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "Va=18900.; # air in inlet gas\n",
-    "Vw1=692.; # water entering\n",
-    "#solution\n",
-    "Ma=(Va/29.); # moles\n",
-    "Mw=(Vw1/18.); # moles\n",
-    "M=(Ma+Mw); # moles\n",
-    "print\"\\t total number of moles re :  \\t\",M\n",
-    "print\"\\t Moles of air is :  \\t\",Ma\n",
-    "print\"\\t Moles of water is :  \\t\",Mw\n",
-    "print\"\\t after compression \\t\"\n",
-    "P=34.2; # pressure,psi\n",
-    "pw=(Mw/M)*(P); # partial pressure\n",
-    "print\"\\t partial pressure is : psi \\t\",round(pw,2)\n",
-    "Td=124; # F, table table 7\n",
-    "print\"\\t dew point is :  F \\t\",Td\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_2.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_2.ipynb
deleted file mode 100755
index 725fa18f..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_2.ipynb
+++ /dev/null
@@ -1,386 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 9: Gases"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.1 pgno:193"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for ammonia gas \t\n",
-      "\t total heat required for ammonia gas is :  Btu/hr \t784824.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t785000\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t22.4772661868\n",
-      "\t R is :  \t15\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.837 \t\n",
-      "\t delt is :  F \t18.8134717984\n",
-      "\t caloric temperature of hot fluid is :  F \t170\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,ammonia at 83psia \t\n",
-      "\t flow area is :  ft**2 \t0.387706776948\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t25462.5417634\n",
-      "\t reynolds number is :  \t40187.0924297\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.4542545455\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0954236111111\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t822647.551124\n",
-      "\t V is :  fps \t3.65621133833\n",
-      "\t reynolds number is :  \t21418.7950051\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t900\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t744.0\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t40.1624954017\n",
-      "\t total surface area is :  ft**2 \t571.6256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.9943154025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0111991543302\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t8\n",
-      "\t rowgas is  lb/ft**3 \t0.209\n",
-      "\t s is  \t0.003344\n",
-      "\t delPs is :  psi \t2.03484815237\n",
-      "\t allowable delPs is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.6\n",
-      "\t delPr is :  psi \t2.9\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=245; # inlet hot fluid,F\n",
-    "T2=95; # outlet hot fluid,F\n",
-    "t1=85; # inlet cold fluid,F\n",
-    "t2=95; # outlet cold fluid,F\n",
-    "W=9872; # lb/hr\n",
-    "w=78500; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for ammonia gas \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for ammonia gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.837 \\t\" # from fig 18\n",
-    "delt=(0.837*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,ammonia at 83psia \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.012*2.42; # at 170F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=118; # from fig.28\n",
-    "k=0.017; # Btu/(hr)*(ft**2)*(F/ft),from table 5\n",
-    "Z=0.97; # Z=(Pr*(1/3)) prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)*1); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=364;\n",
-    "n=8; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.82*2.42; # at 90F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.62/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=900; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00162; # friction factor for reynolds number 40200, using fig.29\n",
-    "Ds=23.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "rowgas=0.209;\n",
-    "print\"\\t rowgas is  lb/ft**3 \\t\",rowgas\n",
-    "s=rowgas/62.5;\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000225; # friction factor for reynolds number 21400, using fig.26\n",
-    "s=1;\n",
-    "D=0.0517; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.090; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.2 pgno:196"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t The air and water both occupy the same volume at their respective partial pressures \t\n",
-      "\t volume of water entering is :  lb \t693.049715558\n",
-      "\t for first stage \t\n",
-      "\t P2 is :  psi \t34.251\n",
-      "\t T2absr is :  R \t706.727218318\n",
-      "\t T2abs is :  F \t247.057218318\n",
-      "\t for intercooler \t\n",
-      "\t final gas volume is :  ft**3/hr \t120257.51073\n",
-      "\t water remaining in air is :  lb/hr \t297.446229853\n",
-      "\t condensation in inter cooler is :  lb/hr \t395.603485705\n",
-      "\t Specific volume of atmospheric air is :  ft**3/lb \t14.8\n",
-      "\t air in inlet gas is :  lb/hr\t18932.4324324\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.216216\n",
-      "\t Qwaters is :  Btu/hr \t46780.8558001\n",
-      "\t latent heat \t\n",
-      "\t Qwater1 is :  Btu/hr \t411467.185481\n",
-      "\t total heat is :  Btu/hr \t1168214.2575\n",
-      "\t for second stage \t\n",
-      "\t P3 is :  psi \t79.80483\n",
-      "\t final gas volume is :  ft**3/hr \t51612.6655492\n",
-      "\t water remaining in air is :  lb/hr \t127.659326117\n",
-      "\t condensation in inter cooler is :  lb/hr \t169.340673883\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.0\n",
-      "\t Qwater is :  Btu/hr \t19631.0\n",
-      "\t latent heat \t\n",
-      "\t Qwater is :  Btu/hr \t176131.0\n",
-      "\t total heat is :  Btu/hr  905729.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "V1=4670; # inlet air volume,cfm\n",
-    "Pp=0.8153; # Saturation partial pressure of water at 95F,psi,from table 7\n",
-    "Ps=404.3;#  Saturation specific volume of water at 95F,ft**3/lb, from table 7\n",
-    "#solution\n",
-    "print\"\\t The air and water both occupy the same volume at their respective partial pressures \\t\"\n",
-    "Vw1=(V1*60/Ps); # water entering per hr,lb\n",
-    "print\"\\t volume of water entering is :  lb \\t\",Vw1\n",
-    "print\"\\t for first stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P1=14.7; # psi\n",
-    "P2=(P1*c); # (c=(P2/P1)),psi\n",
-    "print\"\\t P2 is :  psi \\t\",P2\n",
-    "gama=1.4; # for air\n",
-    "T1abs=95; # F\n",
-    "T2absr=((T1abs+460)*(P2/P1)**((gama-1)/gama));\n",
-    "print\"\\t T2absr is :  R \\t\",T2absr\n",
-    "T2abs=(T2absr-459.67); # F\n",
-    "print\"\\t T2abs is :  F \\t\",T2abs\n",
-    "print\"\\t for intercooler \\t\"\n",
-    "V2=(V1*60*P1/P2); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V2\n",
-    "Vw2=(V2/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw2\n",
-    "C=(Vw1-Vw2); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C\n",
-    "Vs=14.8; # Specific volume of atmospheric air,ft**3/lb\n",
-    "print\"\\t Specific volume of atmospheric air is :  ft**3/lb \\t\",Vs\n",
-    "Va=(V1*60/Vs); # air in inlet gas, lb/hr\n",
-    "print\"\\t air in inlet gas is :  lb/hr\\t\",Va\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=((Va)*(0.25)*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",Qair\n",
-    "Qwaters=(Vw1*0.45*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwaters is :  Btu/hr \\t\",Qwaters\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C*l); # Btu/hr\n",
-    "print\"\\t Qwater1 is :  Btu/hr \\t\",Qwaterl\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \\t\",Qt1\n",
-    "print\"\\t for second stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P3=(P2*c); # (c=(P3/P1)),psi\n",
-    "print\"\\t P3 is :  psi \\t\",P3\n",
-    "V3=(V1*60*P1/P3); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V3\n",
-    "Vw3=(V3/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw3\n",
-    "C1=(297-Vw3); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C1\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=(Va*0.25*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",round(Qair)\n",
-    "Qwaters=(Vw2*0.44*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaters)\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C1*l); # Btu/hr, calculation mistake in book\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaterl)\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \",round(Qt1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.3  pgno:197"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total number of moles re :  \t690.168582375\n",
-      "\t Moles of air is :  \t651.724137931\n",
-      "\t Moles of water is :  \t38.4444444444\n",
-      "\t after compression \t\n",
-      "\t partial pressure is : psi \t1.91\n",
-      "\t dew point is :  F \t124\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "Va=18900.; # air in inlet gas\n",
-    "Vw1=692.; # water entering\n",
-    "#solution\n",
-    "Ma=(Va/29.); # moles\n",
-    "Mw=(Vw1/18.); # moles\n",
-    "M=(Ma+Mw); # moles\n",
-    "print\"\\t total number of moles re :  \\t\",M\n",
-    "print\"\\t Moles of air is :  \\t\",Ma\n",
-    "print\"\\t Moles of water is :  \\t\",Mw\n",
-    "print\"\\t after compression \\t\"\n",
-    "P=34.2; # pressure,psi\n",
-    "pw=(Mw/M)*(P); # partial pressure\n",
-    "print\"\\t partial pressure is : psi \\t\",round(pw,2)\n",
-    "Td=124; # F, table table 7\n",
-    "print\"\\t dew point is :  F \\t\",Td\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
diff --git a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_3.ipynb b/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_3.ipynb
deleted file mode 100755
index 725fa18f..00000000
--- a/Process_Heat_Transfer_by_D._Q._Kern/Chapter_9_Gases_3.ipynb
+++ /dev/null
@@ -1,386 +0,0 @@
-{
- "cells": [
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "# Chapter 9: Gases"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.1 pgno:193"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 3,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.1 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t 1.for heat balance \t\n",
-      "\t for ammonia gas \t\n",
-      "\t total heat required for ammonia gas is :  Btu/hr \t784824.0\n",
-      "\t for water \t\n",
-      "\t total heat required for water is :  Btu/hr \t785000\n",
-      "\t delt1 is :  F \t10\n",
-      "\t delt2 is :  F \t150\n",
-      "\t LMTD is : F \t22.4772661868\n",
-      "\t R is :  \t15\n",
-      "\t S is :  \t0\n",
-      "\t FT is 0.837 \t\n",
-      "\t delt is :  F \t18.8134717984\n",
-      "\t caloric temperature of hot fluid is :  F \t170\n",
-      "\t caloric temperature of cold fluid is :  F \t90\n",
-      "\t hot fluid:shell side,ammonia at 83psia \t\n",
-      "\t flow area is :  ft**2 \t0.387706776948\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t25462.5417634\n",
-      "\t reynolds number is :  \t40187.0924297\n",
-      "\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \t42.4542545455\n",
-      "\t cold fluid:inner tube side,water \t\n",
-      "\t flow area is :  ft**2 \t0.0954236111111\n",
-      "\t mass velocity is :  lb/(hr)*(ft**2) \t822647.551124\n",
-      "\t V is :  fps \t3.65621133833\n",
-      "\t reynolds number is :  \t21418.7950051\n",
-      "\t hi is :  Btu/(hr)*(ft**2)*(F) \t900\n",
-      "\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \t744.0\n",
-      "\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t40.1624954017\n",
-      "\t total surface area is :  ft**2 \t571.6256\n",
-      "\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \t72.9943154025\n",
-      "\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \t-0.0111991543302\n",
-      "\t pressure drop  for annulus \t\n",
-      "\t number of crosses are :  \t8\n",
-      "\t rowgas is  lb/ft**3 \t0.209\n",
-      "\t s is  \t0.003344\n",
-      "\t delPs is :  psi \t2.03484815237\n",
-      "\t allowable delPs is 2 psi \t\n",
-      "\t pressure drop  for inner pipe \t\n",
-      "\t delPt is :  psi \t3.6\n",
-      "\t delPr is :  psi \t2.9\n",
-      "\t delPT is :  psi \t6.5\n",
-      "\t allowable delPT is 10 psi \t\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.1 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "T1=245; # inlet hot fluid,F\n",
-    "T2=95; # outlet hot fluid,F\n",
-    "t1=85; # inlet cold fluid,F\n",
-    "t2=95; # outlet cold fluid,F\n",
-    "W=9872; # lb/hr\n",
-    "w=78500; # lb/hr\n",
-    "#solution\n",
-    "from math import log\n",
-    "print\"\\t 1.for heat balance \\t\"\n",
-    "print\"\\t for ammonia gas \\t\"\n",
-    "c=0.53; # Btu/(lb)*(F)\n",
-    "Q=((W)*(c)*(T1-T2)); # Btu/hr\n",
-    "print\"\\t total heat required for ammonia gas is :  Btu/hr \\t\",Q\n",
-    "print\"\\t for water \\t\"\n",
-    "c=1; # Btu/(lb)*(F)\n",
-    "Q=((w)*(c)*(t2-t1)); # Btu/hr\n",
-    "print\"\\t total heat required for water is :  Btu/hr \\t\",Q\n",
-    "delt1=T2-t1; #F\n",
-    "delt2=T1-t2; # F\n",
-    "print\"\\t delt1 is :  F \\t\",delt1\n",
-    "print\"\\t delt2 is :  F \\t\",delt2\n",
-    "LMTD=((delt2-delt1)/((2.3)*(log(delt2/delt1))));\n",
-    "print\"\\t LMTD is : F \\t\",LMTD\n",
-    "R=((T1-T2)/(t2-t1));\n",
-    "print\"\\t R is :  \\t\",R\n",
-    "S=((t2-t1)/(T1-t1));\n",
-    "print\"\\t S is :  \\t\",S\n",
-    "print\"\\t FT is 0.837 \\t\" # from fig 18\n",
-    "delt=(0.837*LMTD); # F\n",
-    "print\"\\t delt is :  F \\t\",delt\n",
-    "Tc=((T2)+(T1))/2; # caloric temperature of hot fluid,F\n",
-    "print\"\\t caloric temperature of hot fluid is :  F \\t\",Tc\n",
-    "tc=((t1)+(t2))/2; # caloric temperature of cold fluid,F\n",
-    "print\"\\t caloric temperature of cold fluid is :  F \\t\",tc\n",
-    "print\"\\t hot fluid:shell side,ammonia at 83psia \\t\"\n",
-    "ID=23.25; # in\n",
-    "C=0.1875; # clearance\n",
-    "B=12; # baffle spacing,in\n",
-    "PT=0.937;\n",
-    "As=((ID*C*B)/(144*PT)); # flow area,ft**2,from eq 7.1\n",
-    "print\"\\t flow area is :  ft**2 \\t\",As\n",
-    "Gs=(W/As); # mass velocity,lb/(hr)*(ft**2),from eq 7.2\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gs\n",
-    "mu1=0.012*2.42; # at 170F,lb/(ft)*(hr), from fig.15\n",
-    "De=0.55/12; # from fig.28,ft\n",
-    "Res=((De)*(Gs)/mu1); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Res\n",
-    "jH=118; # from fig.28\n",
-    "k=0.017; # Btu/(hr)*(ft**2)*(F/ft),from table 5\n",
-    "Z=0.97; # Z=(Pr*(1/3)) prandelt number\n",
-    "ho=((jH)*(k/De)*(Z)*1); # using eq.6.15,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t individual heat transfer coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",ho\n",
-    "print\"\\t cold fluid:inner tube side,water \\t\"\n",
-    "Nt=364;\n",
-    "n=8; # number of passes\n",
-    "L=8; #ft\n",
-    "at1=0.302; # flow area, in**2,from table 10\n",
-    "at=((Nt*at1)/(144*n)); # total area,ft**2,from eq.7.48\n",
-    "print\"\\t flow area is :  ft**2 \\t\",at\n",
-    "Gt=(w/(at)); # mass velocity,lb/(hr)*(ft**2)\n",
-    "print\"\\t mass velocity is :  lb/(hr)*(ft**2) \\t\",Gt\n",
-    "V=(Gt/(3600*62.5)); # fps\n",
-    "print\"\\t V is :  fps \\t\",V\n",
-    "mu2=0.82*2.42; # at 90F,lb/(ft)*(hr),from fig 14\n",
-    "D=(0.62/12); # ft,from table 10\n",
-    "Ret=((D)*(Gt)/mu2); # reynolds number\n",
-    "print\"\\t reynolds number is :  \\t\",Ret\n",
-    "hi=900; # using fig 25,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t hi is :  Btu/(hr)*(ft**2)*(F) \\t\",hi\n",
-    "ID=0.62; # ft\n",
-    "OD=0.75; #ft\n",
-    "hio=((hi)*(ID/OD)); # using eq.6.5\n",
-    "print\"\\t Correct hi0 to the surface at the OD is :  Btu/(hr)*(ft**2)*(F) \\t\",hio\n",
-    "Uc=((hio)*(ho)/(hio+ho)); # clean overall coefficient,Btu/(hr)*(ft**2)*(F)\n",
-    "print\"\\t clean overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",Uc\n",
-    "A2=0.1963; # actual surface supplied for each tube,ft**2,from table 10\n",
-    "A=(Nt*L*A2); # ft**2\n",
-    "print\"\\t total surface area is :  ft**2 \\t\",A\n",
-    "UD=((Q)/((A)*(delt)));\n",
-    "print\"\\t actual design overall coefficient is :  Btu/(hr)*(ft**2)*(F) \\t\",UD\n",
-    "Rd=((Uc-UD)/((UD)*(Uc))); # (hr)*(ft**2)*(F)/Btu\n",
-    "print\"\\t actual Rd is :  (hr)*(ft**2)*(F)/Btu \\t\",Rd\n",
-    "print\"\\t pressure drop  for annulus \\t\"\n",
-    "f=0.00162; # friction factor for reynolds number 40200, using fig.29\n",
-    "Ds=23.25/12; # ft\n",
-    "phys=1;\n",
-    "N=(12*L/B); # number of crosses,using eq.7.43\n",
-    "print\"\\t number of crosses are :  \\t\",N\n",
-    "rowgas=0.209;\n",
-    "print\"\\t rowgas is  lb/ft**3 \\t\",rowgas\n",
-    "s=rowgas/62.5;\n",
-    "print\"\\t s is  \\t\",s\n",
-    "delPs=((f*(Gs**2)*(Ds)*(N))/(5.22*(10**10)*(De)*(s)*(phys))); # using eq.7.44,psi\n",
-    "print\"\\t delPs is :  psi \\t\",delPs\n",
-    "print\"\\t allowable delPs is 2 psi \\t\"\n",
-    "print\"\\t pressure drop  for inner pipe \\t\"\n",
-    "f=0.000225; # friction factor for reynolds number 21400, using fig.26\n",
-    "s=1;\n",
-    "D=0.0517; #ft\n",
-    "phyt=1;\n",
-    "delPt=((f*(Gt**2)*(L)*(n))/(5.22*(10**10)*(D)*(s)*(phyt))); # using eq.7.45,psi\n",
-    "print\"\\t delPt is :  psi \\t\",round(delPt,1)\n",
-    "X1=0.090; # X1=((V**2)/(2*g)), for Gt 1060000,using fig.27\n",
-    "delPr=((4*n*X1)/(s)); # using eq.7.46,psi\n",
-    "print\"\\t delPr is :  psi \\t\",round(delPr,1)\n",
-    "delPT=delPt+delPr; # using eq.7.47,psi\n",
-    "print\"\\t delPT is :  psi \\t\",round(delPT,1)\n",
-    "print\"\\t allowable delPT is 10 psi \\t\"\n",
-    "#end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.2 pgno:196"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 5,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.2 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t The air and water both occupy the same volume at their respective partial pressures \t\n",
-      "\t volume of water entering is :  lb \t693.049715558\n",
-      "\t for first stage \t\n",
-      "\t P2 is :  psi \t34.251\n",
-      "\t T2absr is :  R \t706.727218318\n",
-      "\t T2abs is :  F \t247.057218318\n",
-      "\t for intercooler \t\n",
-      "\t final gas volume is :  ft**3/hr \t120257.51073\n",
-      "\t water remaining in air is :  lb/hr \t297.446229853\n",
-      "\t condensation in inter cooler is :  lb/hr \t395.603485705\n",
-      "\t Specific volume of atmospheric air is :  ft**3/lb \t14.8\n",
-      "\t air in inlet gas is :  lb/hr\t18932.4324324\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.216216\n",
-      "\t Qwaters is :  Btu/hr \t46780.8558001\n",
-      "\t latent heat \t\n",
-      "\t Qwater1 is :  Btu/hr \t411467.185481\n",
-      "\t total heat is :  Btu/hr \t1168214.2575\n",
-      "\t for second stage \t\n",
-      "\t P3 is :  psi \t79.80483\n",
-      "\t final gas volume is :  ft**3/hr \t51612.6655492\n",
-      "\t water remaining in air is :  lb/hr \t127.659326117\n",
-      "\t condensation in inter cooler is :  lb/hr \t169.340673883\n",
-      "\t heat load(245 to 95F) \t)\n",
-      "\t sensible heat \t\n",
-      "\t Qair is :  Btu/hr \t709966.0\n",
-      "\t Qwater is :  Btu/hr \t19631.0\n",
-      "\t latent heat \t\n",
-      "\t Qwater is :  Btu/hr \t176131.0\n",
-      "\t total heat is :  Btu/hr  905729.0\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.2 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "V1=4670; # inlet air volume,cfm\n",
-    "Pp=0.8153; # Saturation partial pressure of water at 95F,psi,from table 7\n",
-    "Ps=404.3;#  Saturation specific volume of water at 95F,ft**3/lb, from table 7\n",
-    "#solution\n",
-    "print\"\\t The air and water both occupy the same volume at their respective partial pressures \\t\"\n",
-    "Vw1=(V1*60/Ps); # water entering per hr,lb\n",
-    "print\"\\t volume of water entering is :  lb \\t\",Vw1\n",
-    "print\"\\t for first stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P1=14.7; # psi\n",
-    "P2=(P1*c); # (c=(P2/P1)),psi\n",
-    "print\"\\t P2 is :  psi \\t\",P2\n",
-    "gama=1.4; # for air\n",
-    "T1abs=95; # F\n",
-    "T2absr=((T1abs+460)*(P2/P1)**((gama-1)/gama));\n",
-    "print\"\\t T2absr is :  R \\t\",T2absr\n",
-    "T2abs=(T2absr-459.67); # F\n",
-    "print\"\\t T2abs is :  F \\t\",T2abs\n",
-    "print\"\\t for intercooler \\t\"\n",
-    "V2=(V1*60*P1/P2); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V2\n",
-    "Vw2=(V2/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw2\n",
-    "C=(Vw1-Vw2); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C\n",
-    "Vs=14.8; # Specific volume of atmospheric air,ft**3/lb\n",
-    "print\"\\t Specific volume of atmospheric air is :  ft**3/lb \\t\",Vs\n",
-    "Va=(V1*60/Vs); # air in inlet gas, lb/hr\n",
-    "print\"\\t air in inlet gas is :  lb/hr\\t\",Va\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=((Va)*(0.25)*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",Qair\n",
-    "Qwaters=(Vw1*0.45*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwaters is :  Btu/hr \\t\",Qwaters\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C*l); # Btu/hr\n",
-    "print\"\\t Qwater1 is :  Btu/hr \\t\",Qwaterl\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \\t\",Qt1\n",
-    "print\"\\t for second stage \\t\"\n",
-    "c=2.33; # compression ratio\n",
-    "P3=(P2*c); # (c=(P3/P1)),psi\n",
-    "print\"\\t P3 is :  psi \\t\",P3\n",
-    "V3=(V1*60*P1/P3); # ft**3/hr\n",
-    "print\"\\t final gas volume is :  ft**3/hr \\t\",V3\n",
-    "Vw3=(V3/Ps); # water remaining in air, lb/hr\n",
-    "print\"\\t water remaining in air is :  lb/hr \\t\",Vw3\n",
-    "C1=(297-Vw3); # condensation in inter cooler, lb/hr\n",
-    "print\"\\t condensation in inter cooler is :  lb/hr \\t\",C1\n",
-    "print\"\\t heat load(245 to 95F) \\t)\"\n",
-    "print\"\\t sensible heat \\t\"\n",
-    "Qair=(Va*0.25*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qair is :  Btu/hr \\t\",round(Qair)\n",
-    "Qwaters=(Vw2*0.44*(245-T1abs)); # Btu/hr\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaters)\n",
-    "print\"\\t latent heat \\t\"\n",
-    "l=1040.1; # latent heat\n",
-    "Qwaterl=(C1*l); # Btu/hr, calculation mistake in book\n",
-    "print\"\\t Qwater is :  Btu/hr \\t\",round(Qwaterl)\n",
-    "Qt1=Qair+Qwaters+Qwaterl;\n",
-    "print\"\\t total heat is :  Btu/hr \",round(Qt1)\n",
-    "# end\n"
-   ]
-  },
-  {
-   "cell_type": "markdown",
-   "metadata": {},
-   "source": [
-    "## Example 9.3  pgno:197"
-   ]
-  },
-  {
-   "cell_type": "code",
-   "execution_count": 8,
-   "metadata": {
-    "collapsed": false
-   },
-   "outputs": [
-    {
-     "name": "stdout",
-     "output_type": "stream",
-     "text": [
-      "\t example 9.3 \t\n",
-      "\t approximate values are mentioned in the book \t\n",
-      "\t total number of moles re :  \t690.168582375\n",
-      "\t Moles of air is :  \t651.724137931\n",
-      "\t Moles of water is :  \t38.4444444444\n",
-      "\t after compression \t\n",
-      "\t partial pressure is : psi \t1.91\n",
-      "\t dew point is :  F \t124\n"
-     ]
-    }
-   ],
-   "source": [
-    "print\"\\t example 9.3 \\t\"\n",
-    "print\"\\t approximate values are mentioned in the book \\t\"\n",
-    "#given\n",
-    "Va=18900.; # air in inlet gas\n",
-    "Vw1=692.; # water entering\n",
-    "#solution\n",
-    "Ma=(Va/29.); # moles\n",
-    "Mw=(Vw1/18.); # moles\n",
-    "M=(Ma+Mw); # moles\n",
-    "print\"\\t total number of moles re :  \\t\",M\n",
-    "print\"\\t Moles of air is :  \\t\",Ma\n",
-    "print\"\\t Moles of water is :  \\t\",Mw\n",
-    "print\"\\t after compression \\t\"\n",
-    "P=34.2; # pressure,psi\n",
-    "pw=(Mw/M)*(P); # partial pressure\n",
-    "print\"\\t partial pressure is : psi \\t\",round(pw,2)\n",
-    "Td=124; # F, table table 7\n",
-    "print\"\\t dew point is :  F \\t\",Td\n",
-    "# end\n"
-   ]
-  }
- ],
- "metadata": {
-  "kernelspec": {
-   "display_name": "Python 2",
-   "language": "python",
-   "name": "python2"
-  },
-  "language_info": {
-   "codemirror_mode": {
-    "name": "ipython",
-    "version": 2
-   },
-   "file_extension": ".py",
-   "mimetype": "text/x-python",
-   "name": "python",
-   "nbconvert_exporter": "python",
-   "pygments_lexer": "ipython2",
-   "version": "2.7.9"
-  }
- },
- "nbformat": 4,
- "nbformat_minor": 0
-}
author	kinitrupti	2017-05-12 18:40:35 +0530
committer	kinitrupti	2017-05-12 18:40:35 +0530
commit	d36fc3b8f88cc3108ffff6151e376b619b9abb01 (patch)
tree	9806b0d68a708d2cfc4efc8ae3751423c56b7721 /Process_Heat_Transfer_by_D._Q._Kern
parent	1b1bb67e9ea912be5c8591523c8b328766e3680f (diff)
download	Python-Textbook-Companions-d36fc3b8f88cc3108ffff6151e376b619b9abb01.tar.gz Python-Textbook-Companions-d36fc3b8f88cc3108ffff6151e376b619b9abb01.tar.bz2 Python-Textbook-Companions-d36fc3b8f88cc3108ffff6151e376b619b9abb01.zip