add/remove/update books

1 files changed, 446 insertions, 0 deletions

diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch17.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch17.ipynb
new file mode 100755
index 00000000..77951e94
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch17.ipynb
@@ -0,0 +1,446 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:82e0373b19da96ab8fd50304caf9cd3e08cf8bad10412b0998bf9110f7a5ae63"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 17 : Design of Catalytic Reactors"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 434\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dt=[0.081,0.205,3.6]; #Reactor diameter for the three reactors in m\n",
+      "dte=[0.04,0.12,0.70]; #Equivalent diameters for the three reactors in m\n",
+      "db=[0.05,0.057,0.07]; #Estimated bubble size in the three reactors in m\n",
+      "Kr1=1.3889;           #Kinet1ic constant for Reaction 1 in s**-1\n",
+      "Kr2=0.6111;           #Kinetic constant for Reaction 2 in s**-1\n",
+      "Kr3=0.022;            #Kinetic constant for Reaction 3 in s**-1\n",
+      "dp=60.;               #Particle size in micrometer\n",
+      "ephsilonm=0.50;       #Void fraction of fixed bed\n",
+      "ephsilonmf=0.55;      #Void fraction at minimum fluidized condition\n",
+      "umf=0.006;            #Velocity at minimum fluidization condition in m/s\n",
+      "D=2E-5;               #Diffusion coefficient of gas in m**2/s\n",
+      "gammab=0.005;         #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "uo=0.2;               #Superficial gas velocity in m/s\n",
+      "XA=0.9;               #Conversion\n",
+      "g=9.81;               #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "Kr12=Kr1+Kr2;\n",
+      "n=len(dt);\n",
+      "i=0;\n",
+      "ubr = [0,0,0]\n",
+      "ub = [0,0,0]\n",
+      "delta = [0,0,0]\n",
+      "ephsilonf = [0,0,0]\n",
+      "gammac = [0,0,0]\n",
+      "gammae = [0,0,0]\n",
+      "Kbc = [0,0,0]\n",
+      "Kce = [0,0,0]\n",
+      "Kf12 = [0,0,0]\n",
+      "Kf3 = [0,0,0]\n",
+      "KfA = [0,0,0]\n",
+      "KfAR = [0,0,0]\n",
+      "KfAR1 = [0,0,0]\n",
+      "tou = [0,0,0]\n",
+      "y = [0,0,0]\n",
+      "SR = [0,0,0]\n",
+      "XA1 = [0,0,0]\n",
+      "y1 = [0,0,0]\n",
+      "y2 = [0,0,0]\n",
+      "tou2 = [0,0,0]\n",
+      "Lf = [0,0,0]\n",
+      "Lm = [0,0,0]\n",
+      "XA2 = [0,0,0]\n",
+      "\n",
+      "import math\n",
+      "while i<n:\n",
+      "    #Preliminary Calcualtions\n",
+      "    ubr[i]=0.711*(g*db[i])**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "    ub[i]=1.55*((uo-umf)+14.1*(db[i]+0.005))*dte[i]**0.32+ubr[i];#Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)\n",
+      "    delta[i]=uo/ub[i];#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "    ephsilonf[i]=1-(1-delta[i])*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "    fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "    gammac[i]=(1-ephsilonmf)*((3/(ubr[i]*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "    gammae[i]=((1-ephsilonmf)*((1-delta[i])/delta[i]))-gammab-gammac[i];#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "    Kbc[i]=4.5*(umf/db[i])+5.85*((D**0.5*g**0.25)/db[i]**(5/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "    Kce[i]=6.77*((D*ephsilonmf*0.711*(g*db[i])**0.5)/db[i]**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "    #Effective rate constant from Eqn.(12.32)\n",
+      "    Kf12[i]=(gammab*Kr12+1/((1/Kbc[i])+(1/(gammac[i]*Kr12+1/((1/Kce[i])+(1/(gammae[i]*Kr12)))))))*(delta[i]/(1-ephsilonf[i]));\n",
+      "    #Rate of reaction 2 for fluidized bed from Eqn.(12.14)\n",
+      "    Kf3[i]=(gammab*Kr3+1/((1/Kbc[i])+(1/(gammac[i]*Kr3+1/((1/Kce[i])+(1/(gammae[i]*Kr3)))))))*(delta[i]/(1-ephsilonf[i]));\n",
+      "    #Rate of raection with respect to A from Eqn.(12.35)\n",
+      "    KfA[i]=((Kbc[i]*Kce[i]/gammac[i]**2+(Kr12+Kce[i]/gammac[i]+Kce[i]/ \\\n",
+      "    gammae[i])*(Kr3+Kce[i]/gammac[i]+Kce[i]/gammae[i]))*delta[i]*Kbc[i] \\\n",
+      "    *Kr12*Kr3/(1-ephsilonf[i]))/(((Kr12+Kbc[i]/gammac[i])* \\\n",
+      "    (Kr12+Kce[i]/gammae[i])+Kr12*Kce[i]/gammac[i])*((Kr3+Kbc[i]/gammac[i])* \\\n",
+      "    (Kr3+Kce[i]/gammae[i])+Kr3*Kce[i]/gammac[i]));\n",
+      "    KfAR[i]=((Kr1/Kr12)*Kf12[i])-KfA[i];#Rate of reaction from Eqn.(12.34)\n",
+      "    KfAR1[i]=((Kr1/Kr12)*Kf12[i]);#Since KfA is small\n",
+      "    #(b)Relate Selectivity with conversion in three reactors\n",
+      "    x=-math.log(1-XA);#The term Kf12*tou in Eqn.(12.26)\n",
+      "    tou[i]=x/Kf12[i];#Residence time from Eqn.(12.26)\n",
+      "    y[i]=(KfAR1[i]/(Kf3[i]-Kf12[i]))*(math.exp(-x)-math.exp(-tou[i]*Kf3[i]));#CR/CAi from Eqn.(12.27)\n",
+      "    SR[i]=y[i]/XA;#Selectivity of R\n",
+      "    #(c)Relate exit composition to space time\n",
+      "    tou1=5;#Space time in s\n",
+      "    XA1[i]=1-math.exp(-Kf12[i]*tou1);#Conversion from Eqn.(12.26)\n",
+      "    y1[i]=((KfAR1[i]/(Kf12[i]-Kf3[i]))*(math.exp(-Kf3[i]*tou1)-math.exp(-Kf12[i]*tou1)));#CR/CAi R from Eqn.(12.27)\n",
+      "    #(d)Calculate height of bed needed to maximize production\n",
+      "    y2[i]=(KfAR1[i]/Kf12[i])*(Kf12[i]/Kf3[i])**(Kf3[i]/(Kf3[i]-Kf12[i]));#CRmax/CAi R from Eqn.(12.37)\n",
+      "    tou2[i]=math.log(Kf3[i]/Kf12[i])/(Kf3[i]-Kf12[i]);#Space time from Eqn.(38)\n",
+      "    Lf[i]=(uo/(1-ephsilonf[i]))*tou2[i];#Length of bed at fully fluidized condition from Eqn.(12.5)\n",
+      "    Lm[i]=Lf[i]*(1-ephsilonf[i])/(1-ephsilonm);#Length of bed when settled\n",
+      "    XA2[i]=1-math.exp(-Kf12[i]*tou2[i]);#Conversion from Eqn.(12.26)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Let Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively'\n",
+      "print '(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo)',\n",
+      "print '\\tReactor No.\\tKf12(s**-1)\\tuo(m/s)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i\n",
+      "     print '\\t\\t%f'%Kf12[i],\n",
+      "     print '\\t%f'%uo\n",
+      "     i=i+1;\n",
+      "\n",
+      "print '\\n(b)Relation between selectivity with conversion'\n",
+      "print '\\n\\tReactor No.\\tKf12(s**-1)\\tSR(mol R formed/mol A reacted)'\n",
+      "i=0\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i,\n",
+      "     print '\\t\\t%f'%Kf12[i],\n",
+      "     print '\\t%f'%SR[i]\n",
+      "     i=i+1;\n",
+      "\n",
+      "print '(c)Relation between exit compostion and space time',\n",
+      "print '\\tReactor No.\\tXA\\t\\tCR/CAi'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i,\n",
+      "     print '\\t\\t%f'%XA1[i],\n",
+      "     print '\\t%f'%y1[i]\n",
+      "     i=i+1;\n",
+      "\n",
+      "print '(d)Height of bed needed to maximize the production of acrylonitrile',\n",
+      "print '\\tReactor No.\\tLm(m)\\t\\tXA'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i,\n",
+      "     print '\\t\\t%f'%Lm[i],\n",
+      "     print '\\t%f'%XA2[i]\n",
+      "     i=i+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Let Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively\n",
+        "(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo) \tReactor No.\tKf12(s**-1)\tuo(m/s)\n",
+        "\t0\n",
+        "\t\t0.410042 \t0.200000\n",
+        "\t1\n",
+        "\t\t0.270620 \t0.200000\n",
+        "\t2\n",
+        "\t\t0.128980 \t0.200000\n",
+        "\n",
+        "(b)Relation between selectivity with conversion\n",
+        "\n",
+        "\tReactor No.\tKf12(s**-1)\tSR(mol R formed/mol A reacted)\n",
+        "\t0 \t\t0.410042 \t0.641507\n",
+        "\t1 \t\t0.270620 \t0.618358\n",
+        "\t2 \t\t0.128980 \t0.558283\n",
+        "(c)Relation between exit compostion and space time \tReactor No.\tXA\t\tCR/CAi\n",
+        "\t0 \t\t0.871292 \t0.564802\n",
+        "\t1 \t\t0.741562 \t0.484243\n",
+        "\t2 \t\t0.475286 \t0.313823\n",
+        "(d)Height of bed needed to maximize the production of acrylonitrile \tReactor No.\tLm(m)\t\tXA\n",
+        "\t0 \t\t3.056064 \t0.956404\n",
+        "\t1 \t\t4.137401 \t0.939139\n",
+        "\t2 \t\t7.049378 \t0.897005\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 438\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "deltaHr=5.15E8; #Heat of reaction in J/k mol\n",
+      "W=5E4;          #Weight of acrylonitirle produced per 334-day year in tonnes\n",
+      "db=0.07;        #Estimated bubble size in m\n",
+      "dte=0.7;        #Equivalent diameter in m\n",
+      "Kf12=0.35;      #Effective rate constant in s**-1 from Example 1\n",
+      "dp=60;          #Particle size in micrometer\n",
+      "ephsilonm=0.50; #Void fraction of fixed bed\n",
+      "ephsilonmf=0.55;#Void fraction at minimum fluidized condition\n",
+      "T=460;          #Temperature in reactor in degree C\n",
+      "Pr=2.5;         #Pressure inside reactor in bar\n",
+      "#Feed gas composition\n",
+      "x1=1;           #Propylene\n",
+      "x2=1.1;         #Ammonia\n",
+      "x3=11;          #Air\n",
+      "do1=0.08;       #OD of heat exchanger tubes in m\\\n",
+      "L=7;            #Length of tubes in m\n",
+      "ho=300;         #Outside heat transfer coefficient in W/m**2 K\n",
+      "hi=1800;        #Inside heat transfer coefficient in W/m**2 K\n",
+      "Tc=253.4;       #Temperature of coolant in degree C\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Preliminary calculation\n",
+      "uo=0.46;#Superficial gas velocity from Fig.E1(a) for the value of Kf12 & db\n",
+      "tou=8;#Space time from Fig.E2(b) for highest concentraion of product R\n",
+      "Lm=uo*tou/(1-ephsilonm);\n",
+      "y=0.58;#CR/CAi from Fig.E1(c) for the value of tou & Kf12\n",
+      "XA=0.95#From Fig.E1(c) for the value of tou & Kf12\n",
+      "SR=y/XA;#Selectivity of R\n",
+      "\n",
+      "#Cross-sectional area of the reactor\n",
+      "P=W*10**3/(334*24*3600);#Production rate of acrylonitrile\n",
+      "F=(P/0.053)/(SR*XA/0.042);#Feed rate of propylene\n",
+      "V=((F*22.4*(T+273)*(x1+x2+x3))/(42*273*Pr));\n",
+      "At=V/uo;#Cross-sectional area of reactor needed for the fluidized bed\n",
+      "\n",
+      "#Heat exchanger calculation\n",
+      "q=F*XA*deltaHr/42;#Rate of heat liberation in the reactor\n",
+      "U=(ho**-1+hi**-1)**-1;#Overall heat transfer coefficient\n",
+      "deltaT=T-Tc;#Driving force for heat transfer\n",
+      "Aw=q/(U*deltaT);#Heat exchanger area required to remove q\n",
+      "Nt=Aw/(pi*do1*L);\n",
+      "li1=(At/Nt)**0.5;#Pitch for square pitch arrangement\n",
+      "dte1=4*(li1**2-(pi/4)*do1**2)/(pi*do1);\n",
+      "if dte1>dte:\n",
+      "    li=(pi/4*dte*do1+pi/4*do1**2)**0.5;#Pitch if we add dummy tubes\n",
+      "import math\n",
+      "f=li**2-pi/4*do1**2;#Fraction of bed cross section taken up by tubes\n",
+      "dt1=math.sqrt(4/pi*At/(1-f));#Reactor diameter including all its tubes\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Superficial gas velocity=%fm/s'%uo\n",
+      "print 'No. of %1.0fm tubes required=%1.0f'%(L,Nt);\n",
+      "print 'Reactor diameter=%fm'%dt1\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Superficial gas velocity=0.460000m/s\n",
+        "No. of 7m tubes required=295\n",
+        "Reactor diameter=7.173176m\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 444\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "db=0.08;       #Estimated bubble size in m\n",
+      "dte=2;         #Equivalent diameter in m\n",
+      "F1=55.6;       #Feed rate of oil in kg/s\n",
+      "XA=0.63;       #Conversion\n",
+      "uo=0.6;        #Superficial gas velocity in m/s\n",
+      "T1=500.0;      #Temperature of reactor in degree C\n",
+      "T2=580.0;      #Temperature of regenerator in degree C\n",
+      "Fs=F1*23.3;    #Solid circulation rate from Ex.(15.2)\n",
+      "rhos=1200.0;   #Density of catalyst in kg/m**3\n",
+      "dpbar=60.0;    #Average particle size in micrometer\n",
+      "ephsilonm=0.50;#Void fraction of fixed bed\n",
+      "ephsilonmf=0.55;#Void fraction at minimum fluidized condition\n",
+      "umf=0.006;      #Velocity at minimum fluidization condition in m/s\n",
+      "dt=8.0;         #Diameter of reactor in m\n",
+      "D=2E-5;         #Diffusion coefficient of gas in m**2/s\n",
+      "Kr=8.6;         #Rate constant for reaction at 500 degree C in s**-1\n",
+      "Ka1=0.06;       #Rate constant for deactivatiion at 500 degree C in s**-1\n",
+      "Ka2=0.012;      #Rate constant for regeneration at 580 degree C in s**-1\n",
+      "gammab=0.005;   #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "g=9.81;         #Acceleration due to gravity in square m/s**2\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Parameters for the fluidized reactor\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub=1.55*((uo-umf)+14.1*(db+0.005))*dte**0.32+ubr;#Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)\n",
+      "delta=uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "ephsilonf=1-(1-delta)*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "gammac=(1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "Kbc=4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5.0/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "Kce=6.77*((D*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "import math\n",
+      "#Bed height versus catalyst activity in reactor\n",
+      "a1bar=0.07;#Guess value for average activity in reactor\n",
+      "x=Kr*a1bar;#Value of Kra1 to be used in the following equation\n",
+      "Kf=(gammab*x+1/((1/Kbc)+(1/(gammac*x+1/((1/Kce)+(1/(gammae*x)))))))*(delta/(1-ephsilonf));#Effective rate constant from Eqn.(12.14)\n",
+      "tou=-math.log(1-XA)/Kf;#Space time from Eqn.(12.16)\n",
+      "Lm=tou*uo/(1-ephsilonm);#Length of fixed bed for guess value of a1bar\n",
+      "a1bar1=[0.0233,0.0465,0.0698,0.0930,0.116,0.140];#Various activity values to find Lm\n",
+      "x1 = [0,0,0,0,0,0]\n",
+      "Kf1 = [0,0,0,0,0,0]\n",
+      "tou1 = [0,0,0,0,0,0]\n",
+      "Lm1 = [0,0,0,0,0,0]\n",
+      "\n",
+      "n=len(a1bar1);\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    x1[i]=Kr*a1bar1[i];\n",
+      "    Kf1[i]=(gammab*x1[i]+1/((1/Kbc)+(1/(gammac*x1[i]+1/((1/Kce)+ \\\n",
+      "    (1/(gammae*x1[i])))))))*(delta/(1-ephsilonf));\n",
+      "    #Effective rate constant from Eqn.(12.14)\n",
+      "    \n",
+      "    tou1[i]=-math.log(1-XA)/Kf1[i];#Space time from Eqn.(12.16)\n",
+      "    Lm1[i]=tou1[i]*uo/(1-ephsilonm);\n",
+      "    #Length of fixed bed for guess value of a1bar...Condition [i]\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Find the optimum size ratio for various a1bar\n",
+      "Lm=[5,6,7,8,10,12];\n",
+      "W1 = [0,0,0,0,0,0]\n",
+      "t1bar = [0,0,0,0,0,0]\n",
+      "t2bar = [0,0,0,0,0,0]\n",
+      "a1bar2 = [0,0,0,0,0,0]\n",
+      "m=len(Lm);\n",
+      "i=0;\n",
+      "while i<m:\n",
+      "    W1[i]=(pi/4)*dt**2*rhos*(1-ephsilonm)*Lm[i];#Bed weight\n",
+      "    t1bar[i]=W1[i]/Fs;#Mean residence time of solids in reactor\n",
+      "    t2bar[i]=t1bar[i]*(Ka1/Ka2)**0.5;#Mean residence time of soilds at optimum from Eqn.(16)\n",
+      "    a1bar2[i]=(Ka2*t2bar[i])/(Ka1*t1bar[i]+Ka1*t1bar[i]*Ka2*t2bar[i]+Ka2*t2bar[i]);#From Eqn.(15)...Condition (ii)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Final design values\n",
+      "Lm4=7.3;#For satisfying condition [i] & (ii)\n",
+      "a1bar3=0.0744;#By interpolation\n",
+      "x2=a1bar3*Kr;\n",
+      "W11=(pi/4)*dt**2*rhos*(1-ephsilonm)*Lm4;#Bed weight for reactor\n",
+      "t1bar1=W11/Fs;#Mean residence time of solids in reactor\n",
+      "a2bar=(1+Ka1*t1bar1)*a1bar3;#Average activity in regenrator from Eqn.(10)\n",
+      "t2bar1=t1bar1*(Ka1/Ka2)**0.5;#Mean residence time of solids in regenerator from Eqn.(16)\n",
+      "W2=W11*(t2bar1/t1bar1);#Bed weight for regenerator\n",
+      "dt2=dt*(W2/W11)**0.5;#Diameter of regenerator assuming same static bed height for reactor and regerator\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Bed height versus catalyst activity in reactor'\n",
+      "print '\\tAverage activity',\n",
+      "print '\\tLength of fixed bed(m)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '\\t%f'%a1bar1[i],\n",
+      "    print '\\t\\t%f'%Lm1[i];\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Optimum size ratio for various activity in reactor'\n",
+      "print '\\tLength of fixed bed(m)',\n",
+      "print '\\tAverage activity'\n",
+      "i=0\n",
+      "while i<m:\n",
+      "    print '\\t%f'%Lm[i],\n",
+      "    print '\\t\\t%f'%a1bar2[i]\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Final design values'\n",
+      "print '\\tDiameter of reactor(m):%.0f'%dt\n",
+      "print '\\tBed weight for reactor(tons):%.0f'%(W11/10**3)\n",
+      "print '\\tBed weight for regenerator(tons):%.0f'%(W2/10**3)\n",
+      "print '\\tDiameter of regenerator(m):%.0f'%(dt2);\n",
+      "print '\\tSolid circulation rate(tons/hr):%f'%(Fs*3.6);\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Bed height versus catalyst activity in reactor\n",
+        "\tAverage activity \tLength of fixed bed(m)\n",
+        "\t0.023300 \t\t11.059747\n",
+        "\t0.046500 \t\t7.911053\n",
+        "\t0.069800 \t\t6.756202\n",
+        "\t0.093000 \t\t6.118750\n",
+        "\t0.116000 \t\t5.696470\n",
+        "\t0.140000 \t\t5.372072\n",
+        "Optimum size ratio for various activity in reactor\n",
+        "\tLength of fixed bed(m) \tAverage activity\n",
+        "\t5.000000 \t\t0.097879\n",
+        "\t6.000000 \t\t0.086112\n",
+        "\t7.000000 \t\t0.076871\n",
+        "\t8.000000 \t\t0.069420\n",
+        "\t10.000000 \t\t0.058149\n",
+        "\t12.000000 \t\t0.050026\n",
+        "Final design values\n",
+        "\tDiameter of reactor(m):8\n",
+        "\tBed weight for reactor(tons):220\n",
+        "\tBed weight for regenerator(tons):492\n",
+        "\tDiameter of regenerator(m):12\n",
+        "\tSolid circulation rate(tons/hr):4663.728000\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
\ No newline at end of file