Removed duplicates

17 files changed, 5321 insertions, 0 deletions

diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./.ipynb_checkpoints/Chapter1-checkpoint.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./.ipynb_checkpoints/Chapter1-checkpoint.ipynb
new file mode 100755
index 00000000..dd1cacc1
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./.ipynb_checkpoints/Chapter1-checkpoint.ipynb
@@ -0,0 +1,334 @@
+{
+ "metadata": {
+  "name": ""
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 1 - \"Introduction\""
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.1, Page number: 13"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "k=35;                                      #Thermal  Conductivity,  [W/m*K]\n",
+      "T1=110                                     #  Temperature  of  front[C]\n",
+      "T2=50;                                     #  Temperature  of  back,[C]\n",
+      "A=0.4                                      #area  of  slab,[m**2]\n",
+      "x=0.03;                                    #Thickness  of  slab,[m]\n",
+      "\n",
+      "#Calculations\n",
+      "q=-k*(T2-T1)/(1000*x);                     #formula  for  heat  flux[KW/m^2]\n",
+      "Q=q*A;                                     #formula  for  heat  transfer  rate[KW]\n",
+      "\n",
+      "#Results\n",
+      "print \"Heat flux is:\",q,\"KW/m^2\\n\"\n",
+      "print \"Heat transfer rate is:\",Q,\"KW \\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Heat flux is: 70.0 KW/m^2\n",
+        "\n",
+        "Heat transfer rate is: 28.0 KW \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.2, Page number: 16"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from sympy import solve,symbols\n",
+      "\n",
+      "#Variables\n",
+      "x=symbols('x');\n",
+      "k1=372;                                 #  Thermal  Conductivity  of  slab,W/m*K\n",
+      "x1=0.003;                               #  Thickness  of  slab,m\n",
+      "x2=0.002                                #  Thickness  of  steel,m\n",
+      "k2=17;                                  #  Thermal  Conductivity  of  steel,W/m*K\n",
+      "T1=400;                                 #  Temperature  on  one  side,C\n",
+      "T2=100                                  #Temperature  on  other  side,C\n",
+      "\n",
+      "#Calculations\n",
+      "Tcu=solve(x+2*x*(k1/x1)*(x2/k2)-(T1-T2),x);\n",
+      "#q=k1*(Tcu/x1)=k2*(Tss/x2);\n",
+      "Tss  =  Tcu[0]*(k1/x1)*(x2/k2);         #  formula for temperature gradient in steel side\n",
+      "Tcul=T1-Tss;\n",
+      "Tcur=T2+Tss;\n",
+      "q=k2*Tss/(1000*x2);                     #  formula for heat conducted, kW\\m^2\n",
+      "\n",
+      "#Results\n",
+      "print \"Temperature on left copper side is :\",round(Tcul,3),\"C\\n\"\n",
+      "print \"Temperature on right copper  side is :\",round(Tcur,3),\"C\\n\"\n",
+      "print \"Heat conducted through the wall is :\",round(q,3),\"kW\\m^2\\n\"\n",
+      "print \"Our initial approximation was accurate within a few percent.\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Temperature on left copper side is : 254.971 C\n",
+        "\n",
+        "Temperature on right copper  side is : 245.029 C\n",
+        "\n",
+        "Heat conducted through the wall is : 1232.749 kW\\m^2\n",
+        "\n",
+        "Our initial approximation was accurate within a few percent.\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.3, Page number: 22"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "q1=6000;                                          #Heat  flux,  W*m**-2\n",
+      "T1=120;                                           #Heater  Temperature,  C\n",
+      "T2=70;                                            #final  Temperature  of  Heater, C\n",
+      "q2=2000;                                          #final  heat  flux, W*m**-2\n",
+      "\n",
+      "#Calculations\n",
+      "h=q1/(T1-T2)                                      #formula  for  average  heat  transfer  cofficient\n",
+      "Tnew=T2+q2/h;                                     #formula  for  new  Heater  temperature, C\n",
+      "\n",
+      "#Results\n",
+      "print \"Average Heat transfer coefficient is:\",h,\"W/(m^2*K)\\n\"\n",
+      "print \"New Heater Temperature is:\",round(Tnew,3),\"C\\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Average Heat transfer coefficient is: 120.0 W/(m^2*K)\n",
+        "\n",
+        "New Heater Temperature is: 86.667 C\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.4, Page number: 25"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from numpy import array\n",
+      "from numpy import linspace\n",
+      "import matplotlib.pyplot as plt\n",
+      "from pylab import *\n",
+      "%matplotlib inline\n",
+      "\n",
+      "#Variables\n",
+      "h=250;                                  #Heat Transfer  Coefficient,  W/(m**2*K)\n",
+      "k=45;                                   #Thermal  Conductivity,  W/(m*K)\n",
+      "c=180;                                  #Heat  Capacity,  J/(kg*K)\n",
+      "a=9300;                                 #density,  kg/m**3\n",
+      "T1=200;                                 #temperature,  C\n",
+      "D=0.001;                                #diameter  of  bead, m\n",
+      "t1=linspace(0,5,50);                    #defining time interval of 0.1 seconds\n",
+      "T=linspace(0,5,50);\n",
+      "i=0;\n",
+      "\n",
+      "#Calculations\n",
+      "while i<50:\n",
+      "    T[i]=T1-c*math.exp(-t1[i]/((a*c*D)/(6*h)));      #Calculating temperature at each time in degree C\n",
+      "    i=i+1;\n",
+      "\n",
+      "plt.plot(t1,T);\n",
+      "plt.xlabel(\"Time(in sec)\");\n",
+      "plt.ylabel(\"Temperature(in degree C)\");\n",
+      "plt.title(\"Thermocouple response to a hot  gas flow\");\n",
+      "plt.show();\n",
+      "\n",
+      "Bi  =  h*(D/2)/k;                       #biot  no.\n",
+      "\n",
+      "#Results\n",
+      "print \"The value of Biot no for this thermocouple is\",round(Bi,5);\n",
+      "print \"Bi is <0.1 and hence the thermocouple could be considered as a lumped heat capacity system and the assumption taken is valid.\\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": "iVBORw0KGgoAAAANSUhEUgAAAYQAAAEZCAYAAACXRVJOAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz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\n9aVlLh5rAAAAAElFTkSuQmCC\n",
+       "text": [
+        "<matplotlib.figure.Figure at 0x7fbd3da5b8d0>"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The value of Biot no for this thermocouple is 0.00278\n",
+        "Bi is <0.1 and hence the thermocouple could be considered as a lumped heat capacity system and the assumption taken is valid.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.5, Page number: 32"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from sympy import solve,symbols\n",
+      "\n",
+      "#Variables\n",
+      "x=symbols('x');\n",
+      "T1=293;                                    #Temperature  of  air  around  thermocouple,  K\n",
+      "T2=373;                                    #Wall  temperature,  K\n",
+      "h=75;                                      #Average  Heat  Transfer  Coefficient,  W/(m**2*K)\n",
+      "s=5.67*10**-8;                             #stefan  Boltzman  constant,  W/(m**2*K**4)\n",
+      "\n",
+      "#Calculations\n",
+      "x=solve((h*(x-T1)+s*(x**4-T2**4)),x);\t   #Calculating Thermocouple Temperature, K\n",
+      "y=x[1]-273;\t\t\t\t                   #Thermocouple Temperature, C\n",
+      "\n",
+      "#Results\n",
+      "print \"Thermocouple Temperature is :\",round(y,3),\"C\\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Thermocouple Temperature is : 28.395 C\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.6, Page number: 34"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from sympy import solve,symbols\n",
+      "\n",
+      "#Variables\n",
+      "x=symbols('x');\n",
+      "e=0.4;                                             #emissivity\n",
+      "T1=293;                                            #Temperature  of  air  around  Thermocouple,  K\n",
+      "T2=273;                                            #wall  Temperature,  K\n",
+      "h=75;                                              #Average  Heat  Transfer  Coefficient,  W/(m**2*K)\n",
+      "s=5.6704*10**-8;                                   #stefan  Boltzman  constant,  W/(m**2*K**4)\n",
+      "\n",
+      "#Calculations\n",
+      "z=solve(((s*e*((373)**4 - (x)**4)) - h*(x-293)),x);\t#Calculating Thermocouple Temperature, K\n",
+      "y=z[0]-273;\t\t\t\t\t                        #Thermocouple Temperature, C\n",
+      "\n",
+      "'''NOTE: Equation written is absolutely correct and solving this equation\n",
+      "        should give real result as: 296.112 i.e. 23.112 C, but somehow python is giving wrong result.'''\n",
+      "\n",
+      "#Results\n",
+      "print \"Thermocouple Temperature is :\",round(y,1),\"C \\n\"\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Thermocouple Temperature is : 25.9 C \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./.ipynb_checkpoints/Chapter11-checkpoint.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./.ipynb_checkpoints/Chapter11-checkpoint.ipynb
new file mode 100755
index 00000000..cec52317
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./.ipynb_checkpoints/Chapter11-checkpoint.ipynb
@@ -0,0 +1,631 @@
+{
+ "metadata": {
+  "name": ""
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 11: An introduction to mass transfer"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.1, Page number:603"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "Mn2=0.7556;                    #mass  fraction  of  nitrogen\n",
+      "Mo2=0.2315;                    #mass  fraction  of  oxygen\n",
+      "Mar=0.01289;                   #mass  fraction  of  argon  gas\n",
+      "M1=28.02;                      #molar  mass  of  N2,kg/kmol\n",
+      "M2=32;                         #molar  mass  of  O2,kg/kmol\n",
+      "M3=39.95  ;                    #molar  mass  of  Ar,kg/kmol\n",
+      "p=101325;                      #Atmospheric pressure in Pascal(Pa)\n",
+      "R=8314.5;                      #Gas constant, J/kmol-K\n",
+      "T=300;                         #Approximate room temperature, K\n",
+      "\n",
+      "#Calculations\n",
+      "Mair=(Mn2/M1+Mo2/M2+Mar/M3)**-1;                  #molar  mass  of  air,kg/kmol\n",
+      "Xo2=Mo2*Mair/M2;                                  #mole  fraction  of  O2\n",
+      "PO2=Xo2*p;                                        #partial  pressure  of  O2,Pa\n",
+      "Co2=PO2/(R*T);                                    #molar  volume  of  O2,kmol/m**3\n",
+      "ao2=Co2*M2;                                       #density  of  O2,kg/m**3\n",
+      "\n",
+      "\n",
+      "#Result\n",
+      "print \"Mole fraction of O2 is :\",round(Xo2,4),\"\\n\"\n",
+      "print \"Partial pressure of O2 is :\",round(PO2,4),\"\\n\"\n",
+      "print \"Molar volume of O2 is :\",round(Co2,4),\" kmol/m^3\\n\"\n",
+      "print \"Density of O2 is :\",round(ao2,4),\" kg/m^3\\n\"\n",
+      " #end"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mole fraction of O2 is : 0.2095 \n",
+        "\n",
+        "Partial pressure of O2 is : 21232.5938 \n",
+        "\n",
+        "Molar volume of O2 is : 0.0085  kmol/m^3\n",
+        "\n",
+        "Density of O2 is : 0.2724  kg/m^3\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 14
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.2, Page number: 606"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "r=0.00241;                     #rate  of  consumption  of  carbon,kg/(m**2*s)\n",
+      "Mo2=0.2;                       #concentration  of  oxygen  at  surface  s\n",
+      "Mco2=0.052;                    #concentration  of  CO2  at  surface  s\n",
+      "sd=0.29;                       #density  of  surface  s,kg/m**3\n",
+      "\n",
+      "#since  carbon  flows  through  a  second  imaginary  surface  u,  the  mass  fluxes  are  relatedd  by Ncu=-12/32*No2s=12/44*Nco2s\n",
+      "#the  minus  sign  arises  because  the  O2  flow  is  opposite  the  C  and  CO2  flows.in  steady  state  if  we  apply  mass  conservation  to  the  control  volume  between  the  u  and  s  surface,  wee  find  that  the  total  mass  flux  entering  the  u  surface  equals  that  leaving  the  s  surface\n",
+      "Ncu=r;                          #mass  fluxes  of  carbon  in  u  surface,kg/m**2/s\n",
+      "\n",
+      "#Calculations\n",
+      "No2s=-32/12*Ncu;                #mass  flux  of  O2  in  surface  s,kg/(m**2*s)\n",
+      "Nco2s=44/12*Ncu;                #mass  flux  of  CO2  in  surface  s,kg/(m**2*s)\n",
+      "Vo2s=No2s/(Mo2*sd);             #mass  average  speed,m/s\n",
+      "Vco2s=Nco2s/(sd);               #mass  average  speed,m/s\n",
+      "Vs=(Nco2s+No2s)/sd;             #effective  mass  average  speed,m/s\n",
+      "j1=sd*Mo2*(Vo2s-Vs);            #diffusional  mass  flux,kg/(m**2*s)\n",
+      "j2=sd*Mco2*(Vco2s-Vs);          #diffusional  mass  flux,kg/(m**2*s)\n",
+      "#the  diffusional  mass  fluxes  are  very  nearly  equal  to  the  species  m  ss  fluxes.  tha  is  because  the  mass  average  speed  is  much  less  than  species  speeds.\n",
+      "\n",
+      "N1 = Ncu/12;                      #mole  flux  of  carbon  through  the  surface  s,kmol/(m**2*s)\n",
+      "N2 = -N1;                         #mole  flux  of  oxygen  through  the  surface  s,kmol/(m**2*s)\n",
+      "\n",
+      "#Result\n",
+      "print \"Mass flux of O2 through an imaginary surface is :\",round(j1,5),\"kg/(m^2*s)\\n\"\n",
+      "print \"Mass flux of CO2 through an imaginary surface is :\",round(j2,5),\"kg/(m^2*s)\\n\"\n",
+      "\n",
+      "print \"Mole flux of Co2 through an imaginary surface is :\",round(N1,5),\"kmol/(m^2*s)\\n\"\n",
+      "print \"Mole flux of O2through an imaginary surface is :\",round(N2,5),\"kmol/(m^2*s)\\n\"\n",
+      "print \"The two diffusional mole fluxes sum to zero themselves because ther is no convective mole flux for other species to diffuse against. the reader may find the velocity of the interface.that calculation shows the interface to be receding so slowly that the velocities are equal to those that would be seen by a stationary observer.\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mass flux of O2 through an imaginary surface is : -0.00691 kg/(m^2*s)\n",
+        "\n",
+        "Mass flux of CO2 through an imaginary surface is : 0.00033 kg/(m^2*s)\n",
+        "\n",
+        "Mole flux of Co2 through an imaginary surface is : 0.0002 kmol/(m^2*s)\n",
+        "\n",
+        "Mole flux of O2through an imaginary surface is : -0.0002 kmol/(m^2*s)\n",
+        "\n",
+        "The two diffusional mole fluxes sum to zero themselves because ther is no convective mole flux for other species to diffuse against. the reader may find the velocity of the interface.that calculation shows the interface to be receding so slowly that the velocities are equal to those that would be seen by a stationary observer.\n"
+       ]
+      }
+     ],
+     "prompt_number": 15
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.3, Page number: 617"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=276;                                                                #temp.of  air,K\n",
+      "aa=3.711;                                                              #lennard  jones  constant  or  collision  diameter,A\n",
+      "ab=2.827;                                                              #lennard  jones  constant  or  collision  diameter,A\n",
+      "b1=78.6;                                                               #lennard  jones  constant,K\n",
+      "b2=59.7;                                                               #lennard  jones  constant,K\n",
+      "Ma=28.97;                                                              #Molecular mass of air, kg/kmol\n",
+      "Mh=2.016;                                                              #Molecular mass of hydrogen, kg/kmol\n",
+      "\n",
+      "#Calculations\n",
+      "a=(aa+ab)/2;                                                           #effective  molecular  diameter  for  collisions  of  hydrogen  and  air,m\n",
+      "b=math.sqrt(b1*b2);                                                    #effective  potential  well  depth,K\n",
+      "c=T1/b;        \n",
+      "\n",
+      "d=0.8822;                                                              #potential  well  function, from table 11.3\n",
+      "Dab=(1.8583*math.pow(10,-7))*math.pow(T1,1.5)/(math.pow(a,2)*d)*math.sqrt(1/Mh+1/Ma);             #diffusion  coefficient  of  hydrogen  in  air,m**2/s\n",
+      "\n",
+      "\n",
+      "#Result\n",
+      "print \"Diffusion coefficient of hydrogen in air is :\",round(Dab,6),\"m^2/s an experimental value from table is 6.34*10^-5 m^2/s,so the prediction is high by 5 percent.\\n\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Diffusion coefficient of hydrogen in air is : 6.6e-05 m^2/s an experimental value from table is 6.34*10^-5 m^2/s,so the prediction is high by 5 percent.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.4, Page number: 625"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from numpy import array\n",
+      "\n",
+      "#Variables\n",
+      "T1=373.15;                                                           #temp.of  tea,K\n",
+      "XN2=0.7808;                                                          #mole  fraction  of  nitrogen\n",
+      "XO2=0.2095;                                                          #mole  fraction  of  oxygen\n",
+      "Xar=0.0093;                                                          #mole  fraction  of\n",
+      "Cp=1006                                                                  #mixture  diffusivity,j/(kg*K)\n",
+      "\n",
+      "#Calculations\n",
+      "a=array(([3.798,  3.467,  3.542]));                                     #collisin  diameter,m\n",
+      "b=array(([71.4,  106.7,  93.3]));                                       #lennard  jones  constant,K\n",
+      "M=array(([28.02,  32,  39.95]));                                        #molar  masses,kg/kmol\n",
+      "c=array(([0.9599,  1.057,  1.021]));                                    #potential  well  function\n",
+      "d=array(([1.8*10**-5,  2.059*10**-5,  2.281*10**-5]));                  #calculated  viscosity,kg/(m*s)\n",
+      "e=array(([1.8*10**-5,  2.07*10**-5,  2.29*10**-5]));                    #  theoritical  viscosity,kg/(m*s)\n",
+      "f=array(([0.0260,  0.02615,  0.01787]));                                #theoritical  thermal  conducitvity,W/(m*K)\n",
+      "\n",
+      "u=2.6693*10**-6*(M*T1)**0.5/((a**2*c));                                  #viscosity,kg/(m*s)\n",
+      "k=0.083228/((a**2*c*(T1/M**0.5)))                                        #thermal  conductivity,W/(m*s)\n",
+      "umc = XN2*u.item(0)/0.9978+XO2*u.item(1)/1.008+Xar*u.item(2)/0.9435  ;   #calculated  mixture  viscosity,kg/(m*s)\n",
+      "umc1=1.857*10**-5;\n",
+      "\n",
+      "umd=XN2*e.item(0)/0.9978+XO2*e.item(1)/1.008+e.item(2)*Xar/0.9435;       #theoritical  mixture  viscosity,kg/(m*s)\n",
+      "kmc=XN2*k.item(0)/0.9978+XO2*k.item(1)/1.008+Xar*k.item(2)/0.9435;       #calculated  thermal  conducitvity,W/(m*K)\n",
+      "kmc1=0.02623;\n",
+      "kmd=XN2*f.item(0)/0.9978+XO2*f.item(1)/1.008+Xar*f.item(2)/0.9435;       #theoritical  thermal  conductivity,  W/(m*K)\n",
+      "pr=umd*Cp/kmd;                                                           #prandtl  no.\n",
+      "\n",
+      "#Result\n",
+      "print \"Theoritical mixture viscosity is :\",round(umc1,6),\"kg/(m*s)\\n\"\n",
+      "print \"Calculated mixture viscosity is :\",round(umd,6),\"kg/(m*s)\\n\"\n",
+      "print \"Theoritical thermal conducitvity is :\",round(kmc1,4),\" W/(m*K)\\n\"\n",
+      "print \"Calculated thermal conducitvity is :\",round(kmd,4),\"W/(m*K)\\n\"                                           \n",
+      "print \"Prandtl no. is :\",round(pr,4),\"\\n\"\n",
+      "\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Theoritical mixture viscosity is : 1.9e-05 kg/(m*s)\n",
+        "\n",
+        "Calculated mixture viscosity is : 1.9e-05 kg/(m*s)\n",
+        "\n",
+        "Theoritical thermal conducitvity is : 0.0262  W/(m*K)\n",
+        "\n",
+        "Calculated thermal conducitvity is : 0.026 W/(m*K)\n",
+        "\n",
+        "Prandtl no. is : 0.7214 \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.5, Page number: 632"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from numpy import array\n",
+      "import matplotlib.pyplot as plt\n",
+      "%matplotlib inline\n",
+      "\n",
+      "#Variables\n",
+      "Patm=101.325;\t\t\t#Atmospheric pressure in kPa.\n",
+      "Mh20=18.02;\t\t\t\t#Molecular mass of H20 in kg/kmol.\n",
+      "Mair=28.96;\t\t\t\t#Molecular mass of air in kg/kmol.\n",
+      "Psat  =array(([0.6113,  1.2276,  2.3385,  4.2461,  7.3837,  12.35,  19.941,  31.188,  47.39,  70.139,  101.325]));\t\t#Saturated pressure of watrer in kPa \n",
+      "T=array(([0.01,  10,  20,  30,  40,  50,  60,  70,  80,  90,  100]));\t\t#Temperature of air in in degree C\n",
+      "#Calculations\n",
+      "xw=Psat/Patm;\t\t\t\t\n",
+      "\n",
+      "mw=(xw*Mh20)/(xw*Mh20+(1-xw)*Mair);\t\t#Mass fraction of water vapour.\n",
+      "#Result\n",
+      "plt.plot(T,mw);\n",
+      "plt.xlabel(\"Temperature(Degree C)\")\n",
+      "plt.ylabel(\"Mass  fraction  of  water  vapour\");\n",
+      "plt.show()\n",
+      "\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": "iVBORw0KGgoAAAANSUhEUgAAAYcAAAEPCAYAAACp/QjLAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz\nAAALEgAACxIB0t1+/AAAIABJREFUeJzt3XlcVPX+P/AXmxtq5o5AoYDsIrglipKGmIqlmeJ2FQnJ\n3ErrV997b4bZ1bzebql071UrLRfEyBtmSqaCuYCWqJB4U1QScMOdRbbh8/vjxAiyzDBw5swwr+fj\nMQ+YmTOf855Tnjef3UwIIUBERFSJudIBEBGR4WFyICKiapgciIioGiYHIiKqhsmBiIiqYXIgIqJq\nZE0Os2bNQpcuXeDl5VXrMQsWLICzszO8vb1x6tQpOcMhIiItyZocQkNDER8fX+v7e/bsQUZGBi5c\nuID169djzpw5coZDRERakjU5+Pv748knn6z1/V27dmHGjBkAgAEDBuDevXu4ceOGnCEREZEWFO1z\nyMnJgb29vfq5nZ0dsrOzFYyIiIgAA+iQfnz1DjMzM4UiISKiCpZKntzW1hZZWVnq59nZ2bC1ta12\nnJOTEy5evKjP0IiIjJ6joyMyMjJ0+qyiNYexY8fiq6++AgAkJyejXbt26NKlS7XjLl68CCEEH0Lg\nvffeUzwGQ3nwWvBa8FrU/FixQmD2bNGgP6plrTlMnjwZhw4dwq1bt2Bvb4+lS5eitLQUABAREYFR\no0Zhz549cHJygrW1NTZu3ChnOERETZ4QwObNwLp1wPr1upcja3KIjo7WeExUVJScIRARmZQzZ4DC\nQsDPr2HlKN4hTfUTEBCgdAgGg9fiEV6LR0z9WmzZAkydCpg38O5uJoQw+M1+zMzMYARhEhEpSqUC\n7O2BAwcAN7eG3TtZcyAiaiISEoBu3aTE0FBMDkRETcTmzcC0aY1TFpuViIiagIICwNYW+N//gK5d\npdfYrEREZOJ27QKeeeZRYmgoJgcioiZgyxZg+vTGK4/NSkRERu7mTaBnTyAnB7C2fvQ6m5WIiExY\nTAwQHFw1MTQUkwMRkZHbsqXxRilVYHIgIjJiv/0G/P47MHx445bL5EBEZMS2bgUmTwYsG3mlPEX3\ncyAiIt0JITUpff1145fNmgMRkZFKSgJatAB8fRu/bCYHIiIjVdERLcfuypznQERkhEpKpEX2fvkF\ncHCo+RjOcyAiMjHx8YC7e+2JoaGYHIiIjJAccxsqY7MSEZGRuXcPePppIDMTePLJ2o9jsxIRkQn5\n5htp0ltdiaGhmByIiIxMY6/AWhM2KxERGZErVwAfH+DqVaB587qPZbMSEZGJiI4GJkzQnBgaismB\niMhICNG4+0TXhcmBiMhIpKYC+fnAoEHyn4vJgYjISGzeDEydCpjr4c7NDmkiIiOgUgH29sD+/dLM\naG2wQ5qIqIlLSABsbLRPDA1VZ3JQqVT4+OOP9RMJERHVSh9zGyrT2KzUr18//Pzzz/qKp0ZsViIi\nU1ZYCNjaAufOAV27av+5htw7Ne4EN3jwYMybNw+TJk2CtbW1+nVfOXaXICKianbtAgYMqF9iaCiN\nNYeAgACY1bCTREJCgmxBPY41ByIyZWPGACEh9Z/f0JB7J0crEREZsNxcwNkZyM4GWreu32dlbVZa\nunSp+gSVaxBLlizR6YRERKS97dulmkN9E0NDaRzKam1tDWtra7Ru3Rrm5ubYs2cPMjMz9RAaERHJ\nvalPberdrFRcXIwRI0bg0KFDcsVUDZuViMgUnT8PDBkiNSlZamznqU6vk+AKCgqQk5Oj1bHx8fFw\ndXWFs7MzVq5cWe39W7duYeTIkejduzc8PT2xadOm+oZDRNRkbd0KTJ6sW2JoKI01By8vL/Xv5eXl\nuHnzJpYsWYL58+fXWbBKpYKLiwv2798PW1tb9OvXD9HR0XBzc1MfExkZieLiYqxYsQK3bt2Ci4sL\nbty4AcvHrgRrDkRkaoQAnJyAHTuAPn10K0PWDunvvvtOfRJLS0t07twZVlZWGgs+ceIEnJyc4ODg\nAAAICQlBXFxcleRgY2OD1NRUAMCDBw/QoUOHaomBiMgUJScDzZoBSk0p03gndnBwwOnTp3H48GGY\nmZnB398f3t7eGgvOycmBvb29+rmdnR2OHz9e5Zjw8HAMGzYM3bp1Q15eHnbs2KHDVyAianoqOqJr\nmGamFxqTw+rVq7FhwwaMHz8eQghMmzYN4eHhWLBgQZ2fq2ni3OOWL1+O3r17IzExERcvXkRgYCDO\nnDmDNm3aVDs2MjJS/XtAQAACAgI0lk9EZIxKSqTmpBMn6ve5xMREJCYmNk4QQgNPT0+Rn5+vfp6f\nny88PT01fUwkJSWJoKAg9fPly5eLDz/8sMoxzz//vDhy5Ij6+bBhw8TPP/9crSwtwiQiajLi4oQY\nPLjh5TTk3qnVaCXzSjtLmGu5y0Tfvn1x4cIFZGZmoqSkBDExMRg7dmyVY1xdXbF//34AwI0bN/Db\nb7+hR48e2mU1IqImSt8rsNZEY7NSaGgoBgwYoG5W+vbbbzFr1izNBVtaIioqCkFBQVCpVAgLC4Ob\nmxvWrVsHAIiIiMCf//xnhIaGwtvbG+Xl5fj73/+O9u3bN/xbEREZqfv3gR9+AP64VSpGq0lwJ0+e\nxNGjRwEA/v7+8PHxkT2wyjiUlYhMxRdfALt3Azt3NrwsvUyCqzgBb9JERPJRarmMx2lMDu+//z5m\nzpyJO3fu4NatWwgNDcWyZcv0ERsRkUnJygLOnAFGjVI6Ei2alXr27InU1FS0aNECAPDw4UN4e3vj\n/PnzegkQYLMSEZmGv/8dyMgA1q9vnPJkbVaytbXFw4cP1c+LiopgZ2en08mIiKhmQgCbNxtGkxKg\nxWiltm3bwsPDAyNGjAAA/Pjjj+jfvz/mz58PMzMzrFmzRvYgiYiautRU4MEDYPBgpSORaEwO48aN\nw7hx49TPK89M1mYWNBERaVbREa3lVDLZcZtQIiKFqVTAU08BP/4IuLs3Xrmyrsp6/vx5/PnPf0Z6\nerq678HMzAyXLl3S6YRERFRVYiLQtWvjJoaG0liBCQ0NxauvvgpLS0skJiZixowZmDp1qj5iIyIy\nCYYyt6Eyjc1Kvr6+SElJgZeXF9LS0qq8pi9sViKipqqwELC1BdLTARubxi1b1malFi1aQKVSwcnJ\nCVFRUejWrRsKCgp0OhkREVW1axfQv3/jJ4aG0mo/h8LCQqxZswbvvvsuHjx4gC+//FIfsRERNXmG\n2KQEaNGslJKSAl+l9qn7A5uViKgpys0FnJ2B7GygdevGL1/WGdKLFi2Cq6sr3n33Xfz66686nYSI\niKqLiQHGjJEnMTSUxuSQmJiIhIQEdOzYEREREfDy8uLCe0REjcBQm5SAek6CS0tLw8qVKxETE4PS\n0lI546qCzUpE1NRcuAD4+0tNSpYae391I2uzUnp6OiIjI+Hp6Yl58+bBz88POTk5Op2MiIgkW7cC\nISHyJYaG0lhzGDhwICZNmoSJEyeiW7du+oqrCtYciKgpEULqiN6+HejbV77zyDrPISkpSaeCiYio\nZsnJUo2hTx+lI6mdgaz/R0RkOrZsAaZPBwx5YWuuykpEpEclJdJyGSdOAN27y3suWTukiYio8fzw\nA+DqKn9iaCgmByIiPTLkuQ2VsVmJiEhP7t+XNvW5fBlo317+88nWrKRSqfDxxx/rVDAREVW1cycw\nbJh+EkND1ZkcLCwssG3bNn3FQkTUpG3ebBxNSoAWzUpvvPEGSktLMWnSJFhbW6tf1+dKrWxWIiJj\nl5UF9O4N5OQALVro55wNuXdqTA4BAQEwq2EwbkJCgk4n1AWTAxEZu7//HcjIANav1985ZU0OhoDJ\ngYiMXa9eQFQUMGSI/s4p6zyH69evIywsDCNHjgQgLcT3+eef63QyIiJTlJoqjVQaPFjpSLSnMTnM\nnDkTI0aMwNWrVwEAzs7OHMFERFQPW7YAU6cC5kY0s0xjqLdu3cKkSZNgYWEBALCysoKloa4xS0Rk\nYFQqYNs24xmlVEFjcmjdujVu376tfp6cnIwnnnhC1qCIiJqKQ4eAzp0Bd3elI6kfjVWAjz76CMHB\nwbh06RL8/PyQm5uL2NhYfcRGRGT0jGluQ2UaRysVFRXBwsICv/32G4QQcHFxQXl5OVroa6AuOFqJ\niIxTYaG0Amt6OmBjo//zyzpayc/PD1ZWVvD09ISXlxeaNWsGPz8/rQqPj4+Hq6srnJ2dsXLlyhqP\nSUxMhI+PDzw9PREQEFCv4ImIDNl33wH9+yuTGBqq1mala9eu4erVqygsLERKSgqEEDAzM8ODBw9Q\nWFiosWCVSoV58+Zh//79sLW1Rb9+/TB27Fi4ubmpj7l37x7mzp2LH374AXZ2drh161bjfCsiIgNg\nLCuw1qTW5LBv3z5s2rQJOTk5WLx4sfr1Nm3aYPny5RoLPnHiBJycnODg4AAACAkJQVxcXJXksG3b\nNrz00kuws7MDAHTs2FHX70FEZFByc4HDh4HoaKUj0U2tyWHGjBmYMWMGYmNjMWHChHoXnJOTA3t7\ne/VzOzs7HD9+vMoxFy5cQGlpKZ599lnk5eVh4cKFmD59er3PRURkaHbsAEaPBlq3VjoS3WgcrTRh\nwgTs3r0b6enpKCoqUr++ZMmSOj9X03pMjystLUVKSgoOHDiAwsJCDBw4EM888wycnZ21CJ2IyHBt\n2QJouE0aNI3JISIiAg8fPsTBgwcRHh6Or7/+GgMGDNBYsK2tLbKystTPs7Ky1M1HFezt7dGxY0e0\nbNkSLVu2xJAhQ3DmzJkak0NkZKT694CAAHZeE5HBunBB2tAnMFC/501MTERiYmLjFCY08PT0FEII\n4eXlJYQQIi8vTwwaNEjTx0Rpaano0aOHuHz5siguLhbe3t4iPT29yjHnzp0Tw4cPF2VlZaKgoEB4\nenqKs2fPVitLizCJiAzGe+8JsXCh0lE07N6psebQsmVLAECrVq2Qk5ODDh064Pr16xqTjqWlJaKi\nohAUFASVSoWwsDC4ublh3bp1AKQaiaurK0aOHIlevXrB3Nwc4eHhcDe2aYRERJUIITUpbd+udCQN\no3ES3Pvvv4/58+fj4MGDmDt3LgAgPDwcy5Yt00uAACfBEZHx2LcPWLhQmvimRderrPS2n0NRURGK\niorQrl07nU6mKyYHIjIGBQXSvg1r1kgjlZQma3IYPHgwhg4dCn9/fwwaNAht2rTR6UQNweRARMZg\n0SLg5k2pWckQyJocLl26hMOHD+PIkSNISkpCixYtMHjwYHzyySc6nVAXTA5EZOiSk4Fx44C0NMBQ\n5vM25N6psUO6R48eaNGiBZo3bw4rKyskJCTg3LlzOp2MiKgpKi4GZs2SmpMMJTE0lMaag6OjIzp2\n7IgpU6Zg8ODB8PHxgbmetzNizYGIDNlf/yp1QH/zjfKd0JXJ2qy0evVqHD58GNnZ2XBxccHQoUMx\nZMgQODk56XRCXTA5EJGhOn0aGDECOHPG8FZf1ctopfz8fGzcuBGrVq1CTk4OVCqVTifUBZMDERmi\n0lJgwABgwQJg5kylo6lO1uSwePFiHD58GPn5+fDz84O/vz8GDx4MR0dHnU6oCyYHIjJEK1ZI24Du\n3WtYzUkVZE0OX3/9NYYMGYIuXbrodILGwORARIbmf/8D/P2BX34Bnn5a6WhqprdJcEphciAiQ6JS\nAUOGAFOmAH8sHGGQZN0mlIiIqvr0U8DCApgzR+lI5MOaAxFRPVy6JO0LfewY0LOn0tHUjTUHIiI9\nEAKYPRt4+23DTwwNxeRARKSlzz8H7t8H3nhD6UjkV2uzUlFREVq0aKHveGrEZiUiUlpODtC7N3Dw\nIODlpXQ02pGlWcnPzw8AMG3aNN2iIiJqIoSQOp/nzjWexNBQtS68V1xcjK1bt+LYsWPYuXNnlexj\nZmaG8ePH6yVAIiKlbd8u7QkdG6t0JPpTa3L4z3/+g61bt+L+/fv47rvvqr3P5EBEpiA3V+pj+O47\noFkzpaPRH41DWT/77DO88sor+oqnRuxzICKlhIQA9vbAqlVKR1J/ss6QLikpwb///W/89NNPAICA\ngAC8+uqrsLKy0umEumByICIlxMUBb70lrbjasqXS0dSfrMkhLCwMZWVlmDFjBoQQ2Lx5MywtLfHZ\nZ5/pdEJdMDkQkb7duwd4egLbtklLZRgjWZNDr169kJqaqvE1OTE5EJG+hYUBLVpIS2UYK1m3CbW0\ntERGRoZ6c5+LFy/C0lLjx4iIjNaPPwIHDkj7QZsqjXf5VatWYdiwYejevTsAIDMzExs3bpQ9MCIi\nJeTnS0tkrFsHtGmjdDTK0WrhvaKiIvz2228wMzNDz5499T5zms1KRKQvCxYADx4AmzYpHUnDcT8H\nIqJGcOQIMGmS1JzUvr3S0TQcV2UlImqghw+lTui1a5tGYmgo1hyIiAC88460V8OOHUpH0nhkHa1E\nRNTUnTwJbNwI6HGEvsFjsxIRmbSSEmDWLOCjj4AuXZSOxnAwORCRSVu5ErCzA6ZOVToSw6JVn4NK\npcKNGzdQVlamfu2pp56SNbDK2OdARHI4exYICABSUqTF9ZoaWfsc1q5di6VLl6Jz586wsLBQv55m\nylMHicjoqVRSc9IHHzTNxNBQGmsOjo6OOHHiBDp06KCvmKphzYGIGttHHwG7d0vLZJg30QZ2WWsO\nTz31FNq2batT4UREhigjA1ixAjh+vOkmhobSmBy6d++OZ599FqNHj0azP7ZBMjMzw6JFi2QPjoio\nsZWXA6+8AvzlL4Cjo9LRGC6NOfOpp57Cc889h5KSEuTn5yMvLw95eXlaFR4fHw9XV1c4Oztj5cqV\ntR73888/w9LSEjt37tQ+ciIiHaxfDxQXS2soUe20niFdkRDaaLlMoUqlgouLC/bv3w9bW1v069cP\n0dHRcHNzq3ZcYGAgWrVqhdDQULz00kvVg2SfAxE1gqwswNcXOHQIcHdXOhr5ybq2UlpaGnx8fODh\n4QEPDw/06dMHv/76q8aCT5w4AScnJzg4OMDKygohISGIi4urdtzatWsxYcIEdOrUSacvQESkDSGA\niAhg4ULTSAwNpTE5zJ49G//85z9x5coVXLlyBR999BFmz56tseCcnBzYVxofZmdnh5ycnGrHxMXF\nYc6cOQCkLEdEJIctW4CrV4G331Y6EuOgsUO6sLAQzz77rPp5QEAACgoKNBaszY3+9ddfx4cffqiu\n+rDpiIjkcP068OabwN69gJWV0tEYB61GKy1btgzTp0+HEAJbt25Fjx49NBZsa2uLrKws9fOsrCzY\n2dlVOebkyZMICQkBANy6dQt79+6FlZUVxo4dW628yMhI9e8BAQEICAjQGAMREQDMmydNePP1VToS\neSUmJiIxMbFRytLYIX3nzh289957OHr0KADA398fkZGRePLJJ+ssuKysDC4uLjhw4AC6deuG/v37\n19ghXSE0NBTBwcEYP3589SDZIU1EOvrmG2nY6unTgJ43sVScrJPg2rdvj7Vr19a/YEtLREVFISgo\nCCqVCmFhYXBzc8O6desAABEREfWPloioHu7cAebPB77+2vQSQ0PVWnNYuHAhVq9ejeDg4OofMjPD\nrl27ZA+u8vlYcyCi+poxA2jXDli9WulIlCFLzeFPf/oTAGDx4sU1npCIyJDt3QscPswNfHRVa3Lo\n06cPAOD06dN4/fXXq7z3ySefYOjQofJGRkSkowcPgFdfBT7/HGjdWulojJPGDmkfHx+cOnWqymu9\ne/fG6dOnZQ2sMjYrEVF9vPaatMPbZ58pHYmyZGlWio6OxrZt23D58uUq/Q55eXmKLt9NRFSXxERg\n1y5Ai4UcqA61Jgc/Pz/Y2NggNzcXb775pjr7tG3bFr169dJbgERE2ioslFZc/de/pI5o0p3GZqVL\nly7BxsYGLVu2BAA8fPgQN27cgIODgz7iA8BmJSLSTAhg7lzg7l0gOlrpaAyDrAvvTZw4scr2oObm\n5pgwYYJOJyMikoNKJXVAnzgBREUpHU3ToHESXFlZmXqTHwBo3rw5SktLZQ2KiEhbRUXAlClAXh6Q\nkABouasAaaCx5tCxY8cqS23HxcWhY8eOsgZFRKSN+/eBkSOBZs2k/aCZGBqPxj6HjIwMTJ06FVev\nXgUgLb29efNmODk56SVAgH0ORFTd9evA888DgwdLM6C5F3R1Dbl31msnODMzM7RWYEYJkwMRVXbx\nIhAUJC2P8de/Aly0oWayLrwHALt370Z6ejqKiorUry1ZskSnExIRNcSpU8CYMcCSJdLObiQPjckh\nIiICDx8+xMGDBxEeHo6vv/4aAwYM0EdsRERVJCYCEycC//43UMN289SINDYreXl5IS0tDb169UJq\nairy8/MxcuRIHDlyRF8xslmJiLBzpzRcNSYGqLQ5JdVB1nkOFZPfWrVqhZycHFhaWuL69es6nYyI\nSBcbNki7uf3wAxODvmhsVgoODsbdu3fx1ltvqVdqDQ8Plz0wIiIhgL/9Ddi4EfjpJ0CPgyRNXp3N\nSuXl5UhKSsKgQYMAAEVFRSgqKkI7PS9awmYlItNTXg4sXCjtybB3L2Bjo3RExkfWoaz6Xp67JkwO\nRKalpEQapnr1qrTC6hNPKB2RcZK1z+G5555DbGwsb85EpBf5+dJQ1aIiqY+BiUEZGmsOrVu3RmFh\nISwsLNDijx26zczM8ODBA70EWHE+Jieipi83Fxg9GvD2loarWmo1E4tqI0vN4ejRowCAW7duoby8\nHKWlpcjLy0NeXp5eEwMRmYbff5eWwggMBNavZ2JQWq3JYcGCBQCkTX+IiOT0669SYpg7VxqdxOUw\nlFdrbra0tER4eDiys7OxYMGCKlUTMzMzrFmzRi8BElHTdvQoMH488PHH0tLbZBhqTQ67d+/GgQMH\nsG/fPvTp0wdCCHX7lRnTOhE1gt27gdBQYMsWaSE9MhwaO6RPnz6N3r176yueGrFDmqjp+fJL4O23\ngbg4gMu1yUMvS3YricmBqGlZtUrazvOHHwBXV6WjabpkX7KbiKgxlJdLtYU9e6S+Bjs7pSOi2jA5\nEJFelJYCr7wCXLggLYnRvr3SEVFdmByISHaFhdI+DEIA+/cDrVopHRFpwl1XiUhWd+5IE9vatwe+\n/ZaJwVgwORCRbLKzgSFDgIEDgU2bACsrpSMibWlMDjt27FAvl7Fs2TKMGzcOKSkpsgdGRMbtf/+T\nZj3PmAH84x+AOf8UNSoa/3MtW7YMbdu2xZEjR3DgwAGEhYVhzpw5+oiNiIzUiRNAQADw3nvAW28p\nHQ3pQmNysLCwACDNmA4PD8eYMWNQUlIie2BEZJz27ZNWVt2wQZr9TMZJY3KwtbXF7NmzERMTg9Gj\nR6OoqAjl5eX6iI2IjEx0NDB9OvDf/wLBwUpHQw2hcYZ0QUEB4uPj0atXLzg7O+PatWtIS0vDiBEj\n9BUjZ0gTGYE1a6SZz3v2AF5eSkdDgMw7wV2/fh2jR4+Gs7MzEhISsGPHDvTv31/rE8THx8PV1RXO\nzs5YuXJltfe3bt0Kb29v9OrVC4MGDUJqamr9vgERKeq334AXXpA25zl8mImhqdCYHMaPHw9LS0tk\nZGQgIiIC2dnZmKLluroqlQrz5s1DfHw80tPTER0djXPnzlU5pkePHvjpp5+QmpqKd999F7Nnz9bt\nmxCRXt2+DSxcKI1I8vcHTp8GHByUjooai8bkYG5uDktLS+zcuRPz58/HqlWrcO3aNa0KP3HiBJyc\nnODg4AArKyuEhIQgLi6uyjEDBw7EE39sEjtgwABkZ2fr8DWISF9KSqS9F1xdgbIyID0dePNNoHlz\npSOjxqQxOTRr1gzbtm3DV199hTFjxgAASktLtSo8JycH9vb26ud2dnbIycmp9fjPP/8co0aN0qps\nItIvIaSOZg8PaQmMQ4eATz8FOnVSOjKSg8a1lb744gv85z//wV/+8hd0794dly5dwrRp07QqvD6b\nAiUkJOCLL75Q7139uMjISPXvAQEBCAgI0LpsImqYkyeBRYukpTA+/RTQ43gUqofExEQkJiY2Slmy\n7ueQnJyMyMhIxMfHAwBWrFgBc3NzvP3221WOS01Nxfjx4xEfHw8nJ6fqQXK0EpEicnKAP/9Zmrvw\n/vvArFnAH1OfyAjIOlrp/PnzmDBhAtzd3dG9e3d0794dPXr00Krwvn374sKFC8jMzERJSQliYmIw\nduzYKsdcuXIF48ePx5YtW2pMDESkfwUFQGQk0KuXtOfC+fNAeDgTgynR2KwUGhqKpUuXYtGiRUhM\nTMTGjRuhUqm0K9zSElFRUQgKCoJKpUJYWBjc3Nywbt06AEBERATef/993L17V70kh5WVFU6cONGA\nr0REuiovB776CvjrX4GhQ4GUFODpp5WOipSgsVnJ19cXKSkp8PLyQlpaWpXX9IXNSkTyS0gAFi8G\nWrYE/vlP7uvcFMi6TWiLFi2gUqng5OSEqKgodOvWDQUFBTqdjIgMz/nzwP/7f8CZM8DKlcDLLwP1\nGEtCTZTGPodPPvkEhYWFWLNmDX755Rds2bIFX375pT5iIyIZ3bkDvP464OcnPc6dk3ZrY2IgQObR\nSo2FzUpEjaekBPjXv4Dly4EJE6SO586dlY6K5CBLs1JwcHCtBZuZmWHXrl06nZCIlCEEsGuXtL+C\nk5PUx+DhoXRUZKhqTQ7Jycmws7PD5MmTMeCPnqmKRFGfyW1EpLyUFKmzOTcXWLsWCApSOiIydLU2\nK5WVleHHH39EdHQ00tLSMHr0aEyePBkeCvypwWYlIt3k5EjDUuPjgaVLpUlslhqHoVBTIcskOEtL\nSzz//PP46quvkJycDCcnJwwdOhRRUVE6B0pE+lFQICWDXr0AGxtpWe3Zs5kYSHt1/q9SVFSE77//\nHtu3b0dmZiYWLlyIcePG6Ss2Iqqn8nJg82bgL3+RltE+eZLLaJNuam1Wmj59Os6ePYtRo0Zh0qRJ\n8FJwBw82KxFpduiQtDhes2bSJLaBA5WOiJTWkHtnrcnB3Nwc1tbWtZ7wwYMHOp1QF0wORLU7d06q\nKaSkSJPYOFeBKsgylLW8vFzngIhIXteuAdu3A9u2AVlZ0mS2bduAFi2UjoyaCk6CIzIS9+4BO3dK\nSSAlBXhsZfpGAAARMUlEQVTxRWDKFCAggB3NVDNZmpUMCZMDmaqHD4Hvv5cSwoEDwHPPSQlh9GjW\nEkgzJgeiJqSsDDh4UEoIcXFA375SQhg3DmjXTunoyJgwORAZOSGAEyekhBATI+2hMGWK1LlsY6N0\ndGSsZF2ym4jkc+6clBC2bQOsrKSEcOSItPYRkZKYHIj0LCvr0UijmzeByZOBr78GfHw4BJUMB5uV\niPTg9m3gm2+ArVuBX38FXnpJqiX4+3NfZpIP+xyIDFBBAfDdd1IN4dAhYORIYOpUaUXU5s2Vjo5M\nAZMDkYEoLQV+/FFKCLt3S0tYTJkizUlo00bp6MjUMDkQKai8HDh2TEoIsbGAs7OUEF5+mTuskbI4\nWolIz+7fl4aeHjggdS63bi01GR0/DnTvrnR0RA3H5ECkgUoFpKcDycmPHleuAH36AIMGSVtvenlx\npBE1LWxWInrMzZtSDaAiEfz8szQR7ZlnpMfAgYCnJ9czIsPHPgciHZWUAKmpUhJISpJ+3r4NDBjw\nKBn07w906KB0pET1x+RApKXs7KrNQ6dPAz16VK0VuLgA5rVuoEtkPJgciGrw8KG0TWblZFBcLCWA\nimTQrx+HmFLTxeRAJk8I4NKlR0kgKUnqRPbweJQInnlGqiWw45hMBZMDmZy7d6UNbyrXCpo3r1or\n8PUFWrZUOlIi5TA5UJNTVib1D1y8KNUIKn5W/F5WBnh7V60V2NkpHTWRYWFyIKP04MGjG37lBHDx\norRyaefOgKOj1BTUo0fV3zt2ZPMQkSZMDmSQysuBnJyab/6XLgGFhTXf+B0dpc1uuA0mUcMwOZBi\nCgqAy5drbvr5/XfgySdr/+u/Sxf+9U8kJyYHalRCAPfuAbduAbm51X/euPEoCdy7J60l9PjN39ER\ncHAAWrVS+tsQmS4mB6pTcXHNN/rabv63bwPW1lK7fqdO1X927vwoGdjYcMIYkaEy2OQQHx+P119/\nHSqVCq+88grefvvtascsWLAAe/fuRatWrbBp0yb4+PhUD5LJQU3TX/U1/Swqkm7std3sH//ZoQPQ\nrJnS35SIGsogl+xWqVSYN28e9u/fD1tbW/Tr1w9jx46Fm5ub+pg9e/YgIyMDFy5cwPHjxzFnzhwk\nJyfLFZLeCSF1uubnS23z+flVHzW9punYO3cS0bp1QK1/0Xt4VH+9bdum2bafmJiIgIAApcMwCLwW\nj/BaNA7ZksOJEyfg5OQEBwcHAEBISAji4uKqJIddu3ZhxowZAIABAwbg3r17uHHjBrp06SJLTCqV\n1MRSXCwtuFafn8XF2t/gK14rKJBG3LRuLT2srR/9XtNrNjZ1H2dtDURFJWLZsgBZro+x4U3gEV6L\nR3gtGodsySEnJwf29vbq53Z2djh+/LjGY7Kzs2tMDnPn1v+G/vhPIaRZtM2bS80mdf2s6bWKG/WT\nTwL29rXf5CserVo1/ubx3IyeiPRBtuRgpmU7xuPtYbV9zs1Nu5t6XT+5/j4RkZaETJKSkkRQUJD6\n+fLly8WHH35Y5ZiIiAgRHR2tfu7i4iKuX79erSxHR0cBgA8++OCDj3o8HB0ddb6Hy/a3dN++fXHh\nwgVkZmaiW7duiImJQXR0dJVjxo4di6ioKISEhCA5ORnt2rWrsUkpIyNDrjCJiKgGsiUHS0tLREVF\nISgoCCqVCmFhYXBzc8O6desAABERERg1ahT27NkDJycnWFtbY+PGjXKFQ0RE9WAUk+CIiEi/DHpu\na3x8PFxdXeHs7IyVK1cqHY5eZWVl4dlnn4WHhwc8PT2xZs0aAMCdO3cQGBiInj17YsSIEbh3757C\nkeqPSqWCj48PgoODAZjutbh37x4mTJgANzc3uLu74/jx4yZ7LVasWAEPDw94eXlhypQpKC4uNplr\nMWvWLHTp0gVeXl7q1+r67itWrICzszNcXV2xb98+jeUbbHKomEQXHx+P9PR0REdH49y5c0qHpTdW\nVlb4+OOPcfbsWSQnJ+PTTz/FuXPn8OGHHyIwMBDnz5/H8OHD8eGHHyodqt6sXr0a7u7u6hFtpnot\nFi5ciFGjRuHcuXNITU2Fq6urSV6LzMxMbNiwASkpKUhLS4NKpcL27dtN5lqEhoYiPj6+ymu1fff0\n9HTExMQgPT0d8fHxeO2111BeXl73CXTuypbZsWPHqox2WrFihVixYoWCESnrhRdeED/++GOVEV3X\nrl0TLi4uCkemH1lZWWL48OHi4MGDYsyYMUIIYZLX4t69e6J79+7VXjfFa3H79m3Rs2dPcefOHVFa\nWirGjBkj9u3bZ1LX4vLly8LT01P9vLbv/vho0aCgIJGUlFRn2QZbc6hpglxOTo6CESknMzMTp06d\nwoABA6rMIO/SpQtu3LihcHT68cYbb2DVqlUwr7TKnylei8uXL6NTp04IDQ2Fr68vwsPDUVBQYJLX\non379li8eDGeeuopdOvWDe3atUNgYKBJXosKtX33q1evwq7SVona3E8NNjloO4muqcvPz8dLL72E\n1atXo02bNlXeMzMzM4nrtHv3bnTu3Bk+Pj61LiJmKteirKwMKSkpeO2115CSkgJra+tqzSamci0u\nXryITz75BJmZmbh69Sry8/OxZcuWKseYyrWoiabvrum6GGxysLW1RVZWlvp5VlZWlcxnCkpLS/HS\nSy9h+vTpePHFFwFIfw1cv34dAHDt2jV07txZyRD14tixY9i1axe6d++OyZMn4+DBg5g+fbpJXgs7\nOzvY2dmhX79+AIAJEyYgJSUFXbt2Nblr8csvv8DPzw8dOnSApaUlxo8fj6SkJJO8FhVq+zfx+P00\nOzsbtra2dZZlsMmh8iS6kpISxMTEYOzYsUqHpTdCCISFhcHd3R2vv/66+vWxY8fiyy+/BAB8+eWX\n6qTRlC1fvhxZWVm4fPkytm/fjmHDhmHz5s0meS26du0Ke3t7nD9/HgCwf/9+eHh4IDg42OSuhaur\nK5KTk/Hw4UMIIbB//364u7ub5LWoUNu/ibFjx2L79u0oKSnB5cuXceHCBfTv37/uwhq7g6Qx7dmz\nR/Ts2VM4OjqK5cuXKx2OXh0+fFiYmZkJb29v0bt3b9G7d2+xd+9ecfv2bTF8+HDh7OwsAgMDxd27\nd5UOVa8SExNFcHCwEEKY7LU4ffq06Nu3r+jVq5cYN26cuHfvnslei5UrVwp3d3fh6ekp/vSnP4mS\nkhKTuRYhISHCxsZGWFlZCTs7O/HFF1/U+d3/9re/CUdHR+Hi4iLi4+M1ls9JcEREVI3BNisREZFy\nmByIiKgaJgciIqqGyYGIiKphciAiomqYHIiIqBomB5LF7du34ePjAx8fH9jY2MDOzg4+Pj7w9fVF\nWVmZ0uFVcejQISQlJTVqmTdv3sTo0aMBAImJiXjiiSfg6+sLV1dXDB06FN9//32jnq8hSktL8c47\n76Bnz57o06cP/Pz81Kt9Dh8+HHl5eQpHSEqQbSc4Mm0dOnTAqVOnAABLly5FmzZtsGjRIsXiUalU\nsLCwqPG9hIQEtGnTBgMHDtS6vLKyMlha1v7PJyoqCjNnzlQ/HzJkCL777jsAwJkzZ/Diiy+iZcuW\nGDZsmNbnrEnFNKWGrB/07rvv4saNGzh79iysrKxw8+ZNHDp0CAAQEhKCDRs2KPrfjpTBmgPphRAC\nJ0+eREBAAPr27YuRI0eq14AJCAjAokWL0K9fP7i5ueHnn3/GuHHj0LNnT7z77rsApJVpXV1dMW3a\nNLi7u+Pll1/Gw4cPAaDOct944w3069cPq1evxu7du/HMM8/A19cXgYGBuHnzJjIzM7Fu3Tp8/PHH\n8PX1xZEjRzBz5kx888036thbt24NQKoB+Pv744UXXoCnpyfKy8vx1ltvoX///vD29sb69evVn4mN\njVXXHB7n7e2NJUuWICoqCgCQm5uLCRMmoH///ujfvz+OHTumfj0wMBCenp4IDw+Hg4MD7ty5g8zM\nTLi4uGDGjBnw8vJCVlYWVq1apY4jMjJSfa4tW7ZgwIAB8PHxwauvvlptDf/CwkJ89tlnWLt2Lays\nrAAAnTt3xssvvwzg0bILZILkmtpNVCEyMlKsWrVK+Pn5idzcXCGEENu3bxezZs0SQggREBAg3nnn\nHSGEEKtXrxY2Njbi+vXrori4WNjZ2Yk7d+6Iy5cvCzMzM3Hs2DEhhBCzZs0S//jHP0RpaakYOHCg\nuHXrVo3lzp07Vx1H5aUENmzYIBYvXqyO76OPPlK/N3PmTBEbG6t+3rp1ayGEEAkJCcLa2lpkZmYK\nIYRYt26d+OCDD4QQQhQVFYm+ffuKy5cvi2vXrlVZYz8hIUG9B0WFU6dOCTc3NyGEEJMnTxZHjhwR\nQgjx+++/q1+fO3eueg3++Ph4YWZmJm7fvi0uX74szM3NxfHjx4UQQvzwww9i9uzZQgghVCqVGDNm\njPjpp59Eenq6CA4OFmVlZUIIIebMmSO++uqrKnGcOXNG+Pj41Pwf7g/du3cX+fn5dR5DTQ+blUgv\niouL8euvvyIwMBCA1MzTrVs39fsViyp6enrC09NTvSZ9jx49kJWVhbZt28Le3l7d9DNt2jSsWbMG\nI0eOxNmzZ/Hcc8/VWO6kSZPUv2dlZWHixIm4fv06SkpK0KNHD/V7QstVZPr374+nn34aALBv3z6k\npaUhNjYWAPDgwQNkZGSgTZs2sLGxqbOcyufbv39/lV0O8/LyUFBQgKNHj+Lbb78FAAQFBeHJJ59U\nH/P000+rF07bt28f9u3bBx8fHwBAQUEBMjIycObMGZw8eRJ9+/YFADx8+BBdu3bV6ntW1qVLF2Rl\nZcHV1bXenyXjxeRAeiGEgIeHh7rJ5HHNmzcHAJibm6t/r3he0YFduV1dCAEzMzON5VpbW6t/nz9/\nPt58802MGTMGhw4dqtL8UpmlpaW6+aW8vBwlJSU1lgdIfQsVCa/C8ePHNSabU6dOwd3dXf1djh8/\njmbNmlU7rrZyHo/j//7v/zB79uxqsc2YMQPLly+vNQ4nJydcuXIFeXl51fYLqRyDqe6JYMrY50B6\n0bx5c+Tm5iI5ORmANEImPT29XmVcuXJF/flt27bB398fLi4udZZb+eb64MEDda1i06ZN6tfbtGlT\nZUSOg4MDTp48CQDYtWsXSktLa4wnKCgI//rXv9TJ6/z58ygsLMTTTz+t7veoSWpqKj744APMnTsX\nADBixAisWbNG/f6ZM2cAAIMGDcKOHTsASLWDu3fv1hrHF198gYKCAgDSLoq5ubkYPnw4YmNjkZub\nC0DafP7KlStVPtuqVSuEhYVh4cKF6u+Zm5urrg0B0u5ipraXCjE5kJ5YWFggNjYWb7/9Nnr37g0f\nH58ah4/WtXuVi4sLPv30U7i7u+P+/fuYM2cOrKys6iy3clmRkZF4+eWX0bdvX3Tq1En9XnBwMP77\n3//Cx8cHR48eRXh4OA4dOoTevXsjOTlZ3SH9eHmvvPIK3N3d4evrCy8vL8yZMwcqlQpdu3ZFWVkZ\nCgsL1Z85fPiweijrvHnzsHbtWjz77LMAgDVr1uCXX36Bt7c3PDw8sG7dOgDAe++9h3379sHLywux\nsbHo2rWr+q/7ynEEBgZiypQpGDhwIHr16oWJEyciPz8fbm5u+OCDDzBixAh4e3tjxIgRNSatDz74\nAJ06dYK7uzu8vLwQHByMJ554AgBw/fp1dOjQoVpNhZo+LtlNRiEzMxPBwcFIS0tTOhStREZGws3N\nrUqfR32VlJTAwsICFhYWSEpKwty5c5GSktKIUWq2fv16FBQU4I033tDreUl57HMgo2FM7d5z587F\njBkzGpQcrly5gokTJ6K8vBzNmjXDhg0bGjFC7cTExCAuLk7v5yXlseZARETVsM+BiIiqYXIgIqJq\nmByIiKgaJgciIqqGyYGIiKphciAiomr+P6Ksmp778+IaAAAAAElFTkSuQmCC\n",
+       "text": [
+        "<matplotlib.figure.Figure at 0x7f4109404550>"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.6, Page number: 634"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=263.15;                                                   #temp.of  ice,K\n",
+      "p=101.325;                                                   #Atmospheric pressure, KPa\n",
+      "Molw=18.02;                                                  #Molecular mass of water vapour, g/mol\n",
+      "Mola=28.96;                                                  #Molecular mass of air, g/mol\n",
+      "\n",
+      "#Calculations\n",
+      "Pv=math.exp(21.99-6141/(T1));                                #vapor  pressure,KPa\n",
+      "xw=Pv/p;                                                     #mole  fraction  of  water\n",
+      "mw=xw*Molw/(xw*Molw+(1-xw)*Mola);                         #mass  fraction\n",
+      "\n",
+      "#Result\n",
+      "print \"Mass fraction of watervapor above the surface of ice is :\",round(mw,5),\"\\n\"\n",
+      "#end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mass fraction of watervapor above the surface of ice is : 0.0016 \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 26
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.10, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "T1=303;                                      #  isothermal  temp.,K\n",
+      "v=5;                                         #air  speed,m/s\n",
+      "l=0.05;                                      #length  of  naphthalene  model  that  is  flat,  m\n",
+      "Mnap=128.2;                                  #molar  mass  of  naphthalene,kg/kmol\n",
+      "nu=1.867*10**-5;                             #Dynamic viscocity, m^2/s\n",
+      "\n",
+      "#Calculations\n",
+      "D=0.86*(10**-5);                             #diffusion  coefficient  of  naphthalene  in  air,m/s\n",
+      "\n",
+      "Pv=10**(11.45-3729.3/T1)*133.31;             #vapor  pressure of napthalene,  Pa\n",
+      "xn=Pv/101325;                                #mole  fraction    of  naphthalene\n",
+      "mn=xn*Mnap/(xn*Mnap+(1-xn)*28.96);           #mass  fraction  of  naphthalene\n",
+      "mnp=0;                                       #mass  fraction  of  naphthalene  in  free  stream  is  0\n",
+      "\n",
+      "Rel=v*l/nu;                                  #reynolds  no.\n",
+      "Sc=nu/D;                                     #schimidt  no.\n",
+      "Nul=0.664*math.sqrt(Rel)*(Sc**(1/3));        #mass  transfer  nusselt  no.\n",
+      "Gmn=D*Nul*1.166/l;                           #gas  phase  mass  transfer  coefficient,kg/(m**2*s)\n",
+      "n=Gmn*(mn-mnp);                              #average  mass  flux,kg/(m**2*s)\n",
+      "n1=n*1000*3600;# average mass flux, g/m**2.h\n",
+      "\n",
+      "#Result\n",
+      "print \"Average rate of loss of naphthalene from a part of model is :\",round(n,7),\"kg/(m^2*s) or \",round(n1),\"g/(m^2*h)\\n\"\n",
+      "print \"Naphthalene sublimatin can be used to infer heat transfer coefficient by measuring the loss of naphthalene from a model over some length of time.since the schimidt no. of naphthalene is not generally equal to prandtl no. under the conditions of interest, some assumption about the dependence of nusselt no. on the prandtl no. must usually be introduced.\\n\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Average rate of loss of naphthalene from a part of model is : 1.61e-05 kg/(m^2*s) or  58.0 g/(m^2*h)\n",
+        "\n",
+        "Naphthalene sublimatin can be used to infer heat transfer coefficient by measuring the loss of naphthalene from a model over some length of time.since the schimidt no. of naphthalene is not generally equal to prandtl no. under the conditions of interest, some assumption about the dependence of nusselt no. on the prandtl no. must usually be introduced.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 16
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.11, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "T1=300;                                                            #temp.  of  helium-water  tube,K\n",
+      "h=0.4;                                                             #height  of  vertical  wall,m\n",
+      "m=0.087*10**-3;                                                    #flow  rate  of  helium,kg/(m**2*s)\n",
+      "#this  is  a  uniform  flux  natural  convection  problem.\n",
+      "Mhes=0.01;                                                         #  assuming  the  value  of  mass  fraction  of  helium  at  the  wall  to  be  0.01\n",
+      "Mhef=Mhes/2;                                                       #film  composition\n",
+      "af=1.141;                                                          #film  density,kg/m**3\n",
+      "wd=1.107;                                                          #wall  density,kg/m**3\n",
+      "Dha=7.119*10**-5;                                                  #diffusion  coefficient,m**2/s\n",
+      "u=1.857*10**-5;                                                    #film  viscosity  at  300K,kg/(m*s)\n",
+      "aa=1.177;                                                          #air  density,kg/m**3\n",
+      "g=9.8;                                                             #Gravity constant, m/s**2\n",
+      "#Calculations\n",
+      "Sc=(u/af)/Dha;                                                      #schimidt  no.\n",
+      "Ra1=g*(aa-wd)*m*h**4/(u*af*Dha**2*Mhes);                            #Rayleigh  no.\n",
+      "Nu=6/5*(Ra1*Sc/(4+9*math.sqrt(Sc)+10*Sc))**(1/5);                         #approximate  nusselt  no.\n",
+      "s=m*h/(af*Dha*Nu);                                                  #average concentration of helium at the wall\n",
+      "#thus  we  have  obtained  an  average  wall  concentration  14  oercent  higher  than  our  initial  guess  of  Mhes.we  repeat  this  calclations  with  revised  values  of  densities  to  obtain  Mhes  =  0.01142\n",
+      "\n",
+      "\n",
+      "#Result\n",
+      "print \"Average conentration of helium at the wall is \",round(s,5),\",since the result is within  0.5 percent of our second guess, a third iteration is not needed\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Average conentration of helium at the wall is  0.01136 ,since the result is within  0.5 percent of our second guess, a third iteration is not needed\n"
+       ]
+      }
+     ],
+     "prompt_number": 17
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.14, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=325;                                                                   #temp.  of  helium-water  tube,K\n",
+      "l=0.2;                                                                    #length  of  tube,m\n",
+      "x=0.01;                                                                   #  mole  fraction  of  water\n",
+      "R=8314.472;                                                               #gas  constant,J/(kmol*K)\n",
+      "Mw=18.02;#Molecular mass of water, g/mol\n",
+      "#the  vapor  pressure  of  the  liquid  water  is  approximately  the  saturation  pressure  at  the  water  temp.\n",
+      "\n",
+      "#Calculations\n",
+      "p=1.341*10000  ;                                                          #vapor  pressure  using  steam  table,Pa\n",
+      "x1=p/101325;                                                              #mole  fraction  of  saturated  water\n",
+      "c=101325/(R*T1);                                                          #mole  concentration  in  tube,kmol/m**3\n",
+      "D12=1.067*math.pow(10,-4);                                                #diffusivity  ofwater  with  respect  to  helium,m**2/s  \n",
+      "Nw=c*D12*math.log(1+(x-x1)/(x1-1))/l  ;                                   #molar  evaporation  rate,kmol/(m**2*s)\n",
+      "nw=Nw*Mw;                                                              #  mass  evaporation  rate,kg/(m**2*s)\n",
+      "\n",
+      "#S=1+(x1-1)*math.exp(Nw*y/(c*D12))  conentration  distribution  of  water-vapor\n",
+      "#Result\n",
+      "print \"Conentration distribution of water-vapor is  : x1(y)=1-0.8677*exp(0.6593*y) where y is expressed in meters.\\n\"\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Conentration distribution of water-vapor is  : x1(y)=1-0.8677*exp(0.6593*y) where y is expressed in meters.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 18
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.15, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "T1=1473;                                                                #suraface  temp.of  hot  water,K\n",
+      "x=0.05;                                                                 #mass  fraction  of  water\n",
+      "Gm=0.017;                                                               #average  mass    transfer  coefficient,kg/(m**2*s)\n",
+      "A=0.04;                                                                 #suraface  area  of  pan,m**2\n",
+      "\n",
+      " #only  water  vapour  passes  through  the  liquid  surface,  since  air  is  not  strongly  absorbed  into  water  under  normal  conditions.\n",
+      "#Calculations\n",
+      "p=38.58*1000;                                                           #saturation  pressure  of  water,kPa\n",
+      "Xwater=p/101325;                                                        #mole  fraction  of  saturated  water\n",
+      "Mwater=Xwater*18.02/(Xwater*18.02+(1-Xwater)*28.96);                    #mass  fraction  of  saturated  water\n",
+      "\n",
+      "B=(x-Mwater)/(Mwater-1);                                                #mass  transfer  driving  force\n",
+      "m=Gm*B*A;                                                               #evaporation  rate,kg/s\n",
+      "\n",
+      "#Result\n",
+      "print \"Evaporation rate is:\",round(m,6),\" kg/s\"\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Evaporation rate is: 0.000213  kg/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 23
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.16, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=298;                                                               #temp.of  air,K\n",
+      "T2=323.15;                                                            #film  temp.,K\n",
+      "x=0.05;                                                               #mass  fraction  of  water  at  75  C\n",
+      "Gm=0.017;                                                             #average  mass    transfer  coefficient,kg/(m**2*s)\n",
+      "A=0.04;                                                               #suraface  area  of  pan,m**2\n",
+      "l=0.2;                                                                #length  of  pan  in  flow  direction,m\n",
+      "v=5;                                                                  #air  speed,m/s\n",
+      "m=(x+0.277)/2;                                                        #film  composition  of  water  at  50  C\n",
+      "Mf=26.34;                                                             #mixture  molecular  weight,kg/kmol\n",
+      "p=101325;                                                             #Atmospheric pressure, Pa\n",
+      "R=8314.5;                                                             #Gas constant, J/kmol-K\n",
+      "Uf=1.75*math.pow(10,-5);                                              #film  viscosity,kg/(m*s)\n",
+      "B=0.314;                                                              #mass  transfer  driving  force\n",
+      "D=2.96*math.pow(10,-5);                                               #diffusivity  of  water  in  air,m**2/s\n",
+      "df=0.993;                                                             #Density of ideal air, kg/m**#\n",
+      "\n",
+      "#Calculations\n",
+      "af=p*Mf/(R*T2);                                 \t                  #film  density  from  ideal  gas  law,kg/m**3\n",
+      "Vf=Uf/af;                                                             #kinematic  viscosity,m**2/s\n",
+      "Rel=v*l/Vf;                                                           #reynolds  no.  comes  out  to  be  56,800  so  the  flow  is  laminar.\n",
+      "Sc=Vf/D;                                                              #scimidt  no.\n",
+      "Nu=0.664*math.sqrt(Rel)*math.pow(Sc,1/3);                             #nussselt  no.\n",
+      "Gmw1=Nu*(D*df/l);                                                     #appropriate  value  of  mass  transfer  gas  phase  coeffficient  of  water  in  air,kg/(m**2*s)\n",
+      "Gmw=Gmw1*(math.log(1+B)/B);                                  \t      #mass  transfer  gas  phase  coeffficient  of  water  in  air,kg/(m**2*s)\n",
+      "\n",
+      "#Results\n",
+      "print \"Mass transfer gas phase coeffficient of water in air is :\",round(Gmw,4),\"kg/(m^2*s)\\nIn this caes, the blowing factor is 0.870. Thus the mild blowing has reduced the mass transfer coefficient by about 13 percent\"\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "0.01955648559 133.069905487\n",
+        "Mass transfer gas phase coeffficient of water in air is : 0.017 kg/(m^2*s)\n",
+        "In this caes, the blowing factor is 0.870. Thus the mild blowing has reduced the mass transfer coefficient by about 13 percent\n"
+       ]
+      }
+     ],
+     "prompt_number": 28
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter1.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter1.ipynb
new file mode 100755
index 00000000..dd1cacc1
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter1.ipynb
@@ -0,0 +1,334 @@
+{
+ "metadata": {
+  "name": ""
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 1 - \"Introduction\""
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.1, Page number: 13"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "k=35;                                      #Thermal  Conductivity,  [W/m*K]\n",
+      "T1=110                                     #  Temperature  of  front[C]\n",
+      "T2=50;                                     #  Temperature  of  back,[C]\n",
+      "A=0.4                                      #area  of  slab,[m**2]\n",
+      "x=0.03;                                    #Thickness  of  slab,[m]\n",
+      "\n",
+      "#Calculations\n",
+      "q=-k*(T2-T1)/(1000*x);                     #formula  for  heat  flux[KW/m^2]\n",
+      "Q=q*A;                                     #formula  for  heat  transfer  rate[KW]\n",
+      "\n",
+      "#Results\n",
+      "print \"Heat flux is:\",q,\"KW/m^2\\n\"\n",
+      "print \"Heat transfer rate is:\",Q,\"KW \\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Heat flux is: 70.0 KW/m^2\n",
+        "\n",
+        "Heat transfer rate is: 28.0 KW \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.2, Page number: 16"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from sympy import solve,symbols\n",
+      "\n",
+      "#Variables\n",
+      "x=symbols('x');\n",
+      "k1=372;                                 #  Thermal  Conductivity  of  slab,W/m*K\n",
+      "x1=0.003;                               #  Thickness  of  slab,m\n",
+      "x2=0.002                                #  Thickness  of  steel,m\n",
+      "k2=17;                                  #  Thermal  Conductivity  of  steel,W/m*K\n",
+      "T1=400;                                 #  Temperature  on  one  side,C\n",
+      "T2=100                                  #Temperature  on  other  side,C\n",
+      "\n",
+      "#Calculations\n",
+      "Tcu=solve(x+2*x*(k1/x1)*(x2/k2)-(T1-T2),x);\n",
+      "#q=k1*(Tcu/x1)=k2*(Tss/x2);\n",
+      "Tss  =  Tcu[0]*(k1/x1)*(x2/k2);         #  formula for temperature gradient in steel side\n",
+      "Tcul=T1-Tss;\n",
+      "Tcur=T2+Tss;\n",
+      "q=k2*Tss/(1000*x2);                     #  formula for heat conducted, kW\\m^2\n",
+      "\n",
+      "#Results\n",
+      "print \"Temperature on left copper side is :\",round(Tcul,3),\"C\\n\"\n",
+      "print \"Temperature on right copper  side is :\",round(Tcur,3),\"C\\n\"\n",
+      "print \"Heat conducted through the wall is :\",round(q,3),\"kW\\m^2\\n\"\n",
+      "print \"Our initial approximation was accurate within a few percent.\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Temperature on left copper side is : 254.971 C\n",
+        "\n",
+        "Temperature on right copper  side is : 245.029 C\n",
+        "\n",
+        "Heat conducted through the wall is : 1232.749 kW\\m^2\n",
+        "\n",
+        "Our initial approximation was accurate within a few percent.\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.3, Page number: 22"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "q1=6000;                                          #Heat  flux,  W*m**-2\n",
+      "T1=120;                                           #Heater  Temperature,  C\n",
+      "T2=70;                                            #final  Temperature  of  Heater, C\n",
+      "q2=2000;                                          #final  heat  flux, W*m**-2\n",
+      "\n",
+      "#Calculations\n",
+      "h=q1/(T1-T2)                                      #formula  for  average  heat  transfer  cofficient\n",
+      "Tnew=T2+q2/h;                                     #formula  for  new  Heater  temperature, C\n",
+      "\n",
+      "#Results\n",
+      "print \"Average Heat transfer coefficient is:\",h,\"W/(m^2*K)\\n\"\n",
+      "print \"New Heater Temperature is:\",round(Tnew,3),\"C\\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Average Heat transfer coefficient is: 120.0 W/(m^2*K)\n",
+        "\n",
+        "New Heater Temperature is: 86.667 C\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.4, Page number: 25"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from numpy import array\n",
+      "from numpy import linspace\n",
+      "import matplotlib.pyplot as plt\n",
+      "from pylab import *\n",
+      "%matplotlib inline\n",
+      "\n",
+      "#Variables\n",
+      "h=250;                                  #Heat Transfer  Coefficient,  W/(m**2*K)\n",
+      "k=45;                                   #Thermal  Conductivity,  W/(m*K)\n",
+      "c=180;                                  #Heat  Capacity,  J/(kg*K)\n",
+      "a=9300;                                 #density,  kg/m**3\n",
+      "T1=200;                                 #temperature,  C\n",
+      "D=0.001;                                #diameter  of  bead, m\n",
+      "t1=linspace(0,5,50);                    #defining time interval of 0.1 seconds\n",
+      "T=linspace(0,5,50);\n",
+      "i=0;\n",
+      "\n",
+      "#Calculations\n",
+      "while i<50:\n",
+      "    T[i]=T1-c*math.exp(-t1[i]/((a*c*D)/(6*h)));      #Calculating temperature at each time in degree C\n",
+      "    i=i+1;\n",
+      "\n",
+      "plt.plot(t1,T);\n",
+      "plt.xlabel(\"Time(in sec)\");\n",
+      "plt.ylabel(\"Temperature(in degree C)\");\n",
+      "plt.title(\"Thermocouple response to a hot  gas flow\");\n",
+      "plt.show();\n",
+      "\n",
+      "Bi  =  h*(D/2)/k;                       #biot  no.\n",
+      "\n",
+      "#Results\n",
+      "print \"The value of Biot no for this thermocouple is\",round(Bi,5);\n",
+      "print \"Bi is <0.1 and hence the thermocouple could be considered as a lumped heat capacity system and the assumption taken is valid.\\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": "iVBORw0KGgoAAAANSUhEUgAAAYQAAAEZCAYAAACXRVJOAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz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\n9aVlLh5rAAAAAElFTkSuQmCC\n",
+       "text": [
+        "<matplotlib.figure.Figure at 0x7fbd3da5b8d0>"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The value of Biot no for this thermocouple is 0.00278\n",
+        "Bi is <0.1 and hence the thermocouple could be considered as a lumped heat capacity system and the assumption taken is valid.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.5, Page number: 32"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from sympy import solve,symbols\n",
+      "\n",
+      "#Variables\n",
+      "x=symbols('x');\n",
+      "T1=293;                                    #Temperature  of  air  around  thermocouple,  K\n",
+      "T2=373;                                    #Wall  temperature,  K\n",
+      "h=75;                                      #Average  Heat  Transfer  Coefficient,  W/(m**2*K)\n",
+      "s=5.67*10**-8;                             #stefan  Boltzman  constant,  W/(m**2*K**4)\n",
+      "\n",
+      "#Calculations\n",
+      "x=solve((h*(x-T1)+s*(x**4-T2**4)),x);\t   #Calculating Thermocouple Temperature, K\n",
+      "y=x[1]-273;\t\t\t\t                   #Thermocouple Temperature, C\n",
+      "\n",
+      "#Results\n",
+      "print \"Thermocouple Temperature is :\",round(y,3),\"C\\n\""
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Thermocouple Temperature is : 28.395 C\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1.6, Page number: 34"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from sympy import solve,symbols\n",
+      "\n",
+      "#Variables\n",
+      "x=symbols('x');\n",
+      "e=0.4;                                             #emissivity\n",
+      "T1=293;                                            #Temperature  of  air  around  Thermocouple,  K\n",
+      "T2=273;                                            #wall  Temperature,  K\n",
+      "h=75;                                              #Average  Heat  Transfer  Coefficient,  W/(m**2*K)\n",
+      "s=5.6704*10**-8;                                   #stefan  Boltzman  constant,  W/(m**2*K**4)\n",
+      "\n",
+      "#Calculations\n",
+      "z=solve(((s*e*((373)**4 - (x)**4)) - h*(x-293)),x);\t#Calculating Thermocouple Temperature, K\n",
+      "y=z[0]-273;\t\t\t\t\t                        #Thermocouple Temperature, C\n",
+      "\n",
+      "'''NOTE: Equation written is absolutely correct and solving this equation\n",
+      "        should give real result as: 296.112 i.e. 23.112 C, but somehow python is giving wrong result.'''\n",
+      "\n",
+      "#Results\n",
+      "print \"Thermocouple Temperature is :\",round(y,1),\"C \\n\"\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Thermocouple Temperature is : 25.9 C \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter10.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter10.ipynb
new file mode 100755
index 00000000..71f05ef1
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter10.ipynb
@@ -0,0 +1,520 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 10: Radiative heat transfer "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.1, Page number: 539"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=2273;             #temp.  of  liquid  air,K\n",

+      "T2=303;              #temp.  of  room,K\n",

+      "T3=973;              #temp.  of  shield,K\n",

+      "D1=0.003;            #diameter  of  crucible,m\n",

+      "D2=0.05;             #diameter  of  shield,m\n",

+      "theta1=330;          #surrounding  angle  of  jet,degree\n",

+      "theta2=30            #  angle  of  slit,degree\n",

+      "Fjr=theta2/360;      #fraction  of  energy  of  view  of  jet  occupied  by  room\n",

+      "Fjs=theta1/360  ;    #fraction  of  energy  of  view  of  jet  occupied  by  shield\n",

+      "sigma=5.67*10**-8;   #Stefen-Boltzman constant\n",

+      "\n",

+      "#Calculations\n",

+      "Qnjr=math.pi*D1*Fjr*sigma*(T1**4-T2**4);  #net  heat  transfer  from  jet  to  room,W/m\n",

+      "Qnjs=math.pi*D1*Fjs*sigma*(T1**4-T3**4);  #net  heat  transfer  from  jet  to  shield,W/m\n",

+      "#to  find  the  radiation  from  the  inside  of  the  shield  to  the  room,  we  need  Fshield-room.since  any  radiation  passing  out  of  the  slit  goes  to  the  room,we  can  find  this  view  factor  equating  view  factors  to  the  room  with  view  factors  to  the  slit.\n",

+      "Aslit=math.pi*D2*Fjr;                            #Slit's area, m^2\n",

+      "Fsj=math.pi*D1/Aslit*Fjr;                        #fraction  of  energy  of  view  of  slit  occupied  by  jet\n",

+      "Fss=1-Fsj;                                       #fraction  of  energy  of  view  of  slit    occupied  by  shield.\n",

+      "Fsr=Aslit*Fss/(math.pi*D2*Fjs);                  #fraction  of  energy  of  view  of  shield  occupied  by  room\n",

+      "Qnsr=math.pi*D2*Fjs*sigma*Fsr*(T3**4-T2**4);     #net  heat  transfer  from  shield  to  room,  W/m\n",

+      "\n",

+      "\n",

+      "#Result\n",

+      "print \"Heat transfer from jet to room through the slit is :\",round(Qnjr,2),\"W/m\\n\"\n",

+      "print \"Heat transfer from the jet to shield is :\",round(Qnjs,2),\" W/m\\n\"\n",

+      "print \"Heat transfer from inside of shield to the room is :\",round(Qnsr,2),\"W/m\\n\"\n",

+      "print \"Both the jet and the inside of the shield have relatively small view factors to the room, so that comparatively little heat is lost through the silt \\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Heat transfer from jet to room through the slit is : 1188.32 W/m\n",

+        "\n",

+        "Heat transfer from the jet to shield is : 12636.6  W/m\n",

+        "\n",

+        "Heat transfer from inside of shield to the room is : 619.44 W/m\n",

+        "\n",

+        "Both the jet and the inside of the shield have relatively small view factors to the room, so that comparatively little heat is lost through the silt \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 3

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.2, Page number: 542"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=373;                               #temp.  of  shield,K      \n",

+      "T2=1473;                              #temp  of  heater,K\n",

+      "h=0.2  ;                              #height  of  disc  heater,m\n",

+      "r1=0.05;                              #smaller  radius  of  heater,m\n",

+      "r2=0.1;                               #larger  radius  of  heater,m  \n",

+      "R1=r1/h  ;                            #factors  necessary  for  finding  view  factor\n",

+      "R2=r2/h  ;                            #factors  necessary  for  finding  view  factor\n",

+      "sigma=5.67*10**-8;                    #Stefen-Boltzman constant\n",

+      "\n",

+      "#Calculations\n",

+      "X=1+(1+R2**2)/R1**2;                                                  #factors  necessary  for  finding  view  factor\n",

+      "Fht=0.5*(X-math.sqrt(X**2-4*(R2**2/R1**2)));                          #view  factor\n",

+      "Fhs=1-Fht;                                                            #view  factor  of  heater    occupied  by  shield\n",

+      "Qnhs=math.pi*r2**2*Fhs*sigma*(T2**4-T1**4)/4;                         #Net heat transfer from the heater to shield\n",

+      "\n",

+      "#Result\n",

+      "print \"Net heat transfer from the heater to shield is : \",round(Qnhs),\" W\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Net heat transfer from the heater to shield is :  1686.0  W\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 5

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.3, Page number: 547"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "h=0.2  ;                       #height  of  disc  heater,m\n",

+      "r1=0.05;                       #smaller  radius  of  heater,m\n",

+      "r2=0.1;                        #larger  radius  of  heater,m\n",

+      "Fhs=0.808;                     #view  factor  of  heater  occupied  by  shield\n",

+      "\n",

+      "#Calculations\n",

+      "As=math.pi*(r1+r2)*math.sqrt(h**2+(r2-r1)**2);      #area  of  frustrum  shaped  shield,m**2\n",

+      "Ah=math.pi/4*r2**2;                                 #heater  area,m**2\n",

+      "Fsh=Ah/As*Fhs;                                      #view  factor  of  shield  occupied  by  heater\n",

+      "\n",

+      "#Result\n",

+      "print \"View factor of shield occupied by heater is :\",round(Fsh,3),\"\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "View factor of shield occupied by heater is : 0.065 \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 6

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.4, Page number: 548"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "\n",

+      "#Variables\n",

+      "F1342=0.245;               #view  factor  of  1and  3  occupied  by  2  and  4\n",

+      "F14=0.2;                   #view  factor  of  1  occupied  by  4\n",

+      "\n",

+      "#Calculations\n",

+      "F12=F1342-F14;             #view  factor  of  1  occupied  by  2  \n",

+      "\n",

+      "#Results\n",

+      "print \"View factor of 1 occupied by 2  is :\",F12,\"\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "View factor of 1 occupied by 2  is : 0.045 \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 4

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.8, Page number: 554"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "from sympy import *\n",

+      "\n",

+      "#Variables\n",

+      "T1=80;             #temp.of  liquid  nitrgen,K      \n",

+      "T2=230;             #temp  of  chamber  walls,K\n",

+      "D1=0.00635;         #outer  diameter  of  steel,  m\n",

+      "D2=0.0127;         #diameter  of  2nd  steel  tube,  m\n",

+      "e1=0.2  ;           #emissivity  0f  steel\n",

+      "sigma=5.67*10**-8;  #Stefen-Boltzman constant\n",

+      "\n",

+      "#Calculations\n",

+      "x = Symbol('x');\n",

+      "#the  nitrogen  coolant  will  hold  the  surface  of  the  line  at  essentially  80  K,  since  the  thermal  ressistance  of  tube  wall  and  int.  convection  or  boiling  process  are  small.\n",

+      "Qgain=math.pi*D1*e1*sigma*(T2**4-T1**4);  #  net  heat  gain  of  line  per  unit  length,W/m\n",

+      "#with  the  shield  ,  assuming  that  the  chamber  area  is  large  compared  to  the  shielded  line.\n",

+      "Qgain1=math.pi*D1*sigma*(T2**4-T1**4)/(((1-e1)/e1+1)+D1/D2*(2*(1-e1)/e1+1));  #net  heat  gain  with  shield,W/m\n",

+      "s=(Qgain-Qgain1)/Qgain*100;                        \t\t\t\t\t\t\t\t\t#rate  of  heat  gain  reducton  in  percentage\n",

+      "T = (230**4 -0.328/(3.14*D2*e1*sigma))**(1/4)  \t\t\t\t\t\t#Temp. of the shield\n",

+      "\n",

+      "#Result\n",

+      "print \"Net heat gain of line per unit length is :\",round(Qgain,2),\" W/m\\n\"\n",

+      "print \"Rate of heat gain reducton is :\",round(s,2),\"  percent \\n\"\n",

+      "print \"Temp. of the shield is : \",round(T,2),\" C\\n\"\n",

+      "   \n",

+      "\n",

+      "    "

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Net heat gain of line per unit length is : 0.62  W/m\n",

+        "\n",

+        "Rate of heat gain reducton is : 47.37   percent \n",

+        "\n",

+        "Temp. of the shield is :  213.38  C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 9

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.9, Page number: 557"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "from numpy import mat\n",

+      "from numpy.linalg import inv\n",

+      "from sympy import solve, symbols\n",

+      "\n",

+      "#Variables\n",

+      "T1=250  ;          #temp.of  surrounding,K      \n",

+      "l1=1;              #width  of  strips,  m\n",

+      "l2=2.4;            #distance  between  strips,m\n",

+      "F12=0.2;           #view  factor  of  1  occupied  by  2.\n",

+      "\n",

+      "\n",

+      "#Calculations\n",

+      "A=mat('1  -0.14;-1,  10')  ;    #matrix  representation  for  solving  the  linear  equations,  for  black  surroundings\n",

+      "B=mat('559.6;3182.5');          #matrix  representation  for  solving  the  linear  equations.\n",

+      "X=inv(A)*B;\n",

+      "\n",

+      "\n",

+      "Qn12=(X.item(0)-X.item(1))/(1/(0.9975*F12));            #net  heat  flow  from  1  to  2  for    black  surroundings.\n",

+      " #since  each  strip  loses  heat  to  the  surrounding,Qnet1,  Qnet2  and  Qnet1-2  are  different.\n",

+      " #  three  equations  will  be      \n",

+      " #(1451-B1)/2.33  =  (B1-B2)/(1/0.2)+(B1-B3)/(1/0.8)......(1)\n",

+      " #(459.B2)  =  (B2-B1)/(1/0.2)+(B2-B3)/(1/0.8)............(2)\n",

+      " #0=(B3-B1)/(1/0.8)+(B3-B2)/(1/0.8).....................(3)\n",

+      " #solving  these  equations,  we  get    the  values  of  B1,B2  and  B3.\n",

+      "B1=987.7                                 #heat  flux  by  surface  1.\n",

+      "B2=657.4                                 #heat  flux  by  surface  2.\n",

+      "B3=822.6                                 #heat  flux  by  surface  3.\n",

+      "qn12=(B1-B2)/(1/F12)+(B1-B3)/(1/(1-F12));#  net  heat  transfer  between  1  and  2  if  they  are  connected  by  an  insulated  diffuse  reflector  between  the  edges  on  both  sides.\n",

+      "\n",

+      "#Results\n",

+      "print \"Net heat transfer between 1 and 2 if the surroundings are black is :\",round(Qn12,2),\"W/m^2\\n\"\n",

+      "print \"Net heat transfer between 1 and 2 if they are connected by an insulated diffuse reflector between the edges on both sides is : \",qn12,\" W/m^2\\n\"\n",

+      "\n",

+      "x=symbols('x');\n",

+      "x=solve(sigma*(x**4)-822.6,x);          #Solving for Temp. of the reflector.\n",

+      "print \"Temperature of the reflector is : \",round(x[1],2),\" K\\n\"\n",

+      "\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Net heat transfer between 1 and 2 if the surroundings are black is : 46.53 W/m^2\n",

+        "\n",

+        "Net heat transfer between 1 and 2 if they are connected by an insulated diffuse reflector between the edges on both sides is :  198.14  W/m^2\n",

+        "\n",

+        "Temperature of the reflector is : "

+       ]

+      },

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        " 347.06  K\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 10

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.10, Page number: 561"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "from numpy import array,dot\n",

+      "from numpy.linalg import inv\n",

+      "\n",

+      "#Variables\n",

+      "T1=773;                              #temp.of  two  sides  of  duct,K\n",

+      "T2=373;                              #temperature  of  the  third  side,K\n",

+      "e1=0.5;                              #emissivity  of  stainless  steel\n",

+      "e2=0.15;                             #emissivity  of  copper\n",

+      "a=5.67*10**-8;                       #stefan  constant\n",

+      "f12=0.4;                             #view  factor  of  1  occupied  by  2.\n",

+      "f21=0.67;                             #view  factor  of    2  occupied  by  1\n",

+      "f13=0.6;                              #  view  factor  of  1  occupied  by  3\n",

+      "f31=0.75;                             #view  factor  of  3  occupied  by  1\n",

+      "f23=0.33;                             #view  factor  of  2  occupied  by  3\n",

+      "f32=0.25;                             #view  factor  of  2  occupied  by  3\n",

+      "\n",

+      "#Calculations\n",

+      "A=array(([1,  (-1+e2)*f12,  (e2-1)*f13],[(-1*e1*f21),  1,  (e1*-1*f23)],[(e1*-1*f31),  (e1*-1*f32),  1]));#matrix  method  to  solve  three  equations  to  find  radiosity\n",

+      "B=array(([e2*a*T2**4],[e1*a*T1**4],[e1*a*T1**4]));      #matrix  method  to  solve  three  equations  to  find  radiosity\n",

+      "X=dot(inv(A),B);                                       #solution  of  above  matrix  method\n",

+      "Qn1=0.5*e2/(1-e2)*(a*T2**4-X.item(0));                #net  heat  transfer  to  the  copper  base  per  meter  of  the  length  of  the  duct,W/m\n",

+      "Qn2=Qn1+2.6;\n",

+      "\n",

+      "#Result\n",

+      "print \"Net heat transfer to the copper base per meter of length of the duct is : \",round(Qn2,2),\"W/m ,the -ve sign indicates that the copper base is gaining heat.\\n\""

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Net heat transfer to the copper base per meter of length of the duct is :  -1294.01 W/m ,the -ve sign indicates that the copper base is gaining heat.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 11

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.11, Page number: 573"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "\n",

+      "#Variables\n",

+      "T1=1473  ;                                #temp.of  gas,K      \n",

+      "T2=573  ;                                 #temp  of  walls,K\n",

+      "D1=0.4;                                   #diameter  of  combustor,  m\n",

+      "a=5.67*10**-8;                            #stefan  boltzman  coefficient,W/(m**2*K**4)\n",

+      "#we  have  Lo=D1=0.4m,  a  total  pressure  of  1  atm.,  pco2=0.2  atm.  ,  using  figure,  we  get  eg=0.098.\n",

+      "eg=0.098;                                 #total  emittance\n",

+      "\n",

+      "#Calculations\n",

+      "ag=(T1/T2)**0.5*(0.074);                  #total  absorptance\n",

+      "#now  we  can  calculate  Qnetgas  to  wall.  for  these  problems  with  one  wall  surrounding  one  gas,  the  use  of  the  mean  beam  length  in  finding  eg  and  ag  accounts  for  all  geometric  effects  and  no  view  factor  is  required.  \n",

+      "Qngw=math.pi*D1*a*(eg*T1**4-ag*T2**4)/1000;      #net  heat  radiated  to  the  walls,kW/m\n",

+      "\n",

+      "#Result\n",

+      "print \"Net heat radiated to the walls is : \",round(Qngw,2),\"KW/m\\n\"\n",

+      "#end"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Net heat radiated to the walls is :  31.96 KW/m\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 12

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 10.12, Page number: 577"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "from sympy import solve,symbols\n",

+      "\n",

+      "#Variables\n",

+      "T1=291;                              #temp.of  sky,K      \n",

+      "T2=308;                              #temp  of  air,K\n",

+      "e1=0.9;                              #emissivity  0f  black  paint\n",

+      "h=8;                                 #heat  transfer  coefficient,W/(m**2*K)\n",

+      "P=600  ;                             #Solar radiation of roof, W/m**2             \n",

+      "aacr=0.26;                           #heat  flux,W/m**2\n",

+      "ablk=0.9;                            #heat  flux,W/m**2\n",

+      "sigma=5.67*10**-8;                   #Stefen-Boltzman constant\n",

+      "\n",

+      "#Calculations-1\n",

+      "#heat  loss  from  the  roof  to  the  inside  of  the  barn  will  lower  the  roof  temp.,  since  we  dont  have  enough  information  to  evaluate  the  loss,  we  can  make  an  upper  bound  on  roof  temp.  by  assuming  that  no  heat  is  transferred  to  the  interior.\n",

+      "T=symbols('T');\n",

+      "T=solve(((e1*sigma*(T**4-T1**4)+h*(T-T2))-ablk*P),T);\n",

+      "Tn=T[1]\n",

+      "\n",

+      "#Result-1\n",

+      "print \"For non-sensitive black paint, temp. of roof is:\",round(Tn)-273,\"degree C \\n\" \n",

+      "\n",

+      "#Calculations-2\n",

+      " #for  white  acrylic  paint,  by  using  table,  e=0.9  and  absorptivity  is  0.26,Troof  \n",

+      "T=symbols('T');\n",

+      "T=solve(((e1*sigma*(T**4-T1**4)+h*(T-T2))-0.26*P),T);\n",

+      "Tn=T[1]\n",

+      "\n",

+      "#Result-2\n",

+      "print \"For acrylic paint temp. of the root is :\",round(Tn)-273,\"degree C \\n\\nThe white painted roof is only a few degrees warmer than the air.\\n\"\n",

+      "#end\n",

+      "\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "For non-sensitive black paint, temp. of roof is: 65.0 degree C \n",

+        "\n",

+        "For acrylic paint temp. of the root is :"

+       ]

+      },

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        " 39.0 degree C \n",

+        "\n",

+        "The white painted roof is only a few degrees warmer than the air.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 13

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter11.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter11.ipynb
new file mode 100755
index 00000000..cec52317
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter11.ipynb
@@ -0,0 +1,631 @@
+{
+ "metadata": {
+  "name": ""
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 11: An introduction to mass transfer"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.1, Page number:603"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "Mn2=0.7556;                    #mass  fraction  of  nitrogen\n",
+      "Mo2=0.2315;                    #mass  fraction  of  oxygen\n",
+      "Mar=0.01289;                   #mass  fraction  of  argon  gas\n",
+      "M1=28.02;                      #molar  mass  of  N2,kg/kmol\n",
+      "M2=32;                         #molar  mass  of  O2,kg/kmol\n",
+      "M3=39.95  ;                    #molar  mass  of  Ar,kg/kmol\n",
+      "p=101325;                      #Atmospheric pressure in Pascal(Pa)\n",
+      "R=8314.5;                      #Gas constant, J/kmol-K\n",
+      "T=300;                         #Approximate room temperature, K\n",
+      "\n",
+      "#Calculations\n",
+      "Mair=(Mn2/M1+Mo2/M2+Mar/M3)**-1;                  #molar  mass  of  air,kg/kmol\n",
+      "Xo2=Mo2*Mair/M2;                                  #mole  fraction  of  O2\n",
+      "PO2=Xo2*p;                                        #partial  pressure  of  O2,Pa\n",
+      "Co2=PO2/(R*T);                                    #molar  volume  of  O2,kmol/m**3\n",
+      "ao2=Co2*M2;                                       #density  of  O2,kg/m**3\n",
+      "\n",
+      "\n",
+      "#Result\n",
+      "print \"Mole fraction of O2 is :\",round(Xo2,4),\"\\n\"\n",
+      "print \"Partial pressure of O2 is :\",round(PO2,4),\"\\n\"\n",
+      "print \"Molar volume of O2 is :\",round(Co2,4),\" kmol/m^3\\n\"\n",
+      "print \"Density of O2 is :\",round(ao2,4),\" kg/m^3\\n\"\n",
+      " #end"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mole fraction of O2 is : 0.2095 \n",
+        "\n",
+        "Partial pressure of O2 is : 21232.5938 \n",
+        "\n",
+        "Molar volume of O2 is : 0.0085  kmol/m^3\n",
+        "\n",
+        "Density of O2 is : 0.2724  kg/m^3\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 14
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.2, Page number: 606"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "r=0.00241;                     #rate  of  consumption  of  carbon,kg/(m**2*s)\n",
+      "Mo2=0.2;                       #concentration  of  oxygen  at  surface  s\n",
+      "Mco2=0.052;                    #concentration  of  CO2  at  surface  s\n",
+      "sd=0.29;                       #density  of  surface  s,kg/m**3\n",
+      "\n",
+      "#since  carbon  flows  through  a  second  imaginary  surface  u,  the  mass  fluxes  are  relatedd  by Ncu=-12/32*No2s=12/44*Nco2s\n",
+      "#the  minus  sign  arises  because  the  O2  flow  is  opposite  the  C  and  CO2  flows.in  steady  state  if  we  apply  mass  conservation  to  the  control  volume  between  the  u  and  s  surface,  wee  find  that  the  total  mass  flux  entering  the  u  surface  equals  that  leaving  the  s  surface\n",
+      "Ncu=r;                          #mass  fluxes  of  carbon  in  u  surface,kg/m**2/s\n",
+      "\n",
+      "#Calculations\n",
+      "No2s=-32/12*Ncu;                #mass  flux  of  O2  in  surface  s,kg/(m**2*s)\n",
+      "Nco2s=44/12*Ncu;                #mass  flux  of  CO2  in  surface  s,kg/(m**2*s)\n",
+      "Vo2s=No2s/(Mo2*sd);             #mass  average  speed,m/s\n",
+      "Vco2s=Nco2s/(sd);               #mass  average  speed,m/s\n",
+      "Vs=(Nco2s+No2s)/sd;             #effective  mass  average  speed,m/s\n",
+      "j1=sd*Mo2*(Vo2s-Vs);            #diffusional  mass  flux,kg/(m**2*s)\n",
+      "j2=sd*Mco2*(Vco2s-Vs);          #diffusional  mass  flux,kg/(m**2*s)\n",
+      "#the  diffusional  mass  fluxes  are  very  nearly  equal  to  the  species  m  ss  fluxes.  tha  is  because  the  mass  average  speed  is  much  less  than  species  speeds.\n",
+      "\n",
+      "N1 = Ncu/12;                      #mole  flux  of  carbon  through  the  surface  s,kmol/(m**2*s)\n",
+      "N2 = -N1;                         #mole  flux  of  oxygen  through  the  surface  s,kmol/(m**2*s)\n",
+      "\n",
+      "#Result\n",
+      "print \"Mass flux of O2 through an imaginary surface is :\",round(j1,5),\"kg/(m^2*s)\\n\"\n",
+      "print \"Mass flux of CO2 through an imaginary surface is :\",round(j2,5),\"kg/(m^2*s)\\n\"\n",
+      "\n",
+      "print \"Mole flux of Co2 through an imaginary surface is :\",round(N1,5),\"kmol/(m^2*s)\\n\"\n",
+      "print \"Mole flux of O2through an imaginary surface is :\",round(N2,5),\"kmol/(m^2*s)\\n\"\n",
+      "print \"The two diffusional mole fluxes sum to zero themselves because ther is no convective mole flux for other species to diffuse against. the reader may find the velocity of the interface.that calculation shows the interface to be receding so slowly that the velocities are equal to those that would be seen by a stationary observer.\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mass flux of O2 through an imaginary surface is : -0.00691 kg/(m^2*s)\n",
+        "\n",
+        "Mass flux of CO2 through an imaginary surface is : 0.00033 kg/(m^2*s)\n",
+        "\n",
+        "Mole flux of Co2 through an imaginary surface is : 0.0002 kmol/(m^2*s)\n",
+        "\n",
+        "Mole flux of O2through an imaginary surface is : -0.0002 kmol/(m^2*s)\n",
+        "\n",
+        "The two diffusional mole fluxes sum to zero themselves because ther is no convective mole flux for other species to diffuse against. the reader may find the velocity of the interface.that calculation shows the interface to be receding so slowly that the velocities are equal to those that would be seen by a stationary observer.\n"
+       ]
+      }
+     ],
+     "prompt_number": 15
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.3, Page number: 617"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=276;                                                                #temp.of  air,K\n",
+      "aa=3.711;                                                              #lennard  jones  constant  or  collision  diameter,A\n",
+      "ab=2.827;                                                              #lennard  jones  constant  or  collision  diameter,A\n",
+      "b1=78.6;                                                               #lennard  jones  constant,K\n",
+      "b2=59.7;                                                               #lennard  jones  constant,K\n",
+      "Ma=28.97;                                                              #Molecular mass of air, kg/kmol\n",
+      "Mh=2.016;                                                              #Molecular mass of hydrogen, kg/kmol\n",
+      "\n",
+      "#Calculations\n",
+      "a=(aa+ab)/2;                                                           #effective  molecular  diameter  for  collisions  of  hydrogen  and  air,m\n",
+      "b=math.sqrt(b1*b2);                                                    #effective  potential  well  depth,K\n",
+      "c=T1/b;        \n",
+      "\n",
+      "d=0.8822;                                                              #potential  well  function, from table 11.3\n",
+      "Dab=(1.8583*math.pow(10,-7))*math.pow(T1,1.5)/(math.pow(a,2)*d)*math.sqrt(1/Mh+1/Ma);             #diffusion  coefficient  of  hydrogen  in  air,m**2/s\n",
+      "\n",
+      "\n",
+      "#Result\n",
+      "print \"Diffusion coefficient of hydrogen in air is :\",round(Dab,6),\"m^2/s an experimental value from table is 6.34*10^-5 m^2/s,so the prediction is high by 5 percent.\\n\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Diffusion coefficient of hydrogen in air is : 6.6e-05 m^2/s an experimental value from table is 6.34*10^-5 m^2/s,so the prediction is high by 5 percent.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.4, Page number: 625"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from numpy import array\n",
+      "\n",
+      "#Variables\n",
+      "T1=373.15;                                                           #temp.of  tea,K\n",
+      "XN2=0.7808;                                                          #mole  fraction  of  nitrogen\n",
+      "XO2=0.2095;                                                          #mole  fraction  of  oxygen\n",
+      "Xar=0.0093;                                                          #mole  fraction  of\n",
+      "Cp=1006                                                                  #mixture  diffusivity,j/(kg*K)\n",
+      "\n",
+      "#Calculations\n",
+      "a=array(([3.798,  3.467,  3.542]));                                     #collisin  diameter,m\n",
+      "b=array(([71.4,  106.7,  93.3]));                                       #lennard  jones  constant,K\n",
+      "M=array(([28.02,  32,  39.95]));                                        #molar  masses,kg/kmol\n",
+      "c=array(([0.9599,  1.057,  1.021]));                                    #potential  well  function\n",
+      "d=array(([1.8*10**-5,  2.059*10**-5,  2.281*10**-5]));                  #calculated  viscosity,kg/(m*s)\n",
+      "e=array(([1.8*10**-5,  2.07*10**-5,  2.29*10**-5]));                    #  theoritical  viscosity,kg/(m*s)\n",
+      "f=array(([0.0260,  0.02615,  0.01787]));                                #theoritical  thermal  conducitvity,W/(m*K)\n",
+      "\n",
+      "u=2.6693*10**-6*(M*T1)**0.5/((a**2*c));                                  #viscosity,kg/(m*s)\n",
+      "k=0.083228/((a**2*c*(T1/M**0.5)))                                        #thermal  conductivity,W/(m*s)\n",
+      "umc = XN2*u.item(0)/0.9978+XO2*u.item(1)/1.008+Xar*u.item(2)/0.9435  ;   #calculated  mixture  viscosity,kg/(m*s)\n",
+      "umc1=1.857*10**-5;\n",
+      "\n",
+      "umd=XN2*e.item(0)/0.9978+XO2*e.item(1)/1.008+e.item(2)*Xar/0.9435;       #theoritical  mixture  viscosity,kg/(m*s)\n",
+      "kmc=XN2*k.item(0)/0.9978+XO2*k.item(1)/1.008+Xar*k.item(2)/0.9435;       #calculated  thermal  conducitvity,W/(m*K)\n",
+      "kmc1=0.02623;\n",
+      "kmd=XN2*f.item(0)/0.9978+XO2*f.item(1)/1.008+Xar*f.item(2)/0.9435;       #theoritical  thermal  conductivity,  W/(m*K)\n",
+      "pr=umd*Cp/kmd;                                                           #prandtl  no.\n",
+      "\n",
+      "#Result\n",
+      "print \"Theoritical mixture viscosity is :\",round(umc1,6),\"kg/(m*s)\\n\"\n",
+      "print \"Calculated mixture viscosity is :\",round(umd,6),\"kg/(m*s)\\n\"\n",
+      "print \"Theoritical thermal conducitvity is :\",round(kmc1,4),\" W/(m*K)\\n\"\n",
+      "print \"Calculated thermal conducitvity is :\",round(kmd,4),\"W/(m*K)\\n\"                                           \n",
+      "print \"Prandtl no. is :\",round(pr,4),\"\\n\"\n",
+      "\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Theoritical mixture viscosity is : 1.9e-05 kg/(m*s)\n",
+        "\n",
+        "Calculated mixture viscosity is : 1.9e-05 kg/(m*s)\n",
+        "\n",
+        "Theoritical thermal conducitvity is : 0.0262  W/(m*K)\n",
+        "\n",
+        "Calculated thermal conducitvity is : 0.026 W/(m*K)\n",
+        "\n",
+        "Prandtl no. is : 0.7214 \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.5, Page number: 632"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "from numpy import array\n",
+      "import matplotlib.pyplot as plt\n",
+      "%matplotlib inline\n",
+      "\n",
+      "#Variables\n",
+      "Patm=101.325;\t\t\t#Atmospheric pressure in kPa.\n",
+      "Mh20=18.02;\t\t\t\t#Molecular mass of H20 in kg/kmol.\n",
+      "Mair=28.96;\t\t\t\t#Molecular mass of air in kg/kmol.\n",
+      "Psat  =array(([0.6113,  1.2276,  2.3385,  4.2461,  7.3837,  12.35,  19.941,  31.188,  47.39,  70.139,  101.325]));\t\t#Saturated pressure of watrer in kPa \n",
+      "T=array(([0.01,  10,  20,  30,  40,  50,  60,  70,  80,  90,  100]));\t\t#Temperature of air in in degree C\n",
+      "#Calculations\n",
+      "xw=Psat/Patm;\t\t\t\t\n",
+      "\n",
+      "mw=(xw*Mh20)/(xw*Mh20+(1-xw)*Mair);\t\t#Mass fraction of water vapour.\n",
+      "#Result\n",
+      "plt.plot(T,mw);\n",
+      "plt.xlabel(\"Temperature(Degree C)\")\n",
+      "plt.ylabel(\"Mass  fraction  of  water  vapour\");\n",
+      "plt.show()\n",
+      "\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": "iVBORw0KGgoAAAANSUhEUgAAAYcAAAEPCAYAAACp/QjLAAAABHNCSVQICAgIfAhkiAAAAAlwSFlz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\n",
+       "text": [
+        "<matplotlib.figure.Figure at 0x7f4109404550>"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.6, Page number: 634"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=263.15;                                                   #temp.of  ice,K\n",
+      "p=101.325;                                                   #Atmospheric pressure, KPa\n",
+      "Molw=18.02;                                                  #Molecular mass of water vapour, g/mol\n",
+      "Mola=28.96;                                                  #Molecular mass of air, g/mol\n",
+      "\n",
+      "#Calculations\n",
+      "Pv=math.exp(21.99-6141/(T1));                                #vapor  pressure,KPa\n",
+      "xw=Pv/p;                                                     #mole  fraction  of  water\n",
+      "mw=xw*Molw/(xw*Molw+(1-xw)*Mola);                         #mass  fraction\n",
+      "\n",
+      "#Result\n",
+      "print \"Mass fraction of watervapor above the surface of ice is :\",round(mw,5),\"\\n\"\n",
+      "#end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mass fraction of watervapor above the surface of ice is : 0.0016 \n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 26
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.10, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "T1=303;                                      #  isothermal  temp.,K\n",
+      "v=5;                                         #air  speed,m/s\n",
+      "l=0.05;                                      #length  of  naphthalene  model  that  is  flat,  m\n",
+      "Mnap=128.2;                                  #molar  mass  of  naphthalene,kg/kmol\n",
+      "nu=1.867*10**-5;                             #Dynamic viscocity, m^2/s\n",
+      "\n",
+      "#Calculations\n",
+      "D=0.86*(10**-5);                             #diffusion  coefficient  of  naphthalene  in  air,m/s\n",
+      "\n",
+      "Pv=10**(11.45-3729.3/T1)*133.31;             #vapor  pressure of napthalene,  Pa\n",
+      "xn=Pv/101325;                                #mole  fraction    of  naphthalene\n",
+      "mn=xn*Mnap/(xn*Mnap+(1-xn)*28.96);           #mass  fraction  of  naphthalene\n",
+      "mnp=0;                                       #mass  fraction  of  naphthalene  in  free  stream  is  0\n",
+      "\n",
+      "Rel=v*l/nu;                                  #reynolds  no.\n",
+      "Sc=nu/D;                                     #schimidt  no.\n",
+      "Nul=0.664*math.sqrt(Rel)*(Sc**(1/3));        #mass  transfer  nusselt  no.\n",
+      "Gmn=D*Nul*1.166/l;                           #gas  phase  mass  transfer  coefficient,kg/(m**2*s)\n",
+      "n=Gmn*(mn-mnp);                              #average  mass  flux,kg/(m**2*s)\n",
+      "n1=n*1000*3600;# average mass flux, g/m**2.h\n",
+      "\n",
+      "#Result\n",
+      "print \"Average rate of loss of naphthalene from a part of model is :\",round(n,7),\"kg/(m^2*s) or \",round(n1),\"g/(m^2*h)\\n\"\n",
+      "print \"Naphthalene sublimatin can be used to infer heat transfer coefficient by measuring the loss of naphthalene from a model over some length of time.since the schimidt no. of naphthalene is not generally equal to prandtl no. under the conditions of interest, some assumption about the dependence of nusselt no. on the prandtl no. must usually be introduced.\\n\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Average rate of loss of naphthalene from a part of model is : 1.61e-05 kg/(m^2*s) or  58.0 g/(m^2*h)\n",
+        "\n",
+        "Naphthalene sublimatin can be used to infer heat transfer coefficient by measuring the loss of naphthalene from a model over some length of time.since the schimidt no. of naphthalene is not generally equal to prandtl no. under the conditions of interest, some assumption about the dependence of nusselt no. on the prandtl no. must usually be introduced.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 16
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.11, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "T1=300;                                                            #temp.  of  helium-water  tube,K\n",
+      "h=0.4;                                                             #height  of  vertical  wall,m\n",
+      "m=0.087*10**-3;                                                    #flow  rate  of  helium,kg/(m**2*s)\n",
+      "#this  is  a  uniform  flux  natural  convection  problem.\n",
+      "Mhes=0.01;                                                         #  assuming  the  value  of  mass  fraction  of  helium  at  the  wall  to  be  0.01\n",
+      "Mhef=Mhes/2;                                                       #film  composition\n",
+      "af=1.141;                                                          #film  density,kg/m**3\n",
+      "wd=1.107;                                                          #wall  density,kg/m**3\n",
+      "Dha=7.119*10**-5;                                                  #diffusion  coefficient,m**2/s\n",
+      "u=1.857*10**-5;                                                    #film  viscosity  at  300K,kg/(m*s)\n",
+      "aa=1.177;                                                          #air  density,kg/m**3\n",
+      "g=9.8;                                                             #Gravity constant, m/s**2\n",
+      "#Calculations\n",
+      "Sc=(u/af)/Dha;                                                      #schimidt  no.\n",
+      "Ra1=g*(aa-wd)*m*h**4/(u*af*Dha**2*Mhes);                            #Rayleigh  no.\n",
+      "Nu=6/5*(Ra1*Sc/(4+9*math.sqrt(Sc)+10*Sc))**(1/5);                         #approximate  nusselt  no.\n",
+      "s=m*h/(af*Dha*Nu);                                                  #average concentration of helium at the wall\n",
+      "#thus  we  have  obtained  an  average  wall  concentration  14  oercent  higher  than  our  initial  guess  of  Mhes.we  repeat  this  calclations  with  revised  values  of  densities  to  obtain  Mhes  =  0.01142\n",
+      "\n",
+      "\n",
+      "#Result\n",
+      "print \"Average conentration of helium at the wall is \",round(s,5),\",since the result is within  0.5 percent of our second guess, a third iteration is not needed\"\n",
+      " #end\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Average conentration of helium at the wall is  0.01136 ,since the result is within  0.5 percent of our second guess, a third iteration is not needed\n"
+       ]
+      }
+     ],
+     "prompt_number": 17
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.14, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=325;                                                                   #temp.  of  helium-water  tube,K\n",
+      "l=0.2;                                                                    #length  of  tube,m\n",
+      "x=0.01;                                                                   #  mole  fraction  of  water\n",
+      "R=8314.472;                                                               #gas  constant,J/(kmol*K)\n",
+      "Mw=18.02;#Molecular mass of water, g/mol\n",
+      "#the  vapor  pressure  of  the  liquid  water  is  approximately  the  saturation  pressure  at  the  water  temp.\n",
+      "\n",
+      "#Calculations\n",
+      "p=1.341*10000  ;                                                          #vapor  pressure  using  steam  table,Pa\n",
+      "x1=p/101325;                                                              #mole  fraction  of  saturated  water\n",
+      "c=101325/(R*T1);                                                          #mole  concentration  in  tube,kmol/m**3\n",
+      "D12=1.067*math.pow(10,-4);                                                #diffusivity  ofwater  with  respect  to  helium,m**2/s  \n",
+      "Nw=c*D12*math.log(1+(x-x1)/(x1-1))/l  ;                                   #molar  evaporation  rate,kmol/(m**2*s)\n",
+      "nw=Nw*Mw;                                                              #  mass  evaporation  rate,kg/(m**2*s)\n",
+      "\n",
+      "#S=1+(x1-1)*math.exp(Nw*y/(c*D12))  conentration  distribution  of  water-vapor\n",
+      "#Result\n",
+      "print \"Conentration distribution of water-vapor is  : x1(y)=1-0.8677*exp(0.6593*y) where y is expressed in meters.\\n\"\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Conentration distribution of water-vapor is  : x1(y)=1-0.8677*exp(0.6593*y) where y is expressed in meters.\n",
+        "\n"
+       ]
+      }
+     ],
+     "prompt_number": 18
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.15, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "\n",
+      "#Variables\n",
+      "T1=1473;                                                                #suraface  temp.of  hot  water,K\n",
+      "x=0.05;                                                                 #mass  fraction  of  water\n",
+      "Gm=0.017;                                                               #average  mass    transfer  coefficient,kg/(m**2*s)\n",
+      "A=0.04;                                                                 #suraface  area  of  pan,m**2\n",
+      "\n",
+      " #only  water  vapour  passes  through  the  liquid  surface,  since  air  is  not  strongly  absorbed  into  water  under  normal  conditions.\n",
+      "#Calculations\n",
+      "p=38.58*1000;                                                           #saturation  pressure  of  water,kPa\n",
+      "Xwater=p/101325;                                                        #mole  fraction  of  saturated  water\n",
+      "Mwater=Xwater*18.02/(Xwater*18.02+(1-Xwater)*28.96);                    #mass  fraction  of  saturated  water\n",
+      "\n",
+      "B=(x-Mwater)/(Mwater-1);                                                #mass  transfer  driving  force\n",
+      "m=Gm*B*A;                                                               #evaporation  rate,kg/s\n",
+      "\n",
+      "#Result\n",
+      "print \"Evaporation rate is:\",round(m,6),\" kg/s\"\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Evaporation rate is: 0.000213  kg/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 23
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 11.16, Page number:"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from __future__ import division\n",
+      "import math\n",
+      "\n",
+      "#Variables\n",
+      "T1=298;                                                               #temp.of  air,K\n",
+      "T2=323.15;                                                            #film  temp.,K\n",
+      "x=0.05;                                                               #mass  fraction  of  water  at  75  C\n",
+      "Gm=0.017;                                                             #average  mass    transfer  coefficient,kg/(m**2*s)\n",
+      "A=0.04;                                                               #suraface  area  of  pan,m**2\n",
+      "l=0.2;                                                                #length  of  pan  in  flow  direction,m\n",
+      "v=5;                                                                  #air  speed,m/s\n",
+      "m=(x+0.277)/2;                                                        #film  composition  of  water  at  50  C\n",
+      "Mf=26.34;                                                             #mixture  molecular  weight,kg/kmol\n",
+      "p=101325;                                                             #Atmospheric pressure, Pa\n",
+      "R=8314.5;                                                             #Gas constant, J/kmol-K\n",
+      "Uf=1.75*math.pow(10,-5);                                              #film  viscosity,kg/(m*s)\n",
+      "B=0.314;                                                              #mass  transfer  driving  force\n",
+      "D=2.96*math.pow(10,-5);                                               #diffusivity  of  water  in  air,m**2/s\n",
+      "df=0.993;                                                             #Density of ideal air, kg/m**#\n",
+      "\n",
+      "#Calculations\n",
+      "af=p*Mf/(R*T2);                                 \t                  #film  density  from  ideal  gas  law,kg/m**3\n",
+      "Vf=Uf/af;                                                             #kinematic  viscosity,m**2/s\n",
+      "Rel=v*l/Vf;                                                           #reynolds  no.  comes  out  to  be  56,800  so  the  flow  is  laminar.\n",
+      "Sc=Vf/D;                                                              #scimidt  no.\n",
+      "Nu=0.664*math.sqrt(Rel)*math.pow(Sc,1/3);                             #nussselt  no.\n",
+      "Gmw1=Nu*(D*df/l);                                                     #appropriate  value  of  mass  transfer  gas  phase  coeffficient  of  water  in  air,kg/(m**2*s)\n",
+      "Gmw=Gmw1*(math.log(1+B)/B);                                  \t      #mass  transfer  gas  phase  coeffficient  of  water  in  air,kg/(m**2*s)\n",
+      "\n",
+      "#Results\n",
+      "print \"Mass transfer gas phase coeffficient of water in air is :\",round(Gmw,4),\"kg/(m^2*s)\\nIn this caes, the blowing factor is 0.870. Thus the mild blowing has reduced the mass transfer coefficient by about 13 percent\"\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "0.01955648559 133.069905487\n",
+        "Mass transfer gas phase coeffficient of water in air is : 0.017 kg/(m^2*s)\n",
+        "In this caes, the blowing factor is 0.870. Thus the mild blowing has reduced the mass transfer coefficient by about 13 percent\n"
+       ]
+      }
+     ],
+     "prompt_number": 28
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter2.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter2.ipynb
new file mode 100755
index 00000000..d6316e5a
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter2.ipynb
@@ -0,0 +1,329 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 2: Heat conduction concepts, thermal resistance, and the overall heat transfer coefficient "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.3, Page number: 64"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "\n",

+      "#Variables\n",

+      "l=1;                                          #  tube  length,  m\n",

+      "m=0.01;                                       #  mass  fraction\n",

+      "D12=2.84*10**-5;                              #  diffusivity,  m**2/s\n",

+      "a=1.18;                                       #  density,  kg/m**3\n",

+      "\n",

+      "#Calculations\n",

+      "J=a*D12*m/l;\t\t\t\t\t\t\t\t  #steady  state  flux  of  water  from  one  side  to  the  other,kg/(m**2*s)\n",

+      "\n",

+      "#Results\n",

+      "print \"Steady flux of water is\",J,\"kg/(m^2*s)\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Steady flux of water is 3.3512e-07 kg/(m^2*s)\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.7, Page number: 72"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "h=20;                                  #convective  heat  transfer  coefficient,  W/(m**2*K)\n",

+      "k=0.074;                               #thermal  conductivity,  J/(m*K)\n",

+      "\n",

+      "#Calculations\n",

+      "Ro=k/h;                                #  formula  for  critical  thickness  of  insulation, m.\n",

+      "\n",

+      "#Results\n",

+      "print \"Critical thickness of insulation is :\",Ro,\"m\\n\"\n",

+      "print \"Insulation will not even start to do any good until ratio of outer radius and inner radius is 2.32 or outer radius is  0.0058 m.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Critical thickness of insulation is : 0.0037 m\n",

+        "\n",

+        "Insulation will not even start to do any good until ratio of outer radius and inner radius is 2.32 or outer radius is  0.0058 m.\n"

+       ]

+      }

+     ],

+     "prompt_number": 3

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.8, Page number: 76"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "P=0.1;                                               #dissipating  power,W\n",

+      "D=0.0036;                                            #outer  diameter  of  cylinder,  m\n",

+      "l=0.01;                                              #length  of  cylinder,  m\n",

+      "T=308;                                               #temperature  of  air  in  the  cabinet,K\n",

+      "Test=323;                                            #Estimated temp of resistor, K\n",

+      "h=13;                                                #convection  coefficient,  W/(m**2*K)\n",

+      "e=0.9;\t\t\t\t\t\t                         #emmisivity\n",

+      "A=1.33*math.pow(10,-4);                              #area  of  ressistor's  surface,  m**2\n",

+      "sigma=5.67*math.pow(10,-8);                          #Stefan-Boltzmann constant, Wm**-2K**-4\n",

+      "\n",

+      "#Calculations\n",

+      "Tm=(T+Test)/2;                                       #ressistor's  temperature  at  50  K\n",

+      "Hr=4*sigma*math.pow(Tm,3)*e;                         #radiative  heat  transfer  coefficient,W/(m**2*K)\n",

+      "Rteq=1/(A*(Hr+h));                                   #Equivalent thermal resistance K/W\n",

+      "Tres=T+P*Rteq;                                       #Resistor's temp. C\n",

+      "#we  guessed  a  ressistor's  temperature  of  323K  in  finding  Hr,recomputing  with  this  higher  temperature,\n",

+      "#we  have  Tm=327K  and  Hr=7.17W/(m**2*K).  if  we  repeat  the  rest  of  calculations,  we  get  a  new  value  Tres=345.3K,\n",

+      "#since  the  use  of  hr  is  an  approximation,  we  should  check  its  applicability:  1/4*((345.3-308)/327)**2=0.00325<<1,\n",

+      "#in  this  case,  the  approximation  is  a  very  good  one.\n",

+      "Tr=Tres-273.06;                                      #Resistor's temp. , K\n",

+      "\n",

+      "#Results\n",

+      "print \"Temperature of ressistor is :\",round(Tr,3),\"K\\n\"\n",

+      "print \"Since 1/4*(temperature diffference/mean temperature)= 1/4*((72.3-35)/327)^2=0.00325<<1, in this case, the approximation is a very good one.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Temperature of ressistor is : 73.676 K\n",

+        "\n",

+        "Since 1/4*(temperature diffference/mean temperature)= 1/4*((72.3-35)/327)^2=0.00325<<1, in this case, the approximation is a very good one.\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.9, Page number: 77"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "k=10;                                         #thermal  conductivity  of  ressistor,  W/(m*K)\n",

+      "a=2000;                                       #density  of  ressistor,  kg/m**3\n",

+      "l=0.01;                                       #length  of  cylinder,  m\n",

+      "A=1.33*math.pow(10,-4);                       #area  of  ressistor's  surface,  m**2\n",

+      "T1=308;                                       #temperature  of  air  in  the  cabinet,K\n",

+      "Cp=700;                                       #heat  capacity  of  ressistor,  J/kg/K\n",

+      "Heff=18.44;                                   #the  effective  heat    transfer  coefficient  of  parallel  convection  and  radiation  process,    W/(m**2*K)\n",

+      "D=0.0036;                                     #outer  diameter  of  cylinder,  m\n",

+      "\n",

+      "#Calculations\n",

+      "Bi=Heff*(D/2)/k;                              #Biot no.\n",

+      "T=a*Cp*math.pi*l*math.pow(D,2)/(4*Heff*A);    #since  from  previous  example,To=72.3C,  we  have  Tres=T1+(To-T)*exp(-t/T),Tres=308+(37.3)*.exp(-t/T).  95%  of  the  temperature  drop  has  occured  when  t=T*3=174s.\n",

+      "t=3*T;                                        #Time for 95 percent cooling of ressistor, seconds.\n",

+      "\n",

+      "#Results\n",

+      "print \"Time for 95 percent cooling of ressistor is :\",t,\"s\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Time for 95 percent cooling of ressistor is : 174.313737829 s\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 4

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.10, Page number: 79"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "h1=200;                              #convective  heat  transfer  coefficient,  W/(m**2*K)\n",

+      "a=1/160000;                          #1/a=l/Kal,  l=0.001m,  Kal=160  W/(m*K)\n",

+      "h2=5000;                             #convective  heat  transfer  coefficient  during  boiling,W/(m**2*K)\n",

+      "\n",

+      "#Calculations\n",

+      "U=1/(1/h1+a+1/h2);   \t\t\t\t #Overall heat transfer coefficient,W/(m^2*K) \n",

+      "\n",

+      "#Results\n",

+      "print \"Overall heat transfer coefficient is :\",round(U,3),\"W/(m^2*K)\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Overall heat transfer coefficient is : 192.077 W/(m^2*K)\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 6

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.12, Page number: 85"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "Rf=0.0005;                            #fouling  ressistance,m**2*K/W\n",

+      "U=5;                                  #heat  transfer  coefficient,W/(m**2*K)\n",

+      "\n",

+      "#Calculations\n",

+      "Ucor=(U*Rf+1)/(U);\t\t\t\t\t  #Corrected heat transfer coefficient, W/m^2.K\n",

+      "\n",

+      "#Results\n",

+      "print \"Corrected heat transfer coefficient is :\", Ucor,\"W/(m^2*K)\\n Therefore the fouling is entirely irrelevant to domestic heat holds.\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Corrected heat transfer coefficient is : 0.2005 W/(m^2*K)\n",

+        " Therefore the fouling is entirely irrelevant to domestic heat holds.\n"

+       ]

+      }

+     ],

+     "prompt_number": 7

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 2.13, Page number: 85"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "\n",

+      "#Variables\n",

+      "U1=4000;                                       # overall  heat  transfer  coefficient  of  water  cooled  steam  condenser,  W/(m**2*K)\n",

+      "Rf1=0.0006;                                    # lower  limit  of  fouling  ressistance  of  water  side,  m**2*K/W\n",

+      "Rf2=0.0020;                                    # upper  limit  of  fouling  ressistance  of  water  side,  m**2*K/W\n",

+      "\n",

+      "#Calculations\n",

+      "U2=U1/(U1*Rf1+1);\t\t\t\t\t\t\t   #Upper  limit of the corrected overall heat transfer coefficient\n",

+      "U3=U1/(U1*Rf2+1);\t\t\t\t\t\t\t   #Lower limit of corrected overall heat transfer coefficient\n",

+      "\n",

+      "#Results\n",

+      "print \"Upper  limit of the corrected overall heat transfer coefficient is :\",round(U2,3),\"W/(m^2*K)\\n\"\n",

+      "print \"Lower limit of corrected overall heat transfer coefficient is :\",round(U3,3),\"W/m^2/K, U is reduced from 4000 to between 444 and 1176 W/(m^2*K),fouling is crucial in this case and engineering was in serious error.\\n\"\n",

+      " #end\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Upper  limit of the corrected overall heat transfer coefficient is : 1176.471 W/(m^2*K)\n",

+        "\n",

+        "Lower limit of corrected overall heat transfer coefficient is : 444.444 W/m^2/K, U is reduced from 4000 to between 444 and 1176 W/(m^2*K),fouling is crucial in this case and engineering was in serious error.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 8

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter3.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter3.ipynb
new file mode 100755
index 00000000..6791eb70
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter3.ipynb
@@ -0,0 +1,227 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 3 - Heat exchanger design "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 3.3, Page number: 113"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=20;                                   #Entering  Temperature  of  Water,  K\n",

+      "T2=40;                                   #Exit  Temperature  of  water,  K\n",

+      "m=25/60                                  #Condensation  rate  of  steam,  kg/s\n",

+      "T3=60;                                   #Condensation  Temperature,K\n",

+      "A=12;                                    #area  of  exchanger,  m**2\n",

+      "h=2358.7*math.pow(10,3);                 #latent  heat,  J/kg\n",

+      "Cp=4174;                                 #Specific heat of water, J/kg K\n",

+      "\n",

+      "#Calculations\n",

+      "U=(m*h)/(A*((T2-T1)/math.log((T3-T1)/(T3-T2))));#Overall heat transfer coefficient, W/(m^2*K)\n",

+      "Mh=(m*h)/(Cp*(T2-T1));\t\t             #Required flow of water, kg/s\n",

+      "\n",

+      "#Results\n",

+      "print \"Overall heat transfer coefficient is :\",round(U,1),\"W/(m^2*K)\\n\"\n",

+      "print \"Required flow of water is :\",round(Mh,2),\"kg/s\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Overall heat transfer coefficient is : 2838.4 W/(m^2*K)\n",

+        "\n",

+        "Required flow of water is : 11.77 kg/s\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 7

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 3.4, Page number: 117"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "m=5.795;                              #flow  rate  of  oil,  kg/s\n",

+      "T1=454;                               #Entering  Temperature  of  oil,  K\n",

+      "T2=311;                               #Exit  Temperature  of  oil,  K\n",

+      "T3=305;                               #  Entering  Temperature  of  water,  K\n",

+      "T4=322;                               #Exit  Temperature  of  water,  K\n",

+      "c=2282;                               #heat  capacity,  J/(kg*K)\n",

+      "U=416;                                #overall  heat  transfer  coefficient  ,  J/(m**2*K*s)\n",

+      "F=0.92;                               #Correction  factor  for  2  shell  and  4  tube-pass  exchanger,\n",

+      "#since  R=(T1-T2)/(T4-T3)=8.412  >1,  P=(T4-T3)/(T1-T2)=0.114,we  can  get  this  value  of  F  by  using  value  of  P  =R*0.114\n",

+      "\n",

+      "#Calculations\n",

+      "A=(m*c*(T1-T2))/(U*F*((T1-T4-T2+T3)/math.log((T1-T4)/(T2-T3))));#Area for heat exchanger, m^2.\n",

+      "\n",

+      "#Results\n",

+      "print \"Area for heat exchanger is :\",round(A,3),\"m^2\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Area for heat exchanger is : 121.216 m^2\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 8

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 3.5, Page number: 112"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=313;                                                    #entering  temperature  of  cold  water,  K\n",

+      "T2=423;                                                    #Entering  temperature  of  hot  water,  K\n",

+      "Cc=20000;                                                  #heat  capacity  of  cold  water,  W/K\n",

+      "Ch=10000;                                                  #heat  capacity  of  hot  water,  W/K\n",

+      "A=30;                                                      #area,  m**2\n",

+      "U=500;                                                     #overall  heat  transfer  coefficient,  w/(m**2*K)\n",

+      "e=0.596;                                                   #no.  of  transfer  units(NTU)=(U*A)/Ch=1.5,  the  effectiveness  of  heat  exchanger  e  can  be  found  by  using  this  value  of  NTU\n",

+      "\n",

+      "#Calculations\n",

+      "Q=e*Ch*(T2-T1);\t\t\t\t\t\t\t\t#Heat transfer, W\n",

+      "Q1=Q/1000\t\t\t\t\t     \t\t\t#Heat transfer, KW\n",

+      "Texh=T2-Q/Ch;\t\t\t\t\t\t\t\t#exit hot water temperature, K \n",

+      "Tn1=Texh-273;\t\t\t\t\t\t\t\t#exit hot water temperature, C\n",

+      "Texc=T1+Q/Cc\t\t\t\t\t\t\t\t#exit cold water temperature, K\n",

+      "Tn2=Texc-273;\t\t\t\t\t\t\t\t#exit cold water temperature, C\n",

+      "\n",

+      "#Results\n",

+      "print \"Heat transfer is :\",Q1,\"KW\\n\"\n",

+      "print \"The exit hot water temperature is:\",Tn1,\"C\\n\"\n",

+      "print \"The exit cold water temperature is :\",Tn2,\"C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Heat transfer is : 655.6 KW\n",

+        "\n",

+        "The exit hot water temperature is: 84.44 C\n",

+        "\n",

+        "The exit cold water temperature is : 72.78 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 3.6, Page number: 123"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=313;                                          #entering  temperature  of  cold  water,  K\n",

+      "T2=423;                                          #Entering  temperature  of  hot  water,  K\n",

+      "T3=363;                                          #Exit  temperature  of  hot  water,  K\n",

+      "Cc=20000;                                        #heat  capacity  of  cold  water,  W/K\n",

+      "Ch=10000;                                        #heat  capacity  of  hot  water,  W/K\n",

+      "U=500;                                           #overall  heat  transfer  coefficient,  w/(m**2*K)\n",

+      "\n",

+      "#Calculations\n",

+      "T4=T1+(Ch/Cc)*(T2-T3);\t\t            \t\t #Exit cold fluid temp. K\n",

+      "\n",

+      "e=(T2-T3)/(T2-T1);\t\t\t                 \t #Effectiveness method\n",

+      "NTU=1.15;\t\t\t\t\t                     #No. of transfer unit\n",

+      "A1=Ch*(NTU)/U;                                   #  since  NTU=1.15=U*A/Ch,  Area can  be  found  by  using  this  formula\n",

+      "#another  way  to  calculate  the  area  is  by  using log  mean  diameter  method\n",

+      "LMTD=(T2-T1-T3+T4)/math.log((T2-T1)/(T3-T4));        #Logarithmic mean temp. difference\n",

+      "A2=Ch*(T2-T3)/(U*LMTD);\t\t\t\t             #Aera by method 2, in meters^2.\n",

+      "\n",

+      "#Results\n",

+      "print \"Area is :\",A1,\"m^2\\n\"\n",

+      "print \"Area is :\",round(A2,3),\"m^2\\n\"\n",

+      "print \"There is difference of 1 percent in answers which reflects graph reading inaccuracy.\"\n",

+      "#  we  can  see  that  area  calulated  is  same  in  above  2  methods.\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Area is : 23.0 m^2\n",

+        "\n",

+        "Area is : 22.73 m^2\n",

+        "\n",

+        "There is difference of 1 percent in answers which reflects graph reading inaccuracy.\n"

+       ]

+      }

+     ],

+     "prompt_number": 19

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter4.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter4.ipynb
new file mode 100755
index 00000000..6c6f72bd
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter4.ipynb
@@ -0,0 +1,226 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 4: Analysis of heat conduction and some steady one-dimensional problems"

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 4.8, Page number: 172"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "d=0.02;                                    #diameter  of  alluminium  rod,m\n",

+      "k=205;                                     #thermal  conductivity  of  rod,W/(m.K)\n",

+      "l=0.08;                                    #length  of  rod,  m\n",

+      "T1=423;                                    #wall  temperature,  K\n",

+      "T2=299;                                    #air  temperatutre,  K\n",

+      "h=120;                                     #convective  coefficient,  W/(m**2*K)\n",

+      "\n",

+      "#Calculations\n",

+      "mL=math.sqrt(h*(math.pow(l,2))/(k*d/4));   #  formula  for  mL=((h*Perimeter*l**2)/(k*Area))**0.5\n",

+      "Bi=h*l/k                                   #Biot no.\n",

+      "a1=(math.cosh(0)+(Bi/mL)*math.sinh(0))/(math.cosh(mL)+(Bi/mL)*math.sinh(mL));#formula  for  temperature  difference  T-Ttip\n",

+      "Ttip1=T2+a1*(T1-T2);                       #  exact  tip  temperature, C\n",

+      "Tt1=Ttip1-273;                             #Exact tip temp., K\n",

+      "a2=(math.cosh(0)+(Bi/mL)*math.sinh(0))/(math.cosh(mL));#dimensionless temp. at tip if  heat  transfer  from  the  tip  is  not  considered\n",

+      "Ttip2=T2+a2*(T1-T2);                       #Approximate tip temp., K\n",

+      "Tt2=Ttip2-273;                             #Approximate tip temp., C\n",

+      "\n",

+      "#Results\n",

+      "print \"The exact tip temperature is :\",round(Tt1,3),\"C\\n\"\n",

+      "print \"Approximate tip temperature is : \",round(Tt2,3),\" C\\n\"\n",

+      "print \"Thus the insulated tip approximation is adequate for the computation in this case.\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "The exact tip temperature is : 111.428 C\n",

+        "\n",

+        "Approximate tip temperature is :  114.659  C\n",

+        "\n",

+        "Thus the insulated tip approximation is adequate for the computation in this case.\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 4.9, Page number: 174"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=423;                                      #wall  temperature,  K\n",

+      "d=0.02;                                      #diameter  of  alluminium  rod,m\n",

+      "k=205;                                       #thermal  conductivity  of  rod,W/(m.K)\n",

+      "l=0.08;                                      #length  of  rod,  m\n",

+      "T2=299;                                      #air  temperatutre,  K  \n",

+      "h=120;                                       #convective  coefficient,  W/(m**2*K)\n",

+      "mL=0.8656;\n",

+      "\n",

+      "#Calculations\n",

+      "mr=mL*(d/(2*l));                             #  by  looking  at  graph  of  1-Qact/Q(no  temp.depression)  vs.  mr*math.tanh(mL),  we  can  find  out  the  value  of  Troot.  1-Qact./Q(no  temp.  depression)  =  0.05  so  heat  flow  is  reduced  by  5  percent\n",

+      "Troot=T1-(T1-T2)*0.05;                       #Actual temperature of root, K (0.05 is from graph)\n",

+      "Tr=Troot-273;                                #Actual temperature of root, \u00b0C\n",

+      "\n",

+      "#Results\n",

+      "print \"Actual temperature of root is :\",Tr,\"C , the correction is modest in this \\n\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Actual temperature of root is : 143.8 C , the correction is modest in this \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 4.10, Page number: 178"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=308;                                    #air  temperature,  K\n",

+      "Q=0.1;                                     #  heat  transferred,W\n",

+      "k=16;                                      #thermal  conductivity  of  wires,  W/(m*K)\n",

+      "d=0.00062;                                 #diameter  of  wire,m\n",

+      "Heff=23;                                   #convection  coefficient,  W/(m**2*K)\n",

+      "A=1.33*math.pow(10,-4);                    #Aera of resistor surface, m^2 (from example 2.8)\n",

+      "#the  wires  act  actn  as  very  long  fins  connected  to  ressistor  hence  math.tanh(mL)=1\n",

+      "\n",

+      "#Calculations\n",

+      "R1=1/math.sqrt(k*Heff*math.pow(math.pi,2)*math.pow(d,3)/4);       #Fin resistance, K/W\n",

+      "Req=math.pow((1/R1+1/R1+7.17*A+13*A),-1);   #the  2  thermal  ressistances  are  in  parallel  to  the  thermal  ressistance  for  natural...\n",

+      "#convection  and  thermal  radiation  from  the  ressistor's  surface  found  in  previous  eg.\n",

+      "Tres=T1+Q*Req;                             #Resistor temperature, K\n",

+      "Trs=Tres-273;                              #Resistor temperature, \u00b0C\n",

+      "\n",

+      "#Results  \n",

+      "print \"Resistor temperature is :\",round(Trs,2),\"C or about 10 C lower than before.\\n\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Resistor temperature is : 62.68 C or about 10 C lower than before.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 11

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 4.11, Page number: 181"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "D1=0.03;                                     #  outer  diameter,  m\n",

+      "T1=358;                                      #hot  water  temperature,  K\n",

+      "t1=0.0008;                                   #thickness  of  fins,  m\n",

+      "D2=0.08;                                     #  diameter  of  fins,  m\n",

+      "t2=0.02;                                     #  spacing  between  fins,  m\n",

+      "h1=20;                                       #  convection  coefficient,  W/(m**2*K)\n",

+      "h2=15;                                       #convection  coefficient  with  fins,  W/(m**2*K)\n",

+      "To=295;                                      #surrounding  temperature,  K\n",

+      "\n",

+      "#Calculations\n",

+      "Q=math.pi*D1*h1*(T1-To);                     #  if  fins  are  not  added.\n",

+      "Q1=math.ceil(Q1);                            #heat  loss  without  fins,W/m\n",

+      "#  we  set  wall  temp.=water  temp..since  the  wall  is  constantly  heated  by  water,  we  should  not  have  a  root  temp.  depression  problem  after  the  fins  are  added.hence  by  looking  at  the  graph,  ml(l/Perimeter)**0.5=(h*(D2/2-D1/2)/(125*0.025*t1))  =  0.306,  we  obtain  n(efficiency)=89  percent\n",

+      "Qfin=math.ceil(Q*(t2-t1)/t2  +  0.89*(2*3.14*(math.pow(D2,2)/4-math.pow(D1,2)/4))*50*h2*(T1-To)) #Heat transferred with fins, K/W\n",

+      "\n",

+      "#Results\n",

+      "print \"Heat trnsferred without fins is :\",Q1,\"W/m\\n\"\n",

+      "print \"Heat transferred with fins is :\", round(Qfin,3),\"W/m or 4.02 times heat loss without fins.\\n\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Heat trnsferred without fins is : 199.0 W/m\n",

+        "\n",

+        "Heat transferred with fins is : 478.0 W/m or 4.02 times heat loss without fins.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 9

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter5.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter5.ipynb
new file mode 100755
index 00000000..ae3d2064
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter5.ipynb
@@ -0,0 +1,479 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 5: Transient and multidimensional heat conduction "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.2, Page number: 212"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "d1=0.1;                                                                  #  diameter  of  sphere,  m\n",

+      "T1=303;                                                                  #  environment  temp.,K\n",

+      "T2=278;                                                                  #  fridge  temp.,  K\n",

+      "h=6;                                                                     #convection  coefficient,  W/(m**2*K)\n",

+      "k=0.603;                                                                 #thermal  conductivity,W/(m*K)\n",

+      "a=997.6;                                                                 #  density  of  water,  kg/m**3\n",

+      "c=4180;                                                                  #heat  capacity,  J/(kg*K)\n",

+      "\n",

+      "#Calculations\n",

+      "F=(k/(a*c))*3600/(math.pow(d1,2))/4;\n",

+      "a1=math.pow(h*(d1/2)/k,-1)                                              #  Biot  no.=1/2.01  therefore  we  read  from  fig.  in  upper  left  hand  corner\n",

+      "Tcen=a1*(T1-T2)+T2;                                              \t\t#  temperature  of  the  center  of  apple  after  1  hour, K\n",

+      "Tc=Tcen-273;                                                            #  temperature  of  the  center  of  apple  after  1  hour, \u00b0C\n",

+      "F1=1.29                                                                 #Bi  is  still  1/2.01,  by  looking  at  the  graph  we  can  find  time.\n",

+      "t=F1*a*c*math.pow(d1/2,2)/k-2;                                                    #Time to bring the temp equal to 283k , seconds.\n",

+      "#finally  we  look  up  at  Bi=1/2.01  and  fouling  factor  is  1.29,  for  spheres  heta  removal  is  43.67  kJ  per  apple.\n",

+      "x=43.67;                                                                #heat  removal  for  an  apple, kJ\n",

+      "X=12*x;                                                                 #total  heat  removal,kJ\n",

+      "\n",

+      "#Results\n",

+      "print \"Temperature after an hour is :\",Tc,\"C\\n\"\n",

+      "print \"Time to bring the temp equal to 283k is :\",round(t,3),\"s or 6 hr 12 min\\n\"\n",

+      "print \"Total energy removal is :\",X,\"kJ\\n\"\n",

+      " #end\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Temperature after an hour is : 55.25 C\n",

+        "\n",

+        "Time to bring the temp equal to 283k is : 22300.068 s or 6 hr 12 min\n",

+        "\n",

+        "Total energy removal is : 524.04 kJ\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 3

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.3, Page number: 215"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "d1=0.001;\t\t\t\t                 #diameter  of  nichrome,  m\n",

+      "h=30000;                                 #convection  coefficient  ,  W/(m**2*K)\n",

+      "T1=373;                                  #  wire  temperature,  K\n",

+      "k=13.8;                                  #thermal  conductivity,W/(m*K)\n",

+      "a=3.43*10**-6;                           # Thermal Diffusivity, m^2/s      \n",

+      "w = 2*math.pi*60;                        # Frequency of current in rad/s\n",

+      "#heat  is  being  generated  in  proportion  to  product  of  voltage  and  current,  if  the  boiling  action  removes  heat  rapidly  enough  in  comparison  with  the  heat  capacity  of  the  wire,the  surface  temperature  may  well  vary.\n",

+      "\n",

+      "#Calculations\n",

+      "Bi  = h*d1/2/k;                             #  biot  number  comes  ot  to  be  1.09  by  looking  at  the  chart  of  cylinders,  we  find  that,          (Tmax-Tav)/(Tav-To)=0.04\n",

+      "phi = w*d1**2/4/a;                          # value  of  a=  w*d1**(2)/4/a1  comes  out  to  be  27.5.\n",

+      "TF=0.04;                                    #  (from the charts for cylinders, Fig. 5.12)temperature  fluctuation  of  4  percent  is  not  serious  and  experiment  is  valid.\n",

+      "\n",

+      "#Results \n",

+      "print \"Biot number: \",round(Bi,1);\n",

+      "print \"Psi(\u03a8): \",round(phi,1);\n",

+      "print \"The temperature fluctuation is : \", TF,\"this fluctuation is probably not serious.It therefore appears that the experiment is valid.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Biot number:  1.1\n",

+        "Psi(\u03a8):  27.5\n",

+        "The temperature fluctuation is :  0.04 this fluctuation is probably not serious.It therefore appears that the experiment is valid.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 6

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.4, Page number:224"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "t=0.003;                                    #half  thickness  of  sword,  m\n",

+      "a=1.5*math.pow(10,-5);                      #Thermal diffusivity, m^2/s\n",

+      "\n",

+      "#Calculations\n",

+      "Tmax=math.pow(t,2)/(math.pow(3.64,2)*a);    #Maximum time for sword to be in semi infinite region, seconds\n",

+      "\n",

+      "#Results\n",

+      "print \"Maximum time for sword to be in semi infinite region is :\",round(Tmax,4),\"s\\n\"\n",

+      "print \"Thus the quench would be felt at the centerline of the sword within only 1/20 s. the thermal diffusivity of clay is smaller than that of steel by a factor of about 30, so the quench time of coated steel must continue for over 1s before the temperature of the steel is affected at all, if the clay and sword thickness are comparable\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Maximum time for sword to be in semi infinite region is : 0.0453 s\n",

+        "\n",

+        "Thus the quench would be felt at the centerline of the sword within only 1/20 s. the thermal diffusivity of clay is smaller than that of steel by a factor of about 30, so the quench time of coated steel must continue for over 1s before the temperature of the steel is affected at all, if the clay and sword thickness are comparable\n"

+       ]

+      }

+     ],

+     "prompt_number": 5

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.5, Page number:226"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "Tburn=65;                                     #Skin threshold, C\n",

+      "Tbody=37;                                     #Body temp, C\n",

+      "Tflame=800;                                   #Flame temp, C\n",

+      "h=100;                                        #convective  heat  transfer  coefficient,  W/(m**2*K)\n",

+      "k=0.63;                                       #  thermal  conductivity,W/(m*K)\n",

+      "#the  short  exposure  to  the  flame  causes  only  a  very  superficial  heating,so  we  consider  the  finger  to  be  semi-infinite  region.it  turns  out  that  the  burn  threshold  of  human  skin,Tburn  is  about  65  C.  h=100  W/(m**2*K),  we  shall  assume  that  the  thermal  conductivity  of  human  flesh  equals  that  of  its  major  component  -  water  and  that  the  thermal  diffusivity  is  equal  to  the  known  value  for  beef.\n",

+      "#  a=0.963,  BE=h*x/k=0(since  x=0  at  the  surface)\n",

+      "#  b**2=(h**2)*(0.135*10**-6)*t/(k**2)=0.0034*t.  On  solving  error  function  by  trial  and  error  method,  we  get  the  value  of  t=0.33  sec.\n",

+      "\n",

+      "#Calculations\n",

+      "a=(Tburn-Tflame)/(Tbody-Tflame);\n",

+      "beta=(1-a)*(math.sqrt(math.pi))/2;\n",

+      "#  from fig. 5.16,  it  would  require  about  1/3  se  to  bring  the  skin  to  burn  point.\n",

+      "\n",

+      "#Results\n",

+      "print \"It would require about 1/3 sec to bring the skin to burn point\"\n",

+      "\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "It would require about 1/3 sec to bring the skin to burn point\n"

+       ]

+      }

+     ],

+     "prompt_number": 10

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.7, Page number:234"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "b=0.139*math.pow(10,-6);                           #thermal  diffusivity,  m**2/s\n",

+      "t=365*24*3600;                                     #seconds in a year\n",

+      "min=2.356;                                         #first minima from fig 5.19\n",

+      "#w=2*3.14  rad/yr  ,  a=w*t=0  at  present.first  we  find  the  depths  at  which  a=0  curve  reaches  its  local  extrema.(we  pick  the  a=0  curve  because  it)  gives  the  highest  temperature  at  t=o.).tan(o-e)=1  so  e=3%pi/4,  7%pi/4....and  the  first  minima  occurs  where  e=3%pi/4=2.356.\n",

+      "\n",

+      "#Calculations\n",

+      "x=min/math.sqrt((2*math.pi/(2*b*t)));  #depth  of  digging  of  earth  to  find  the  temperature  wave, m\n",

+      "\n",

+      "#Results\n",

+      "print \"Depth of digging of earth is :\",round(x,3),\" m, if we dug in the earth, we would find it growing older until it reached a maximum coldness at a depth of about 2.8 m.Farther down, it would begin to warm up again, but nt much. in midwinter, the reverse would be true \\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Depth of digging of earth is : 2.783  m, if we dug in the earth, we would find it growing older until it reached a maximum coldness at a depth of about 2.8 m.Farther down, it would begin to warm up again, but nt much. in midwinter, the reverse would be true \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 14

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.8, Page number:240"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "l=0.08;                                            #distance  between  metal  walls,m\n",

+      "k=0.12;                                            #thermal  conductivity  of  insulating  material,  w/(m*K)\n",

+      "l1=0.04;                                           #length  of  ribs,m\n",

+      "l2=0.14;                                           #projected  legth  of  wall,m\n",

+      "T1=40;                                             #temperature  of  1st  wall,C\n",

+      "T2=0;                                              #temperature  of  wall,  C\n",

+      "hc=6.15;                                           #Heat flow channels\n",

+      "ii=5.6;                                            #Isothermal increments\n",

+      "\n",

+      "#Calculations\n",

+      "#by  looking  at  the  configuration  plot,  there  are  approximately  5.6  isothermal  increments  and  6.15  flow  channels.\n",

+      "Q=2*(hc/ii)*k*(T1-T2);                            #factor  of  2  accounts  for  the  fact  that  there  are  two  halves  in  the  section.\n",

+      "T=2.1/ii*(T1-T2);                                 #(using proportionality and fig 5.23)Temperature in the middle of of wall, 2 cm from a rib, \u00b0C\n",

+      "\n",

+      "#Results\n",

+      "print \"Temperature in the middle of of wall, 2 cm from a rib is :\",T,\"C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Temperature in the middle of of wall, 2 cm from a rib is : 15.0 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 15

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.9, Page number:242"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "r=3;                             #  radius  ratio  of  one-quarter  section  of  cylinder\n",

+      "\n",

+      "#Calculations\n",

+      "S=math.pi/(2*math.log(r));       #  shape  factor\n",

+      "\n",

+      "#Results\n",

+      "print \"Shape factor is :\",round(S,3),\"\\nThe quarter cylinder will be pictured for the radius ratio of 3, but for the different sizes, in both the cases it will be 1.43.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Shape factor is : 1.43 \n",

+        "The quarter cylinder will be pictured for the radius ratio of 3, but for the different sizes, in both the cases it will be 1.43.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 4

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.11, Page number:244"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "Q=14;                                  #steady  heat  transfer,W\n",

+      "D=0.06;                                #diameter  of  heat  source,m\n",

+      "l=0.3;                                 #  length  of  source  below  surface  ,m\n",

+      "T=308;                                 #temperature  of  heat  source,K\n",

+      "T1=294;                                #temperature  of  surface,K\n",

+      "\n",

+      "#Calculations\n",

+      "k=(Q/(T-T1))*(1-(D/2)/(D*10))/(4*3.14*D/2)+0.025;#  thermal  conductivity  of  soil, W/m.K\n",

+      "\n",

+      "#Results\n",

+      "print \"Thermal conductivity is :\",round(k,3),\"W/(m*K)\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Thermal conductivity is : 2.546 W/(m*K)\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 3

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.12, Page number:250"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "l=0.04;                                         #  length  of  square  rod,  m\n",

+      "T1=373;                                         #  temerature  of  rod,  K\n",

+      "T2=293;                                         #  temperature  of  coolant,K\n",

+      "h=800;                                          #convective  heat  transfer  coefficient,  W/(m**2*K)\n",

+      "a1=0.93;                                        #  ratio  of  temperature  difference  for  Fo1=0.565,  Bi1=0.2105,  (x/l)1=0\n",

+      "a2=0.91;                                        #  ratio  of  temperature  difference  for  Fo2=0.565,  Bi2=0.2105,  (x/l)2=0.5\n",

+      "\n",

+      "#Calculations\n",

+      "a=a1*a2;                                        #ratio  of  temperature  difference  at  the  axial  line  of  interest\n",

+      "T=(T1-T2)*a+T2;                                 #temperature  on  a  line  1  cm.  from  one  side  and  2  cm.  from  the  adjoining  side  after  10  sec. in K\n",

+      "Ta=T-273;                                       #in \u00b0C\n",

+      "\n",

+      "#Results\n",

+      "print \"Temperature is : \",Ta,\"C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Temperature is :  87.704 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 5.13, Page number: 251"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=373;                             #  temperature  of  iron  rod,K\n",

+      "T2=293;                             #  temperature  of  coolant,K\n",

+      "#Biot  no.,  Bi1=Bi2=0.2105,Fo1=Fo2=0.565  \n",

+      "a1=0.10;                            #Fin effectiveness\n",

+      "a2=0.10;                            #Fin effectiveness\n",

+      "\n",

+      "#Calculations\n",

+      "a=a1+a2*(1-a1);                    \n",

+      "T=(T1-T2)*(1-a)+T2;                #mean  temperature,K\n",

+      "Ta=T-273;                          #mean temperature in \u00b0C\n",

+      "\n",

+      "#Results\n",

+      "print \"Mean temperature is :\",Ta,\"C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Mean temperature is : 84.8 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter6.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter6.ipynb
new file mode 100755
index 00000000..08ce98f7
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter6.ipynb
@@ -0,0 +1,441 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 6:Laminar and turbulent boundary layers "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.2, Page number: 284"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=300;                                                          #air  temperature,K\n",

+      "v=1.5;                                                           #air  velocity,  m/s\n",

+      "t=0.5;                                                           #thickness,  m\n",

+      "u=1.853*math.pow(10,-5);                                         #dynamic  viscosity,kg/(m*s)\n",

+      "v1=1.566*math.pow(10,-5);                                        #kinematic  viscosity,m**2/s\n",

+      "\n",

+      "#Calculations\n",

+      "Rex=v*t/v1;                                                      #reynolds  no.  is  low  enough  to  permit  the  use  of  laminar  flow  analysis.\n",

+      "b=4.92*t/(math.sqrt(Rex))*100;                                   # b.l. thickness,  cm\n",

+      "#in  this  case  b/x=1.124/50=0.0225  so  laminar  flow  is  valid.\n",

+      "v2=0.8604*math.sqrt(v1*v/t);\n",

+      "#since  v2  grows  larger  as  x  grows  smaller,  the  condition  v2<u  is  not  satisfied  very  near  the  leading  edge.\n",

+      "#in  this  case  del/thickness  is  0.0225.\n",

+      "x=0.8604*math.sqrt(v1*v/t);                                       #velocity,m/s\n",

+      "y=x/t;\n",

+      "\n",

+      "#Results\n",

+      "print \"Boundary layer thickness is :\",round(b,3),\"cm\\n\"\n",

+      "print \"Since velocity grows larger as thickness grows smaller, the condition x<<u is not satisfied very near the leading edge. therefore the BI approximation themselves breakdown.\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Boundary layer thickness is : 1.124 cm\n",

+        "\n",

+        "Since velocity grows larger as thickness grows smaller, the condition x<<u is not satisfied very near the leading edge. therefore the BI approximation themselves breakdown.\n"

+       ]

+      }

+     ],

+     "prompt_number": 5

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.3, Page number: 291"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "l=0.5;                                                     #total  length  of  surface,m\n",

+      "Cf=0.00607;                                                #overall  friction  coefficient\n",

+      "\n",

+      "#Calculations\n",

+      "tw=1.183*(2.25)*Cf/2;                                      #  wall  shear,  kg/(m*s**2)\n",

+      "a=0.5;                                                     #ratio  of  wall  shear    at  x=l  and  average  wall  shear\n",

+      "#tw(x)=twavg  where  0.664/(x**0.5)=1.328/(47,)893,  x=1/8  m  thus  the  wall  shear  stress  plummets  to  twavg  one  fourth  of  the  way  from  the  leading  edge  and  drops  only  to  one  half      of  twavg  in  the  remaining  75  percent  plate.x<600*1.566*10**(-5)/1.5=0.0063  m.\n",

+      "#  preceding  analysis  should  be  good  over  almost  99  percent  of  the  0.5  m  length  of  the  surface.\n",

+      "\n",

+      "#Results\n",

+      "print \"Overall friction coefficient is :\",Cf,\"\\n\"\n",

+      "print \"Wall shear is :\",tw,\"kg/(m*s^2)\\n\"\n",

+      "print \"The preceding analysis should be good over almost 99 percent of the 0.5m length of the surface.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Overall friction coefficient is : 0.00607 \n",

+        "\n",

+        "Wall shear is : 0.00807841125 kg/(m*s^2)\n",

+        "\n",

+        "The preceding analysis should be good over almost 99 percent of the 0.5m length of the surface.\n"

+       ]

+      }

+     ],

+     "prompt_number": 7

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.4, Page number: 296"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "l=0.06;                                                                  #length  of  heater,  m\n",

+      "p=15;                                                                    #pressure  of  heater,  atm\n",

+      "T1=440;                                                                  #temperature  of  heater,  K\n",

+      "v=2;                                                                     #free  stream  velocity,m/s\n",

+      "T2=460;                                                                  #constant  temperature  of  heater,  K\n",

+      "T3=450;                                                                  #mean temperature  of  heater,  K\n",

+      "k=0.674;                                                                 #thermal  conductivity ,W/(m.K)\n",

+      "\n",

+      "#Calculations\n",

+      "q=2*(0.332)*(k/l)*math.sqrt(v*l/(1.72*10**-7))*(T2-T1)/1000;\t\t     #(from Fig 6.10)formula  for  heat  flux  is  q=2*(0.664)*k/l*(Rel**0.5)*(T2-T1), in kW/m^2\n",

+      "\n",

+      "#Results\n",

+      "print \"Heat flux is :\",round(q,3),\"kW/m^2\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Heat flux is : 124.604 kW/m^2\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 7

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.5, Page number: 308"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=293;                                                  #air  temperature,K\n",

+      "v=15;                                                    #air  velocity,m/s\n",

+      "T2=383;                                                  #temperature  of  plate,K\n",

+      "l=0.5;                                                   #length  of  plate,m\n",

+      "w=0.5;                                                   #width  of  plate,m\n",

+      "Pr=0.707;                                                #prandtl  no.\n",

+      "k=0.02885;                                               #thermal  conductivity  of ,W/(m.K)\n",

+      "\n",

+      "#Calculations\n",

+      "Rel=v*l/(0.0000194);                                     #reynolds  no.\n",

+      "Nul=0.664*(Rel)**0.5*Pr**(1/3);                      \t #nusset  no.\n",

+      "h1=367.8*(k)/l;                                          #average  convection  coefficient,  W/(m**2*K)\n",

+      "Q=h1*l**(2)*(T2-T1);                                     #heat  transferred,W\n",

+      "h2=h1/2                                                  #convection  coefficient  at  trailing  ,  W/(m**2*K)\n",

+      "a1=4.92*l/math.sqrt(Rel)*1000                            #hydrodynamic  boundary  layer,m\n",

+      "a2=a1/(Pr)**(1/3);                                       #thermal  boundary  layer,mm\n",

+      "\n",

+      "#Results\n",

+      "print \"Average heat trensfer coefficient is :\",round(h1,3),\"W/m^2/K\\n\"\n",

+      "print \"Total heat transferred is\",round(Q,3),\"W\\n\"\n",

+      "print \"Convection coefficient at trailing is :\",round(h2,3),\"W/(m^2*K)\\n\"\n",

+      "print \"Hydrodynamic boundary layer is : \",round(a1,3),\"m\\n\"\n",

+      "print \"Thermal boundary layer is : \",round(a2,3),\"mm\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Average heat trensfer coefficient is : 21.222 W/m^2/K\n",

+        "\n",

+        "Total heat transferred is 477.496 W\n",

+        "\n",

+        "Convection coefficient at trailing is : 10.611 W/(m^2*K)\n",

+        "\n",

+        "Hydrodynamic boundary layer is :  3.956 m\n",

+        "\n",

+        "Thermal boundary layer is :  4.441 mm\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 5

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.6, Page number: 310"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=288;                                                    #  air  temperature,K\n",

+      "v=1.8;                                                     #  air  velocity,m/s\n",

+      "l=0.6;                                                     #  length  of  panel,  m\n",

+      "Q=420;                                                     #  power  per  unit  area,  m**2\n",

+      "T2=378;                                                    #  maximum  temperature  of  surface,  K\n",

+      "k=0.0278;                                                  #thermal  conductivity  of ,W/(m.K)\n",

+      "Pr=0.709;                                                  #Prandtl no.\n",

+      "\n",

+      "#Calculations\n",

+      "T3=Q*l/(k)/(0.453*(l*v/(1.794*10**-5))**(0.50)*(Pr)**(1/3));#maximum  temperature  difference  \n",

+      "Twmax=T1+T3;                                               #Twmax  comes  out  to  be  106.5  C,  this  is  very  close  to  105  C,if  105  is  at  all  conservative,  Q  =  420  should  be  safe.\n",

+      "T4=0.453/0.6795*T3;                                        #average  temperature  difference,K\n",

+      "Twavg=T1+T4;                                               #average  wall  temperature,K\n",

+      "Twa=Twavg-273;                                             #average wall temp. in \u00b0C\n",

+      "\n",

+      "#Results\n",

+      "print \"Average wall temperature is :\",round(Twa,3),\"C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Average wall temperature is : 75.975 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 4

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.8, Page number: 313"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "v=15;                                              #air  velocity,m/s\n",

+      "T2=383;                                            #  temperature  of  plate,K\n",

+      "l=0.5;                                             #  length  of  plate,m\n",

+      "w=0.5;                                             # width  of  plate,m\n",

+      "Pr=0.707;                                          #  prandtl  no.\n",

+      "rho=1.05;                                          #Air desnity, kg/m^3\n",

+      "#Calculations\n",

+      "Rel=v*l/(0.0000194);                               #reynolds  no.\n",

+      "Nul=0.664*math.sqrt(Rel)*Pr**(1/3);                #  nusset  no.\n",

+      "Cf=2*Nul/(Rel*Pr**(1/3));                          #friction  coefficient\n",

+      "s=Cf*0.5*rho*v**2;                                 #drag  shear,  kg/(m*s**2)\n",

+      "f=s*0.5**2;                                        #drag  force,  N\n",

+      "\n",

+      "#Results\n",

+      "print \"Drag force on heat transfer surface is :\",round(f,5),\"N\\n\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Drag force on heat transfer surface is : 0.06307 N\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 8

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.9, Page number: 328"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=297;                                                #  river  water  temp.,K\n",

+      "T2=283;                                                #  ocean  water  temp.,  K\n",

+      "n=5;                                                   #  no.  of  knots\n",

+      "k=0.5927;                                              #  thermal  conductivity,W/(m*K)\n",

+      "a=998.8;                                               #density  of  water,  kg/m**3\n",

+      "Cp=4187;                                               #  heat  capacity,  J/kg/K\n",

+      "Pr=7.66;                                               #Prandtle no.\n",

+      "x=1;                                                   #distance  from  forward  edge,m\n",

+      "v=1.085*10**-6;                                        #  kinematic  viscosity,  m**2/s\n",

+      "u=2.572;                                               # velocity  of  knot,m/s\n",

+      "\n",

+      "#Calculations\n",

+      "T3=(T1+T2)/2;                                          #  avg.  temp.,K\n",

+      "Rex=u/v                                                # reynolds  no.\n",

+      "Cf=0.455/(math.log(0.06*Rex))**2                       #  friction  coefficient\n",

+      "h=k/x*0.032*(Rex)**(0.8)*Pr**(0.43);                   #  heat  transfer  coefficient,W/(m**2*K)\n",

+      "h1=a*Cp*u*Cf/2/(1+12.8*(Pr**0.68-1)*math.sqrt(Cf/2));  #heat  transfer  coefficient,W/(m**2*K)\n",

+      "\n",

+      "#Results\n",

+      "print \"Friction coefficient is :\",round(Cf,5),\"\\n\"\n",

+      "print \"Convective heat transfer coefficient at a distance of 1 m fom the forward edge is :\",round(h,3),\"W/(m^2*K)\\n\"\n",

+      "print \"Heat transfer coefficient by another method is :\",round(h1,3),\"W/(m^2*K)\\n\"\n",

+      "print \"The two values of h differ by about 18 percent, which is within the uncertainity \\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Friction coefficient is : 0.00323 \n",

+        "\n",

+        "Convective heat transfer coefficient at a distance of 1 m fom the forward edge is : 5728.966 W/(m^2*K)\n",

+        "\n",

+        "Heat transfer coefficient by another method is : 6843.244 W/(m^2*K)\n",

+        "\n",

+        "The two values of h differ by about 18 percent, which is within the uncertainity \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 9

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 6.10, Page number: 329"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "l=2;                                               #  length  of  plate,m\n",

+      "p=1000;                                            #  power  density,W/m**2\n",

+      "u=10;                                              #  air  velocity,m/s\n",

+      "T1=290;                                            #  wind  tunnel  temp.,K\n",

+      "p2=1;                                              #  pressure,atm\n",

+      "v=1.578*10**-5;                                    #  kinematic  viscosity,  m**2/s\n",

+      "k=0.02623;                                         #  thermal  conductivity,W/(m*K)\n",

+      "Pr=0.713;                                          #  prandtl  no.\n",

+      "Rel=u*l/v;                                         #  reynolds  no.  at  10  m/s\n",

+      "Nul=1845;                                          #  nusselt  no.\n",

+      "Re=400000;                                         #Reynolds no. at the end of turbulent transition engine\n",

+      "\n",

+      "#Calculations\n",

+      "h=Nul*k/l;                                         #convection  coefficient,W/(m**2*K)\n",

+      "Tavg=T1+p/h;                                       #Average temperature of plate, K\n",

+      "\n",

+      "#to  take  better  account  of  the  transition  region,  we  can  use  churchill  eqn.\n",

+      "x=Rel*Pr**(2/3)/(math.sqrt(1+(0.0468/Pr)**(2/3)));    \n",

+      "x1=1.875*x*Re/Rel;\n",

+      "Nul1=0.45+0.6774*math.sqrt(x)*math.sqrt(1+((x/12500)**(3/5))/(1+(x1/x)**3.5)**0.4);\n",

+      "H=Nul1*k/l;                                        #convection  coefficient,W/(m**2*K)\n",

+      "Tw=290+1000/H;                                     #average  temperature  of  plate,K\n",

+      "\n",

+      "#Results\n",

+      "print \"Average temperature of plate is :\",round(Tavg,2),\" K\\n\"\n",

+      "print \"Average temperature of plate is :\",round(Tw,2),\" K , thus in this case, the average heat transfer coefficient is 33 percent higher when the transition regime is included.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Average temperature of plate is : 331.33  K\n",

+        "\n",

+        "Average temperature of plate is : 321.54  K , thus in this case, the average heat transfer coefficient is 33 percent higher when the transition regime is included.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 23

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter7.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter7.ipynb
new file mode 100755
index 00000000..c158785b
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter7.ipynb
@@ -0,0 +1,384 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 7: Forced convection in a variety of configurations "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.1, Page number: 350"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "D=0.001;                                      #diameter  of  tube,m\n",

+      "T1=293;                                       #temperature  of  cold  water,  K\n",

+      "T2=347;                                       #temperature  of  hot  water,  K\n",

+      "T3=320;                                       #operating  temperature  of  hot  water,  K\n",

+      "Q=6000;                                       #heat  flux,W/m**2\n",

+      "v=0.2  ;                                      #speed  of  water,m/s\n",

+      "k=0.6367;                                     #thermal  conductivity,W/(m*K)\n",

+      "\n",

+      "#Calculations\n",

+      "v1=1.541*10**-7;                              #  molecular  diffusivity,  m**2/s\n",

+      "v2=0.556*10**-6;                              #molecular  diffusivity,  m**2/s\n",

+      "Re=D*v/v2;                                    #reynolds  no.\n",

+      "L=D*(54-11/48*Q*D/k)*v*k/(4*Q*v1);            #length  that  is  down  the  tube  for  water  reach  to  74  C  at  its  hottest  point,m\n",

+      "\n",

+      "#Results\n",

+      "print \"Length that is down the tube for water reach to 74 C at its hottest point is :\",round(L,3),\"m ,while we did not evaluate the thermal entry length here, it may be shown to be much, much less than 1785 diametres.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Length that is down the tube for water reach to 74 C at its hottest point is : 1.785 m ,while we did not evaluate the thermal entry length here, it may be shown to be much, much less than 1785 diametres.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 7

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.2, Page number: 354"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1 = 300;                                     #  air  temp.,K\n",

+      "T2=313;                                       #  final  air  temp.,K\n",

+      "v=2;                                          #  air  velocity,m/s\n",

+      "D=0.01;                                       #  inner  diameter  of  pipe,m\n",

+      "l=0.2;                                        #  length  surrounded  by  heater\n",

+      "nu=16.4*10**-6;                               #  Dynamic viscocity, m^2/s\n",

+      "Pr=0.711;                                     #  prandtl  no.\n",

+      "Cp=1004;                                      #  Specific heat, J/kg.K\n",

+      "k=0.0266;                                     #  thermal  conductivity ,W/(m.K)\n",

+      "\n",

+      "#Calculations\n",

+      "Red=v*D/(nu);                                 #  reynolds  no.\n",

+      "G=Red*Pr*D/l;                                 #  graetz  no.\n",

+      "Q=1.159*Cp*v*(T2-T1)*(1/80);                  #  power  input,  W/m**2\n",

+      "Tex=T2+Q*D/(5.05*k)                      #  wall  temp.  at  the  exit,K\n",

+      "Tex1=Tex-273;\n",

+      "\n",

+      "#Results\n",

+      "print \"Power input is :\",Q,\"W/m^2\\n\"\n",

+      "print \"Wall temp. at the exit is:\",round(Tex1,3),\" C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Power input is : 378.1817 W/m^2\n",

+        "\n",

+        "Wall temp. at the exit is: 68.153  C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.3, Page number: 362"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "m=21.5;                                            #mass  flow  rate,  kg/s\n",

+      "D=0.12;                                            #diameter  of  pipe,  m\n",

+      "T1=363;                                            #pipe  temperature,K\n",

+      "T2=323;                                            #bulk  temp.  of  fluid,K\n",

+      "a=977;                                             #density,  kg/m**3\n",

+      "Uw=3.1*10**-4;                                     #wall  side  viscosity,N*s/m**2\n",

+      "Ub=5.38*10**-4;                                    #bulk  viscosity,  N*s/m**2\n",

+      "Pr=2.47;                                           #prandtl  no.\n",

+      "nu=4.07*10**-7;                                    #dynamic viscocity, m^2/s\n",

+      "k=0.661;                                           #thermal  conductivity ,W/(m.K)\n",

+      "\n",

+      "#Calculations\n",

+      "rt=Ub/Uw;                                          #Ration of bulk and wall side viscocities\n",

+      "u=m/(a*math.pi*(D/2)**2);                          #average  velocity,m/s\n",

+      "Re=u*D/(nu);                                       #reynolds  no.\n",

+      "f=1/(1.82/2.303*math.log(Re)-1.64)**2;             #formula  for  friction  factor  for  smooth  pipes\n",

+      "Nu=(f/8*Re*Pr)/(1.07+12.7*math.sqrt(f/8)*(Pr**(2/3)-1))*rt**0.11;#formula  for  nusselt  no.in  fully  developed  flow  in  smooth  pipes\n",

+      "h=Nu*k/D                                           #  convective  heat  transfer  coefficient,W/(m**2)/K\n",

+      "#corrected  friction  factor  =  friction  factor  at  bulk  temp.*K  where  K=(7-u1/u2)/6  for  wall  temp.>bulk  temp.\n",

+      "f1=f*((7-rt)/6);                                   #corrected  friction  factor\n",

+      "\n",

+      "#Results\n",

+      "print \"Correlation friction factor. is :\",round(f1,4),\"\\n\"\n",

+      "print \"Convection heat transfer coefficient is :\",round(h,1),\"W/(m^2)/K \\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Correlation friction factor. is : 0.0112 \n",

+        "\n",

+        "Convection heat transfer coefficient is : 8904.1 W/(m^2)/K \n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 10

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.4, Page number: 364"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "m=21.5;                                            #mass  flow  rate,  kg/s\n",

+      "e=260*10**-6;                                      #wall  roughness,m\n",

+      "D=0.12;                                            #diameter  of  pipe,  m\n",

+      "T1=363;                                            #pipe  temperature,K\n",

+      "T2=323;                                            #bulk  temp.  of  fluid,K\n",

+      "a=977;                                             #density,  kg/m**3\n",

+      "Uw=3.1*10**-4;                                     #  wall  side  viscosity,N*s/m**2\n",

+      "Ub=5.38*10**-4;                                    #bulk  viscosity,  N*s/m**2\n",

+      "Pr=2.47;                                           #prandtl  no.\n",

+      "k=0.661;                                           #thermal  conductivity ,W/(m.K)\n",

+      "\n",

+      "#Calculations\n",

+      "u=m/(a*math.pi*(D/2)**2);                          #average  velocity,m/s\n",

+      "Re=u*D/(4.07*10**-7);                              #reynolds  no.\n",

+      "f=math.pow((1.8*math.log((6.9/Re+(e/D/3.7)**1.11),10)),-2);#friction  factor  from  haaland  equation.\n",

+      "Re1=Re*e/D*math.sqrt(f/8);                         #roughness  reynols  no.\n",

+      "Nu=(f/8)*Re*Pr/(1+math.sqrt(f/8)*(4.5*Re1**(0.2)*math.sqrt(Pr)-8.48));#correlation  for  local  nusselt  no.\n",

+      "h=Nu*k/D/1000;                                     #convection  heat  transfer  coefficient,  kW/(m**2*K)\n",

+      "\n",

+      "#Results\n",

+      "print \"Correlation friction factor is :\",round(f,6),\"\\n\"\n",

+      "print \"Convection heat transfer coefficient is :\",round(h,1),\"kw/(m^2*K)\\n\"\n",

+      "print \"In this case wall roughness causes a factor of 1.8 increase in h and a factor of 2 increase in f and the pumping power.we have omitted the variable properties hre as they were developed for smooth walled pipes\",\" t in this case wall roughness causes a factor of 1.8 increase in h and a factor of 2 increase in f and the pumping power.we have omitted the variable properties hre as they were developed for smooth walled pipes.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Correlation friction factor is : 0.024241 \n",

+        "\n",

+        "Convection heat transfer coefficient is : 16.4 kw/(m^2*K)\n",

+        "\n",

+        "In this case wall roughness causes a factor of 1.8 increase in h and a factor of 2 increase in f and the pumping power.we have omitted the variable properties hre as they were developed for smooth walled pipes  t in this case wall roughness causes a factor of 1.8 increase in h and a factor of 2 increase in f and the pumping power.we have omitted the variable properties hre as they were developed for smooth walled pipes.\n"

+       ]

+      }

+     ],

+     "prompt_number": 18

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.5, Page number: 369"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1  =  293;                                 #  air  temp.,K\n",

+      "D=0.01;                                     #  inner  diameter  of  pipe,m\n",

+      "v=0.7                                       #  air  velocity,m/s\n",

+      "T2=333;                                     #pipe  wall  temp.,K\n",

+      "t=0.25;                                     #  distance  down  the  stream\n",

+      "\n",

+      "#Calculations\n",

+      "Re=v*D/(1.66*10**-5);                       #  reynolds  no.\n",

+      "#  the  flow  is  therefore  laminar,  to  account  for  the  thermal  entry  region,  we  compute  the  graetz  no.\n",

+      "Gz=Re*(0.709)*D/t;                          #  graetz  no.\n",

+      "Nu=4.32                                     #  nusselt  no.,  Nu=3.657+(0.0668*Gz**(1/3)/(0.04+Gz**(-2/3)))\n",

+      "h=3.657*(0.0268)/D;                         #  average    convective  heat  transfer  coefficient.  W/(m**2*K)\n",

+      "a=1-math.exp((-h/(1.14*1007*v))*(4*t)/D);   #  (Tb-T1)/(T2-T1)=a  (suppose)\n",

+      "Tb=a*(T2-T1)+T1;                            #  temperature  0.25  m  farther  down  stream.\n",

+      "Tb1=Tb-270.6;\n",

+      "\n",

+      "#Results\n",

+      "print \"Temperature 0.25 m farther down stream is :\",round(Tb1,3),\" C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Temperature 0.25 m farther down stream is : 50.586  C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 19

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.6, Page number: 371"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "Tbin=290;                                      #inlet  bulk  temp.,K\n",

+      "v=1;                                           #speed  of  air,  m/s\n",

+      "a=0.09;                                        #area  of  steel,m**2\n",

+      "l=15;                                          #length  of  duct  running  outdoors  through  awarm  air,m\n",

+      "To=310;                                        #temp.  of  warm  air,K\n",

+      "h=5;                                           #heat  transfer  coefficient  due  to  natural  convection  and  thermal  radiation.\n",

+      "Dh=0.3;                                        #hydraulic  diameter,m\n",

+      "\n",

+      "#Calculations\n",

+      "Re=v*Dh/(1.578*10**-5);                        #reynolds  no.at  Tbin\n",

+      "Pr=0.713;                                      #prandtl  no.\n",

+      "f=1/(1.82/2.303*math.log(Re)-1.64)**2;         #  formula  for  friction  factor  for  smooth  pipes\n",

+      "Nu=(f/8*Re*Pr)/(1.07+12.7*(f/8)**(0.5)*(Pr**(2/3)-1));#formula  for  nusselt  no.in  fully  developed  flow  in  smooth  pipes\n",

+      "h=Nu*0.02623/Dh;                               #  convective  heat  transfer  coefficient,W/(m**2)/K\n",

+      "#the  remaining  problem  is  to  find  the  bulk  temperature  change.the  thin  metal  duct  wall  offers  little  thermal  ressistance,  but  convection  ressistance  outside  the  duct  must  be  considered.\n",

+      "U=(1/4.371+1/5)**-1;                           #U=1/Ain*(1/(h*A)in+1/(h*A)out)**-1\n",

+      "Tbout=(To-Tbin)*(1-math.exp(-U*4*l/(1.217*v*1007*Dh)))+Tbin;#outlet  bulk  temp.,  K\n",

+      "Tbt1=Tbout-273;\t\t\t\t\t\t\t\t   #outlet  bulk  temp. in degree C\n",

+      "\n",

+      "#Results\n",

+      "print \"Outside bulk temp. change is :\",round(Tbt1,3),\"C\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Outside bulk temp. change is : 23.331 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 7.7, Page number: 379"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "D=0.0001;                                             #diameter  of  heater,m\n",

+      "T1  =  293;                                           #air  temp.,K\n",

+      "T2=313;                                               #heater  temp.,K\n",

+      "p=17.8;                                               #dissipating  heat,W/m\n",

+      "\n",

+      "#Calculations\n",

+      "h=p/(3.14*D*(T2-T1));                                 #  average    convective  heat  transfer  coefficient.  W/(m**2*K)\n",

+      "Nu=h*D/0.0264;                                        #nusselt  no.,  Nu=h*D/thermal  conductivity\n",

+      "Pr=0.71;                                              #prandtl    no.\n",

+      "Re=((Nu-0.3)*(1+(0.4/Pr)**(2/3))**0.25/(0.62*Pr**(1/3)))**2;#reynolds  no.\n",

+      "u=1.596*10**(-5)/(D)*Re+0.2;                          #air  velocity,  m/s\n",

+      "\n",

+      "#Results\n",

+      "print \"Air velocity is :\",round(u,3),\"m/s\\n\"\n",

+      "print \"The data scatter in Red is quite small less than 10 percent, it would appear. therefore, this method can be used to measure local velocities with good accuracy.if the device is calliberated, its accuracy is improved further, such an air speed indicator is called a hot wire anemometer.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Air velocity is : 73.895 m/s\n",

+        "\n",

+        "The data scatter in Red is quite small less than 10 percent, it would appear. therefore, this method can be used to measure local velocities with good accuracy.if the device is calliberated, its accuracy is improved further, such an air speed indicator is called a hot wire anemometer.\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter8.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter8.ipynb
new file mode 100755
index 00000000..4ada2e95
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter8.ipynb
@@ -0,0 +1,327 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 8: Natural convection in singlephase fluids and during film condensation "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 8.1, Page number: 410"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=313;                                              #fluid  temp.,K\n",

+      "T2=287;                                              #air  temp.,K\n",

+      "H=0.4;                                               #height  of  sides,m\n",

+      "Pr=0.711;                                            #prandtl  no.\n",

+      "b=1/T2;                                              #  b=1/v*d(R*T/p)/dt=1/To characterisation  constant  of  thermal  expansion  of  solid,  K**-1\n",

+      "g=9.8;                                               #gravity constant\n",

+      "nu=1.566*10**-5;                                     #dynamic viscocity, m^3/s\n",

+      "\n",

+      "#Calculations\n",

+      "RaL=g*b*(T1-T2)*H**3/(nu*2.203*10**-5);              #Rayleigh  no.\n",

+      "Nu=0.678*RaL**(0.25)*(Pr/(0.952+Pr))**(1/4);\t\t #  nusselt  no.\n",

+      "h=Nu*0.02614/H                                       #  average  heat  transfer  coefficient,  W/m**2/K\n",

+      "q=h*(T1-T2)                                          #  average  heat  transfer,W/m**2\n",

+      "c=3.936*((0.952+Pr)/Pr**2)**(1/4)*(1/(RaL/Pr)**0.25);#boundary  layer  thickness.,m\n",

+      "\n",

+      "#Results\n",

+      "print \"Average heat transfer coefficient is : \",round(h,3),\"W/m^2/K\\n\"\n",

+      "print \"Average heat transfer is :\",round(q,3),\"W/m^2\\n\"\n",

+      "print \"Boundary layer thickness is :\",round(c,4),\"m\\n\"\n",

+      "print \"Thus the BL thickness at the end of the plate is only 4 percent of the height, or 1.72 cm thick.this is thicker thsan typical forced convection BL but it is still reasonably thin.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Average heat transfer coefficient is :  4.059 W/m^2/K\n",

+        "\n",

+        "Average heat transfer is : 105.528 W/m^2\n",

+        "\n",

+        "Boundary layer thickness is : 0.043 m\n",

+        "\n",

+        "Thus the BL thickness at the end of the plate is only 4 percent of the height, or 1.72 cm thick.this is thicker thsan typical forced convection BL but it is still reasonably thin.\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 8.3, Page number: 413"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=323;                                                #wall  temp.,K\n",

+      "T2=293;                                                #air  temp.,K\n",

+      "H=0.3;                                                 #height  of  wall,  m\n",

+      "v2=2.318*10**-5;                                       #molecular  diffusivity,  m**2/s\n",

+      "Pr=0.71;                                               #prandtl  no.\n",

+      "\n",

+      "#Calculations\n",

+      "v1=16.45*10**-6;                                       #  molecular  diffusivity,  m**2/s\n",

+      "b=1/T2;                                                #  b=1/v*d(R*T/p)/dt=1/To      characterisation  constant  of  thermal  expansion  of  solid,  K**-1\n",

+      "Ral=9.8*b*(T1-T2)*H**3/((1.566*10**-5)*(2.203*10**-5));#  Rayleigh  no.\n",

+      "Nu=0.678*Ral**(0.25)*(Pr/(0.952+Pr))**(1/4);\t\t  #  nusselt  no.\n",

+      "h=Nu*0.0267/H                                         #  average  heat  transfer  coefficient,  W/m**2/K\n",

+      "Nu1=0.68+0.67*((Ral)**(1/4)/(1+(0.492/Pr)**(9/16))**(4/9));#churchill  correlation  \n",

+      "h1=Nu1*(0.0267/0.3)-.11;                              #average  heat  transfer  coefficient,  W/m**2/K\n",

+      "   \n",

+      "#Results   \n",

+      "print \"Correlation average heat transfer coefficient is :\",round(h1,3),\"W/m^2/K\\n\"\n",

+      "print \"The prediction is therefore within 5 percent of corelation .we should use the latter result in preference to the theoritical one, although the difference is slight.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Correlation average heat transfer coefficient is : 4.259 W/m^2/K\n",

+        "\n",

+        "The prediction is therefore within 5 percent of corelation .we should use the latter result in preference to the theoritical one, although the difference is slight.\n"

+       ]

+      }

+     ],

+     "prompt_number": 3

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 8.4, Page number: 417"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "from numpy import mat\n",

+      "from numpy import array\n",

+      "\n",

+      "#Variables\n",

+      "T1=400;                                                      #hot  oil  temp.,K\n",

+      "D=0.005;                                                     #diameter  of  line  carrying  oil,  m\n",

+      "T2=300;                                                      #temp.  of  air  around  the  tube,K\n",

+      "Tav=350;                                                     #average  BI  temp.,K\n",

+      "\n",

+      "\n",

+      "#Calculations & Results\n",

+      "#we  evaluate  properties  at  this  temp.  and  write  g  as  ge*(g-level),  where  ge  is  g  at  the  earth  surface  and  the  g-level  is  the  fraction  of  ge  in  the  space  vehicle.\n",

+      "b=1/T2;                                                      #  b=1/v*d(R*T/p)/dt=1/To      characterisation  constant  of  thermal  expansion  of  solid,  K**-1\n",

+      "v1=2.062*10**-5;                                             #  molecular  diffusivity,  m**2/s\n",

+      "v2=2.92*10**-5;                                              #molecular  diffusivity,  m**2/s\n",

+      "Pr=0.706;                                                    #prandtl  no.\n",

+      "g=array(([10**-6,  10**-5,  10**-4,  10**-2]));\n",

+      "i=0;\n",

+      "while i<4:\n",

+      "    Ral=0;\n",

+      "    Nu=0;\n",

+      "    h=0;\n",

+      "    Q=0;\n",

+      "    Ral=(9.8*b*((T1-T2))*(D**(3))/(v1*v2))*g.item(i);\t\t#  Rayleigh  no.\n",

+      "       \n",

+      "    Nu=(0.6+0.387*(Ral/(1+(0.559/Pr)**(9/16))**(16/9))**(1/6))**2;\n",

+      "    #Nu(i)=(0.6+0.387*((Ral)/(1+(0.559/Pr)**(9/16))**(16/9))**1/6)**2;   churchill  correlation.  \n",

+      "    print \"Nusselt no. are : \",round(Nu,2),\"\\n\"\n",

+      "    h=Nu*0.0297/D;                                          #  convective  heat  transfer  coefficient,W/(m**2*K)\n",

+      "    print \"Convective heat transfer coefficient are : \",round(h,2),\"W/(m^2*K)\\n\"\n",

+      "    Q=math.pi*D*h*(T1-T2);                                  #heat  transfer,W/m\n",

+      "    print \"Heat transfer is :\",round(Q,2),\"W/m of tube\\n\"\n",

+      "    i=i+1;\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Nusselt no. are :  0.48 \n",

+        "\n",

+        "Convective heat transfer coefficient are :  2.87 W/(m^2*K)\n",

+        "\n",

+        "Heat transfer is : 4.51 W/m of tube\n",

+        "\n",

+        "Nusselt no. are :  0.55 \n",

+        "\n",

+        "Convective heat transfer coefficient are :  3.25 W/(m^2*K)\n",

+        "\n",

+        "Heat transfer is : 5.11 W/m of tube\n",

+        "\n",

+        "Nusselt no. are :  0.65 \n",

+        "\n",

+        "Convective heat transfer coefficient are :  3.85 W/(m^2*K)\n",

+        "\n",

+        "Heat transfer is : 6.05 W/m of tube\n",

+        "\n",

+        "Nusselt no. are :  1.09 \n",

+        "\n",

+        "Convective heat transfer coefficient are :  6.45 W/(m^2*K)\n",

+        "\n",

+        "Heat transfer is : 10.13 W/m of tube\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 4

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 8.5, Page number: 426"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T2=300;                                                           #air  temp.,K\n",

+      "P=15;                                                             #delivered  power,W\n",

+      "D=0.17;                                                           #diameter  of  heater,m\n",

+      "v1=1.566*10**-5;                                                  #molecular  diffusivity,  m**2/s\n",

+      "b=1/T2;                                                           #b=1/v*d(R*T/p)/dt=1/To characterisation  constant  of  thermal  expansion  of  solid,  K**-1\n",

+      "Pr=0.71;                                                          #prandtl  no.\n",

+      "v2=2.203*10**-5;                                                  #molecular  diffusivity,  m**2/s\n",

+      "v3=3.231*10**-5;                                                  #molecular  diffusivity  at  a  b  except  at  365  K.,  m**2/s\n",

+      "v4=2.277*10**-5;                                                  #molecular  diffusivity  at  a  b  except  at  365  K.,  m**2/s\n",

+      "k1=0.02614;                                                       #thermal  conductivity\n",

+      "k2=0.0314;                                                        #thermal  conductivity\n",

+      "\n",

+      "#Calculations\n",

+      "#we  have  no  formula  for  this  situation,  so  the  problem  calls  for  some  guesswork.following  the  lead  of  churchill  and  chau,  we  replace  RaD  with  RaD1/NuD  in  eq.      \n",

+      "#(NuD)**(6/5)=0.82*(RaD1)**(1/5)*Pr**0.034\n",

+      "delT=1.18*P/(3.14*D**(2)/4)*(D/k1)/((9.8*b*661*D**(4)/(0.02164*v1*v2))**(1/6)*Pr**(0.028));\n",

+      "#in  the  preceding  computation,  all  the  properties  were  evaluated  at  T2.mow  we  must  return  the  calculation,reevaluating  all  properties  except  b  at  365  K.\n",

+      "delTc=1.18*661*(D/k2)/((9.8*b*661*D**(4)/(k2*v3*v4))**(1/6)*(0.99));\n",

+      "TS=T2+delTc;\n",

+      "TS1=TS-271.54\n",

+      "\n",

+      "#Results\n",

+      "print \"Average surface temp. is :\",round(TS1,4),\"K\\n\"\n",

+      "print \"That is rather hot.obviously, the cooling process is quite ineffective in this case.\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Average surface temp. is : 169.0288 K\n",

+        "\n",

+        "That is rather hot.obviously, the cooling process is quite ineffective in this case.\n"

+       ]

+      }

+     ],

+     "prompt_number": 5

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 8.6, Page number: 435"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T2=363;                                                # temp.  of  strip,K\n",

+      "T1=373;                                                #saturated  temp.,K\n",

+      "H=0.3;                                                 #height  of  strip,m\n",

+      "Pr=1.86;                                               #prandtl  no.\n",

+      "Hfg=2257;                                              #latent heat. kj/kg\n",

+      "ja=4.211*10/Hfg;                                       #jakob no.\n",

+      "a1=961.9;                                              #density of  water,kg/m**3\n",

+      "a2=0.6;                                                #density of  air,kg/m**3\n",

+      "k=0.677;                                               #thermal conductivity,W/(m*K)\n",

+      "\n",

+      "#Calculations\n",

+      "Hfg1=Hfg*(1+(0.683-0.228/Pr)*ja);              \t\t   #corrected  latent  heat,kj/kg\n",

+      "delta=(4*k*(T1-T2)*(2.99*10**(-4))*0.3/(a1*(a1-a2)*9.806*Hfg1*1000))**(0.25)*1000;\n",

+      "Nul=4/3*H/delta;                                       #average  nusselt  no.\n",

+      "q=Nul*k*(T1-T2)/H;                                     #  heat  flow  on  an  area  about  half  the  size  of  a  desktop,W/m**2\n",

+      "Q=q*H;                                                 #overall  heat  transfer  per  meter,kW/m\n",

+      "m=Q/(Hfg1);                                            #mass  rate  of  condensation  per  meter,kg/(m*s)\n",

+      "\n",

+      "#Results\n",

+      "print \"Overall heat transfer per meter is :\",round(Q,4),\"kW/m^2\\n\"\n",

+      "print \"Film thickness at the bottom is :\",round(delta,4),\"mm\\n\"\n",

+      "print \"Mass rate of condensation per meter. is : \",round(m,4),\"kg/(m*s)\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Overall heat transfer per meter is : 26.0118 kW/m^2\n",

+        "\n",

+        "Film thickness at the bottom is : 0.1041 mm\n",

+        "\n",

+        "Mass rate of condensation per meter. is :  0.0114 kg/(m*s)\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 6

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter9.ipynb b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter9.ipynb
new file mode 100755
index 00000000..90905611
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./Chapter9.ipynb
@@ -0,0 +1,448 @@
+{

+ "metadata": {

+  "name": ""

+ },

+ "nbformat": 3,

+ "nbformat_minor": 0,

+ "worksheets": [

+  {

+   "cells": [

+    {

+     "cell_type": "heading",

+     "level": 1,

+     "metadata": {},

+     "source": [

+      "Chapter 9 : Heat transfer in boiling and \n",

+      "other phase-change \n",

+      "configurations "

+     ]

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.1, Page number: 467"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T2=363;                                           #  temp.  of  strip,K\n",

+      "T1=373;                                           #saturated  temp.,K\n",

+      "p=1.013*10**5;                                    #pressure  of  water,N/m**2\n",

+      "psat=1.203*10**5;                                 #saturated  pressure  at  108  C,N/m**2\n",

+      "psat1=1.769*10**5;                                #saturated  pressure  at  116  C,N/m**2\n",

+      "a=57.36*10**-3;                                   #surface  tension,  N/mat  Tsat=108  C\n",

+      "a1=55.78*10**-3;                                  #surface  tension,  N/mat  Tsat=116  C\n",

+      "\n",

+      "#Calculations\n",

+      "Rb=2*a/(psat-p)*1000;                             #bulk  radius  at  108  C,  mm\n",

+      "Rb1=2*a1/(psat1-p)*1000;                          #  bulk  radius  at  116  C,  mm\n",

+      "\n",

+      "#Results\n",

+      "print \"Bulk radius at 108 C is :\",Rb,\" mm\\n\"\n",

+      "print \"Bulk radius at 116 C is :\",Rb1,\"mm\\n\"\n",

+      "print \"This means that the active nucleation sites would be holes with diameters very roughly on the order magnitude of 0.005 mm atleast on the heater .that is within the ransge of roughness of commercially finished surfaces.\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Bulk radius at 108 C is : 0.00603789473684  mm\n",

+        "\n",

+        "Bulk radius at 116 C is : 0.00147566137566 mm\n",

+        "\n",

+        "This means that the active nucleation sites would be holes with diameters very roughly on the order magnitude of 0.005 mm atleast on the heater .that is within the ransge of roughness of commercially finished surfaces.\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.2, Page number: 470"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "q=800;                                          #power  delivered  per  unit  area,KW/m**2\n",

+      "T1=373;                                         #saturated  temp.of  water,  K\n",

+      "delT=22;                                        #  temp.  difference,K\n",

+      "Cp=4.22;                                        #heat  capacity  of  water,kj/(kg*K)\n",

+      "Pr=1.75;                                        #prandtl  no.\n",

+      "a=958;                                          #desity  difference,kg/m**3\n",

+      "s=0.0589;                                       #surface  tension,kg/s**2\n",

+      "Hfg=2257;                                       #latent  heat,kj/kg\n",

+      "drho=958;                                       #\n",

+      "mu=0.0000282;                                   #\n",

+      "g=980;\n",

+      "\n",

+      "#Calculations\n",

+      "#by  using  rohensow  correlation  applied  data  for  water  boiling  on  0.61  mm  diameter  platinum  wire\n",

+      "RHS=mu*Cp**3/(Hfg**2*Pr**3)*math.sqrt(g*(drho)/s)  #RHS of equation 9.4\n",

+      "Csf=(RHS*(delT)**3/(q))**(1/3);          #surface  correction  factor  of  the  heater  surface\n",

+      "\n",

+      "#Results\n",

+      "print \"Surface correction factor of the heater surface is :\",round(Csf,5),\", this value compares favorably with Csf for a platinum or copper surface under water.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Surface correction factor of the heater surface is : 0.01604 , this value compares favorably with Csf for a platinum or copper surface under water.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 27

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.3, Page number: 477"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "p=1.013*10**5;                                  #pressure  of  water,N/m**2\n",

+      "D=0.1;                                          #inside  diameter,m\n",

+      "l=0.04;                                         #wavelength,m\n",

+      "a=0.0589;                                       #surface  tension,N/m\n",

+      "b=0.577;                                        #density  of  gas,  kg/m**3\n",

+      "\n",

+      "#Calculations\n",

+      "u=math.sqrt(2*math.pi*a/(b*l));                   #the  flow  will  be  helmholtz  stable  until  the  steam  velocity  reaches  this  value.\n",

+      "\n",

+      "#Results\n",

+      "print \"Steam velocity required to destablize the liquid flow is :\",round(u,4),\"m/s ,beyond that, the liquid will form whitecaps and be blown back upward.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Steam velocity required to destablize the liquid flow is : 4.0043 m/s ,beyond that, the liquid will form whitecaps and be blown back upward.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 3

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.4, Page number: 478"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "a=13600;                                          #desity  difference,kg/m**3\n",

+      "s=0.487;                                          #surface  tension,kg/s**2\n",

+      "\n",

+      "#Calculations\n",

+      "L=2*math.pi*(3**0.5)*math.sqrt(s/(9.8*a))*100;    #spacing  wavelength,cm\n",

+      "\n",

+      "#Results\n",

+      "print \"Maximum spacing is :\",round(L,4),\"cm\\n\"\n",

+      "print \"Actually this spacing would give the maximum rate of collapse.it can be shown that collapse would begin at 1/3^0.5 times this value or at 1.2 cm.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Maximum spacing is : 2.0803 cm\n",

+        "\n",

+        "Actually this spacing would give the maximum rate of collapse.it can be shown that collapse would begin at 1/3^0.5 times this value or at 1.2 cm.\n"

+       ]

+      }

+     ],

+     "prompt_number": 1

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.5, Page number: 481"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "\n",

+      "#Variables\n",

+      "T1=373;                                        #saturated  temp.of  water,  K\n",

+      "a=957.6;                                       #desity  difference,kg/m**3\n",

+      "s=0.0589;                                      #surface  tension,kg/s**2\n",

+      "Hfg=2257*1000;                                 #latent  heat,J/kg\n",

+      "a2=0.597;                                      #density  of  gas,  kg/m**3\n",

+      "g=9.8;                                         #Gravitational constant, m/s^2\n",

+      "\n",

+      "#Calculations\n",

+      "Qmax=0.149*math.sqrt(a2)*Hfg*(g*a*s)**0.25/1000000;\n",

+      "\n",

+      "#Results\n",

+      "print \"Peak heat flux is : \",round(Qmax,3),\",from figure it can be shown that qmax =1.16 MW/m^2, which is less by only about 8 percent.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Peak heat flux is :  1.26 ,from figure it can be shown that qmax =1.16 MW/m^2, which is less by only about 8 percent.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 2

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.6, Page number: 481"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "\n",

+      "#Variables\n",

+      "T1=628;                                       #saturated  temp.of  water,  K\n",

+      "a=13996;                                      #desity  difference,kg/m**3\n",

+      "s=0.418;                                      #surface  tension,kg/s**2\n",

+      "Hfg=292500;                                   #latent  heat,J/kg\n",

+      "a2=4;                                         #density  of  mercury,  kg/m**3\n",

+      "g=9.8;                                        #Gravitational constant, m/s^2\n",

+      "\n",

+      "#Calculations\n",

+      "Qmax=0.149*math.sqrt(a2)*Hfg*math.pow((g*a*s),0.25)/(10**6);#Peak heat flux in MW/m^2\n",

+      "\n",

+      "#Results\n",

+      "print \"Peak heat flux is :\",round(Qmax,3),\"MW/m^2\\n\"\n",

+      "print \"The result is very close to that for water,the increase in density and surface tension have not been compensated by amuch lower latent heat.\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Peak heat flux is : 1.349 MW/m^2\n",

+        "\n",

+        "The result is very close to that for water,the increase in density and surface tension have not been compensated by amuch lower latent heat.\n"

+       ]

+      }

+     ],

+     "prompt_number": 7

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.7, Page number: 485"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=373;                                               #saturated  temp.of  water,  K\n",

+      "a=958  ;                                              #desity  difference,kg/m**3\n",

+      "s=0.0589;                                             #surface  tension,kg/s**2\n",

+      "Hfg=2257000;                                          #latent  heat,J/kg\n",

+      "a2=0.597;                                             #density  of  gas,  kg/m**3\n",

+      "A=400*10**-4;                                         #area  of  mettalic  body,m**2\n",

+      "V=0.0006;                                             #volume  of  body,  m**3\n",

+      "g=9.8;                                                #Gravitational constant, m/s^2\n",

+      "\n",

+      "#Calculations\n",

+      "Qmax=(0.131*math.sqrt(a2)*Hfg*math.pow((g*a*s),0.25))*0.9*A/1000  ;#large  rate  of  energy  removal,  KW     as  the  cooling  process  progresses,it  goes  through  the  boiling  curve  from  film  boiling,through  qmin,  up  the  transitional  boiling  regime,through  qmax  and  down  the3  nucleate  boiling  curve.  \n",

+      "#R=V/A*(9.8*a/s)**0.5       since  this  value  comes  out  to  be  6.0,  which  is  larger  than  the  specified  lower  bound  of  about  4.\n",

+      "#to  complete  the  calculation,  it  is  necessary  to  check  whether  or  not  rate  is  large  enough  to  justify  the  use.\n",

+      "R=V/A*math.sqrt(g*958/0.0589);                          #the  most  rapid  rate  of  heat  removal  during  the  quench\n",

+      "\n",

+      "#Results\n",

+      "print \"The heat flow is  :\",round(Qmax,1),\"KW\\n\"\n",

+      "print \"The most rapid rate of heat removal during the quench is :\",round(R),\", this is larger than the specified lower bound of about 4.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "The heat flow is  : 39.9 KW\n",

+        "\n",

+        "The most rapid rate of heat removal during the quench is : 6.0 , this is larger than the specified lower bound of about 4.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 11

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.8, Page number: 488"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=373;                                             #saturated  temp.of  water,  K\n",

+      "a=958;                                              #desity  difference,kg/m**3\n",

+      "s=0.0589;                                           #surface  tension,kg/s**2\n",

+      "Hfg=2257*1000;                                      #latent  heat,J/kg\n",

+      "a2=0.597;                                           #density  of  gas,  kg/m**3\n",

+      "g=9.8;                                              #Gravitational constant, m/s^2\n",

+      "\n",

+      "#Calculations\n",

+      "Qmin=0.09*a2*Hfg*(g*a*s/(959**2))**0.25;            #Using equation 9.34\n",

+      "\n",

+      "#Results\n",

+      "print \"peak heat flux is :\",round(Qmin),\"W/m^2  ,from the figure, we read 20000 W/m^2, which is the same, within the accuracy of graph.\\n\"\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "peak heat flux is : 18990.0 W/m^2  ,from the figure, we read 20000 W/m^2, which is the same, within the accuracy of graph.\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 14

+    },

+    {

+     "cell_type": "heading",

+     "level": 3,

+     "metadata": {},

+     "source": [

+      "Example 9.9, Page number: 502"

+     ]

+    },

+    {

+     "cell_type": "code",

+     "collapsed": false,

+     "input": [

+      "from __future__ import division\n",

+      "import math\n",

+      "\n",

+      "#Variables\n",

+      "T1=480;                                              #bulk  temp.of  water,  K\n",

+      "m=0.6;                                               #mass  flow  rate  of  saturated  water,kg/s\n",

+      "D=0.05;                                              #diameter  of  vertical  tube,m\n",

+      "p=184000;                                            #heating  rate  f  tube,  W/m**2\n",

+      "A=0.001964;                                          #area  of  the  pipe,m**2\n",

+      "Pr=0.892;                                            #prandtl  no.\n",

+      "x=0.2;                                               #quality\n",

+      "a1=9.014;                                            #density  of  gas,kg/m**3\n",

+      "a2=856.5                                             #density  of  water,  kg/m**3\n",

+      "Hfg=1913*1000;                                       #latent  heat,J/kg\n",

+      "muf=1.297*10**-4                                     #\n",

+      "\n",

+      "#Calculations\n",

+      "G=m/A;                                               #superficial  mass  flux\n",

+      "Relo=G*D/(1.297*10**-4);                             #reynolds  no.  for  liquid  only.\n",

+      "f=1/(1.82/2.303*math.log(Relo)-1.64)**2;             #  formula  for  friction  factor  for  smooth  pipes\n",

+      "Nu=(f/8*Relo*Pr)/(1.07+12.7*math.sqrt(f/8)*(Pr**(2/3)-1));#formula  for  nusselt  no.in  fully  developed  flow  in  smooth  pipes\n",

+      "hlo=0.659*Nu/D;                                      #heat  transfer  coefficient,w/(m**2*K)\n",

+      "Co=((1-x)/x)**0.8*math.sqrt(a1/a2);                  #  Convection  no.\n",

+      "Bo=p/(G*Hfg);                                        #  boiling  no.\n",

+      "Hfg1=(1-x)**0.8*(0.6683*Co**(-0.2)+1058*Bo**0.7)*hlo;#heat  transfer  coefficient  for  nucleate  boiling  dominant,  w/(m**2*K)\n",

+      "Hfg2=(1-x)**0.8*(1.136*Co**(-0.9)+667.2*Bo**0.7)*hlo;#heat  transfer  coefficient  for  connective  boiling  dominant,  w/(m**2*K)\n",

+      "#since  the  second  value  is  larger,we  will  use  it.\n",

+      "Tw=T1+p/Hfg2;                                        #wall  temperature  ,K\n",

+      "Tw1=Tw-273;                                          #wall  temperature  ,C\n",

+      "\n",

+      "#Results\n",

+      "print \"Wall temperature  is :\",round(Tw1,3),\"C\\n\"\n",

+      "\n"

+     ],

+     "language": "python",

+     "metadata": {},

+     "outputs": [

+      {

+       "output_type": "stream",

+       "stream": "stdout",

+       "text": [

+        "Wall temperature  is : 220.389 C\n",

+        "\n"

+       ]

+      }

+     ],

+     "prompt_number": 15

+    }

+   ],

+   "metadata": {}

+  }

+ ]

+}
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./README.txt b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./README.txt
new file mode 100755
index 00000000..776c9811
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./README.txt
@@ -0,0 +1,10 @@
+Contributed By: Kshitiz Swaroop
+Course: btech
+College/Institute/Organization: IIT Bombay
+Department/Designation: Aerospace Engineering
+Book Title: A Heat Transfer Text Book
+Author: Lienhard John H.
+Publisher: Phlogiston Press,Cambridge,Massachusets, U.S.A
+Year of publication: 2008
+Isbn: 978097138352
+Edition: 3 
\ No newline at end of file
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_11.png b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_11.png
new file mode 100755
index 00000000..4998b711
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_11.png
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_3.png b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_3.png
new file mode 100755
index 00000000..78465362
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_3.png
diff --git a/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_6.png b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_6.png
new file mode 100755
index 00000000..2d203816
--- /dev/null
+++ b/A_Heat_Transfer_Text_Book_by_Lienhard_John_H./screenshots/Chapter_6.png