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| author | kinitrupti | 2017-05-12 18:53:46 +0530 |
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| committer | kinitrupti | 2017-05-12 18:53:46 +0530 |
| commit | 6279fa19ac6e2a4087df2e6fe985430ecc2c2d5d (patch) | |
| tree | 22789c9dbe468dae6697dcd12d8e97de4bcf94a2 /Chemical_Reaction_Engineering_by_O._Levenspiel | |
| parent | d36fc3b8f88cc3108ffff6151e376b619b9abb01 (diff) | |
| download | Python-Textbook-Companions-6279fa19ac6e2a4087df2e6fe985430ecc2c2d5d.tar.gz Python-Textbook-Companions-6279fa19ac6e2a4087df2e6fe985430ecc2c2d5d.tar.bz2 Python-Textbook-Companions-6279fa19ac6e2a4087df2e6fe985430ecc2c2d5d.zip | |
Removed duplicates
Diffstat (limited to 'Chemical_Reaction_Engineering_by_O._Levenspiel')
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diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/README.txt b/Chemical_Reaction_Engineering_by_O._Levenspiel/README.txt new file mode 100755 index 00000000..e84d96a5 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/README.txt @@ -0,0 +1,10 @@ +Contributed By: Manish Punjabi +Course: mtech +College/Institute/Organization: IIT Bombay +Department/Designation: IEOR +Book Title: Chemical Reaction Engineering +Author: O. Levenspiel +Publisher: Wiley India, New Delhi +Year of publication: 2008 +Isbn: 9788126510009 +Edition: 3
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch1.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch1.ipynb new file mode 100755 index 00000000..dd76e3c5 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch1.ipynb @@ -0,0 +1,119 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 1 : Overview of Chemical Reaction Engineering" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 1.1 page no : 6" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "#l=75 cm,d=60 cm,H20 Produced=108kg/s\n", + "l=0.75 # cylindrical long\n", + "d=0.6; # cylindrical diameter\n", + "V=(3.14*d*d*l)/4;\n", + "M=18.; # molecular weight\n", + "\n", + "# Calculations\n", + "H20_produced=108./M;\n", + "H2_used=H20_produced;\n", + "O2_used=0.5*H20_produced;\n", + "#Rate of reaction of H2(mol/m**3.s)\n", + "r_H2=(H2_used/V)*1000;\n", + "#Rate of reaction of O2(mol/m**3.s)\n", + "r_O2=(O2_used/V)*1000;\n", + "\n", + "# Results\n", + "print \"rate of reaction of H2mol/m**3.s is %.3e mol used/(m**3 of rocket).s\"%(r_H2)\n", + "print \"rate of reaction of O2mol/m**3.s is %.3e mol/m**3.s\"%(r_O2)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "rate of reaction of H2mol/m**3.s is 2.831e+04 mol used/(m**3 of rocket).s\n", + "rate of reaction of O2mol/m**3.s is 1.415e+04 mol/m**3.s\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 1.2 page no : 7" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Assuming density of a person = 1000kg/m3\n", + "\n", + "# Variables\n", + "d = 1000.;\n", + "mass = 75.; # human being\n", + "\n", + "# Calculations\n", + "V = mass/d;\n", + "#moles of O2 consumed per day\n", + "O2_used = (6000./2816)*6;\n", + "# Rate of reaction (mol/m3.s)\n", + "r_O2 = (O2_used/V)/(24.*3600);\n", + "\n", + "# Results\n", + "print \"rate of reaction of O2mol/m**3.s is %.3f mol O2 used/m***3.s\"%(r_O2)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "rate of reaction of O2mol/m**3.s is 0.002 mol O2 used/m***3.s\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch10.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch10.ipynb new file mode 100755 index 00000000..bfe8563f --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch10.ipynb @@ -0,0 +1,119 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 10 : Choosing the Right Kind of Reactor" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 10.1 pageno : 243" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "CAo = 1. # feed\n", + "CA = 0.25\n", + "v = 100. #litre/min\n", + "ko = .025\n", + "k1 = 0.2 # min**-1\n", + "k2 = 0.4 # liter/mol.min\n", + "\n", + "# Calculations\n", + "rA = ko+k1*CA+k2*CA**2\n", + "V = (v/4.)*(CAo-CA)/rA\n", + "#For 4 Reactor System\n", + "Vt = 4*V;\n", + "\n", + "# Results\n", + "print \" The Total volume of 4 reactor system is %.f litres\"%(Vt)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The Total volume of 4 reactor system is 750 litres\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 10.2 pageno : 245" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "print \"For Intermediate R is desired\"\n", + "#we want step 1 fast than 2 and step 1 fast than 3\n", + "print \" E1<E2,E1<E3 so use a low temperature and plug flow \"\n", + "print \"For Product S is desired\"\n", + "#Here speed is all that matters\n", + "print \" High speed is all that matters so use a high temperature and plug flow \"\n", + "print \"For Intermediate T is desired\"\n", + "#We want step 2 fast than 1 and step 2 fast than 4\n", + "print \" E2>E1,E3>E5 so use a falling temperature and plug flow \"\n", + "print \"For Intermediate U is desired\"\n", + "#We want step 1 fast than 2 and step 3 fast than 5\n", + "print \" E2>E1,E3>E5 so use a rimath.sing temperature and plug flow \"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "For Intermediate R is desired\n", + " E1<E2,E1<E3 so use a low temperature and plug flow \n", + "For Product S is desired\n", + " High speed is all that matters so use a high temperature and plug flow \n", + "For Intermediate T is desired\n", + " E2>E1,E3>E5 so use a falling temperature and plug flow \n", + "For Intermediate U is desired\n", + " E2>E1,E3>E5 so use a rimath.sing temperature and plug flow \n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch11.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch11.ipynb new file mode 100755 index 00000000..737bc733 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch11.ipynb @@ -0,0 +1,331 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 11 : Basics of Non-Ideal Flow" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 11.1 pageno : 267" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "%matplotlib inline\n", + "\n", + "from numpy import *\n", + "from matplotlib.pyplot import *\n", + "import math \n", + "\n", + "# Variables\n", + "T = array([0,5,10,15,20,25,30,35]) # time\n", + "Cpulse = array([0,3,5,5,4,2,1,0]) # tracer output concentration\n", + "dt = 5.;\n", + "sum1 = 0.;\n", + "sum2 = 0.;\n", + "Area = 0. #Initialization\n", + "\n", + "# Calculations\n", + "for i in range(8):\n", + " sum1 = sum1+T[i]*Cpulse[i]*dt;\n", + " sum2 = sum2+Cpulse[i]*dt;\n", + " Area = Area+Cpulse[i]*dt;\n", + "\n", + "t = sum1/sum2;\n", + "E = zeros(8)\n", + "for j in range(8):\n", + " E[j] = Cpulse[j]/Area;\n", + "\n", + "# Results\n", + "print \" The mean residence time is %.f min \"%(t)\n", + "plot(T,E)\n", + "plot(T,E,\"go\")\n", + "xlabel(\"t, min\")\n", + "ylabel(\"E\")\n", + "show()" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + " The mean residence time is 15 min \n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x32abdd0>" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 11.2 pageno : 268" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "M = 150. #Molecular mass(gm)\n", + "v = 5. #litre/sec\n", + "v = 5*60. #litre/min\n", + "V = 860. #litres\n", + "Cpulse = .75\n", + "# Calculations and Results\n", + "#From Material Balance\n", + "Area1 = M/v; #gm.min/litre\n", + "A1 = 0.375;\n", + "Area2 = A1*(1+1./4+1./16+1./64+1./256+1./1024+1./4096); #Taking Significant Areas\n", + "\n", + "\n", + "print \" From material balance Area is %.1f gm.min/litre\"%(Area1)\n", + "print \" From Tracer Curve Area is %.1f gm.min/litre\"%(Area2)\n", + "print \" Part a\"\n", + "print \" As the two areas are equal,this is a properly done experiment \"\n", + "#For the liquid,calculating t\n", + "sum1 = 0;\n", + "for i in range(10):\n", + " sum1 = sum1+2*i*A1/(4**(i-1));\n", + " t = sum1/Area1;\n", + "\n", + "#liquid volume in vessel\n", + "Vl = t*v;\n", + "#Fraction of liquid\n", + "f = Vl/V;\n", + "E = Cpulse/(M/v)\n", + "\n", + "print \" Part b\"\n", + "print \" Fraction of liquid is %.f %%\"%(f*100)\n", + "\n", + "print \" Part c\"\n", + "print \" The E curve is %.1f C\"%E\n", + "print \" Part d\"\n", + "print \" The vessel has a strong recirculation of liquid,probably induced by the rising bubbles\"\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " From material balance Area is 0.5 gm.min/litre\n", + " From Tracer Curve Area is 0.5 gm.min/litre\n", + " Part a\n", + " As the two areas are equal,this is a properly done experiment \n", + " Part b\n", + " Fraction of liquid is 93 %\n", + " Part c\n", + " The E curve is 1.5 C\n", + " Part d\n", + " The vessel has a strong recirculation of liquid,probably induced by the rising bubbles\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 11.3 pageno : 272\n" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "Cin = zeros(14)\n", + "E = zeros(14)\n", + "Cout = zeros(14)\n", + "Cin[0] = 0.\n", + "Cin[1] = 8.\n", + "Cin[2] = 4.\n", + "Cin[3] = 6\n", + "Cin[4] = 0\n", + "E[4] = 0\n", + "E[5] = 0.05\n", + "E[6] = 0.5\n", + "E[7] = 0.35\n", + "E[8] = 0.1\n", + "E[9] = 0.\n", + "\n", + "# Calculations\n", + "for t in range(8,14):\n", + " sum1 = 0;\n", + " for p in range(5,t-1):\n", + " if p>10 or (t-p)>5:\n", + " h = 2;\n", + " else:\n", + " sum1 = sum1+Cin[t-p] * E[p];\n", + " Cout[t] = sum1;\n", + "\n", + "t = linspace(1,14,14)\n", + "Cout = transpose(Cout)\n", + "\n", + "# Results\n", + "plot(t,Cout)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "metadata": {}, + "output_type": "pyout", + "prompt_number": 6, + "text": [ + "[<matplotlib.lines.Line2D at 0x43ec990>]" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x4149950>" + ] + } + ], + "prompt_number": 6 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 11.4 pageno : 275" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "import math \n", + "\n", + "# Variables\n", + "k = 0.307; # min**-1\n", + "t = 15.; \n", + "\n", + "# Calculations and Results\n", + "fr_unconverted = math.exp(-k*t);\n", + "print \" The fraction of reactant unconverted in a plug flow reactor is %.2f\"%(fr_unconverted)\n", + "\n", + "#For the real reactor\n", + "T = [5,10,15,20,25,30]; #given time\n", + "E = [0.03,0.05,0.05,0.04,0.02,0.01]; #given\n", + "dt = 5;\n", + "sum1 = 0;\n", + "for i in range(6):\n", + " sum1 = sum1+math.exp(-k*T[i])*E[i]*dt;\n", + "\n", + "print \" The fraction of reactant unconverted in a real reactor is %.3f\"%(sum1)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The fraction of reactant unconverted in a plug flow reactor is 0.01\n", + " The fraction of reactant unconverted in a real reactor is 0.047\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 11.5 pageno : 277" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "k = 0.5 #litre/mol.min\n", + "CAo = 2. #mol/litre\n", + "to = 1.\n", + "t1 = 3.\n", + "E = 0.5\n", + "\n", + "# Calculations\n", + "#Using eqn 13\n", + "def f2(t): \n", + "\t return 1./(1+t)\n", + "\n", + "XA_avg = 1-(E* quad(f2,to,t1)[0])\n", + "# Results\n", + "print \" Average concentration of A remaining in the droplet is %.3f\"%(XA_avg)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Average concentration of A remaining in the droplet is 0.653\n" + ] + } + ], + "prompt_number": 6 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch12.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch12.ipynb new file mode 100755 index 00000000..f90bf55b --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch12.ipynb @@ -0,0 +1,116 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 12 : Compartment Models" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 12.1 page no : 289" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "tg = (8.*(9.-6)*(0.5)+11.*(15.-9)*(0.5))/((15.-6)*0.5) #sec\n", + "tl = 40. #sec\n", + "vg = 0.5\n", + "vl = 0.1;\n", + "\n", + "# Calculations\n", + "Vg = tg*vg;\n", + "Vl = tl*vl;\n", + "G = Vg*10\n", + "L = Vl*10\n", + "Stagnant = (100-G-L)\n", + "\n", + "# Results\n", + "print \" fraction of gas is %.f %%\"%(G)\n", + "print \" fraction of liquid is %.f %%\"%(L)\n", + "print \" fraction of Stangnant liquid is %.f %%\"%(Stagnant)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " fraction of gas is 50 %\n", + " fraction of liquid is 40 %\n", + " fraction of Stangnant liquid is 10 %\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 12.2 page no : 290" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "CAo = 1.;\n", + "XA = 0.75 #present\n", + "CA = 1-XA;\n", + "\n", + "# Calculations\n", + "kt1 = (CAo-CA)/CA;\n", + "kt2 = 3*kt1; #volume is reduced by 1/3\n", + "CA_unconverted = 1./(kt2+1);\n", + "XA = 1-CA_unconverted #New XA after replacing the stirrer\n", + "\n", + "# Results\n", + "print \" New Conversion expected is %.1f %%\"%(XA*100)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " New Conversion expected is 90.0 %\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch13.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch13.ipynb new file mode 100755 index 00000000..205d7e7f --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch13.ipynb @@ -0,0 +1,174 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 13 : The Dispersion ,Wodel" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 13.1 page no : 305" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "T = [0,5,10,15,20,25,30,35]; # time\n", + "Cpulse = [0,3,5,5,4,2,1,0]; # gm/liter \n", + "sum1 = 0;\n", + "sum2 = 0\n", + "sum3 = 0;\n", + "\n", + "# Calculations\n", + "for i in range(8):\n", + " sum1 = sum1+Cpulse[i];\n", + " sum2 = sum2+Cpulse[i]*T[i];\n", + " sum3 = sum3+Cpulse[i]*T[i]*T[i];\n", + "\n", + "t = sum2/sum1;\n", + "sigma_sqr = (sum3/sum1)-((sum2/sum1))**2;\n", + "sigmatheta_sqr = sigma_sqr/t**2;\n", + "m = 0.1\n", + "\n", + "while m <= 0.2:\n", + " sigmat_sqr = 2*m-2*(m**2)*(1-math.exp(-(1./m)));\n", + " if sigmat_sqr >= sigmatheta_sqr:\n", + " break;\n", + " m += 0.001\n", + "\n", + "# Results\n", + "print \" The vessel print ersion number is %.3f\"%(m)\n", + "\n", + "# answer may vary because of rounding error." + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The vessel print ersion number is 0.100\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 3, + "metadata": {}, + "source": [ + "Example 13.2 pageno : 306" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "l = 1219.; # long diameter\n", + "u = 0.0067; #Velocity(mm/s) \n", + "\n", + "#Using the probability graph\n", + "t1 = 178550.\n", + "#84th percentile point fall at\n", + "t2 = 187750.;\n", + "\n", + "# Calculations\n", + "sigma = (t2-t1)/2;\n", + "t = l/u;\n", + "sigma_theta = sigma/t;\n", + "#Vessel print ersion number\n", + "d = sigma_theta**2/2;\n", + "\n", + "# Results\n", + "print \" The vessel print ersion number is %.5f\"%(d)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The vessel print ersion number is 0.00032\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 13.3 page no : 308" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "v = 0.4; # bed voidage\n", + "u = 1.2; # velocity of fluid\n", + "l = 90. #length(cm)\n", + "sigma1_sqr = 39. # output signals\n", + "sigma2_sqr = 64. # output signals \n", + "\n", + "# Calculations\n", + "dsigma_sqr = sigma2_sqr-sigma1_sqr;\n", + "t = l*v/u;\n", + "sigmatheta_sqr = dsigma_sqr/t**2;\n", + "d = sigmatheta_sqr/2;\n", + "\n", + "# Results\n", + "print \" The vessel print ersion number is %.4f\"%(d)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The vessel print ersion number is 0.0139\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch14.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch14.ipynb new file mode 100755 index 00000000..cca681a6 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch14.ipynb @@ -0,0 +1,232 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 14 The Tanks-in-Series Model" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 14.1 pageno : 329" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "#Original and new length(m)\n", + "import math \n", + "\n", + "# Variables\n", + "L1 = 32. # diameter pipe\n", + "L2 = 50. # pipeline length \n", + "sigma1 = 8. # bottles \n", + "\n", + "# Calculations\n", + "# For small deviaqtion from plug flow,sigma_sqr is directly proportional to L\n", + "sigma2 = sigma1*math.sqrt(L2/L1);\n", + "\n", + "# Results\n", + "print \" No of bottles of rose expected is %.f\"%(sigma2)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " No of bottles of rose expected is 10\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 14.2 pageno : 330" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "sigma1 = 14. # hours\n", + "sigma2 = 10.5; # hours\n", + "L1 = 119. # ohio miles apart\n", + "\n", + "# Calculations\n", + "#spread of curve is directly proportional to sqrt of distance from origin\n", + "L = sigma1**2*L1/(sigma1**2-sigma2**2);\n", + "\n", + "# Results\n", + "print \" The dumping of toxic phenol must have occured within %.f miles upstream of cincinnati\"%(L)\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The dumping of toxic phenol must have occured within 272 miles upstream of cincinnati\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 14.3 pageno : 332" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "# from figure\n", + "vo = 1.; \n", + "t1 = 1./6;\n", + "t2 = 1.;\n", + "t3 = 11./6;\n", + "w = 1./10;\n", + "\n", + "# Calculations\n", + "A2_by_A1 = 0.5;\n", + "R = A2_by_A1/(1-A2_by_A1);\n", + "#From the location of 1st peak\n", + "V1 = (R+1)*vo*t1;\n", + "#From the time between peaks\n", + "V2 = (R*vo)*((t2-t1)-(t1));\n", + "#From fig 14.3\n", + "N = 1+(2*(t1/w))**2;\n", + "\n", + "# Results\n", + "print \" The reflux ratio is %.f\"%(R)\n", + "print \" The volume of 1st tank is %.3f\"%( V1)\n", + "print \" The volume of 2nd tank is %.3f\"%(V2)\n", + "print \" The number of tanks are %.f \"%(N)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The reflux ratio is 1\n", + " The volume of 1st tank is 0.333\n", + " The volume of 2nd tank is 0.667\n", + " The number of tanks are 12 \n" + ] + } + ], + "prompt_number": 4 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 14.4 page no :333" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "%matplotlib inline\n", + "\n", + "from matplotlib.pyplot import *\n", + "import math \n", + "from numpy import *\n", + "\n", + "# Variables\n", + "# from figure E14.4a\n", + "t2 = 280.\n", + "t1 = 220.\n", + "sigma1_sqr = 100.\n", + "sigma2_sqr = 1000.\n", + "\n", + "# Calculations\n", + "dt = t2-t1;\n", + "dsigma_sqr = sigma2_sqr-sigma1_sqr;\n", + "N = dt**2/dsigma_sqr;\n", + "\n", + "E = zeros(200)\n", + "\n", + "for t in range(200):\n", + " E[t] = ((t**(N-1))*(N**N)*math.exp(-t*N/dt))/((math.factorial(N-1))*(dt**N));\n", + "\n", + "t = zeros(200) \n", + "for i in range(200):\n", + " t[i] = i;\n", + "\n", + "# Results\n", + "plot(t,E)\n", + "xlabel(\"t, s\")\n", + "ylabel(\"E, s**-1\")\n", + "show()\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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BBx8EnnlG7UqIqDUME5Xt2CEXw6K2PfYYsH498N13aldCRC1RLExMJhNiY2Oh0+mQm5vb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\nfT/rT0BE5BMUuWMXGRkJi8X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+ "text": [ + "<matplotlib.figure.Figure at 0x2625a50>" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [], + "prompt_number": 7 + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch16.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch16.ipynb new file mode 100755 index 00000000..f90f61a4 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch16.ipynb @@ -0,0 +1,98 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 16 Earliness of Mixing, Segregation, and RTD" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 16.1 pageno : 358" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "Co = 1.\n", + "k = 1.\n", + "t = 1. #given\n", + "\n", + "# Calculations and Results\n", + "C1 = (-1+math.sqrt(1-4*t*(-Co)))/2*t;\n", + "#For the plug flow reactor\n", + "#t = 1/k(1/C2-1/C1)\n", + "C2 = C1/(1+k*t*C1);\n", + "print \" Conversion for flow scheme A is %.3f\"%(C2)\n", + "\n", + "#For plug flow\n", + "C3 = Co/(1+k*t*Co);\n", + "#For mixed flow reactor\n", + "C4 = (-1+math.sqrt(1-4*t*(-C3)))/2*t;\n", + "print \" Conversion for flow scheme B is %.3f\"%(C4)\n", + "\n", + "#Using exit age distribution fn for 2 equal plug-mixed flow reactor system,umath.sing fig 12.1\n", + "t_bar = 2.\n", + "in_ = 1000.\n", + "\n", + "def f3(t): \n", + "\t return (2/t_bar)*(math.exp(1-2*t/t_bar))/(1+Co*k*t)\n", + "\n", + "C5 = quad(f3,t_bar/2,in_)[0]\n", + "\n", + "print \" Conversion for flow scheme C,D,E is %.3f\"%(C5)\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Conversion for flow scheme A is 0.382\n", + " Conversion for flow scheme B is 0.366\n", + " Conversion for flow scheme C,D,E is 0.361" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch18.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch18.ipynb new file mode 100755 index 00000000..ca1fa2ec --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch18.ipynb @@ -0,0 +1,465 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 18 Solid Catalyzed Reactions" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 18.1 pageno : 407" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "dp = 2.4*(10**-3);L = dp/6;\n", + "De = 5*10**-5;\n", + "Keff = 1.6;\n", + "h = 160. #heat transfer coefficient(KJ/hr.m2cat.K)\n", + "kg = 300. #mass transfer coefficient(m3/hr.m2cat)\n", + "Hr = -160. #KJ/molA\n", + "CAg = 20. #mol/m3\n", + "rA_obs = 10.**5 #mol/hr.m3cat\n", + "\n", + "# Calculations and Results\n", + "kobs = rA_obs/CAg;\n", + "Vp = 3.14*(dp**3)/6;\n", + "S = 3.14*(dp**2);\n", + "ratio = kobs*Vp/(kg*S);\n", + "\n", + "print \" Part a\"\n", + "if ratio<0.01 :\n", + " print \" Resistance to mass transport to film should not influence rate of reaction\"\n", + "else:\n", + " print \" Resistance to mass transport to film should influence rate of reaction\"\n", + "\n", + "\n", + "print \" Part b\"\n", + "\n", + "Mw = rA_obs*(L**2)/(De*CAg);\n", + "print \" Mw = %.f\"%(Mw)\n", + "if Mw>4:\n", + " print \" Pore diffusion is influencing and hence strong pore diffusion\"\n", + "else:\n", + " print \" Pore diffusion is not influencing and hence weak pore diffuusion\"\n", + "\n", + "dt_max_pellet = De*(CAg-0)*(-Hr)/Keff;\n", + "#Temp variation Across the gas film\n", + "dt_max_film = L*rA_obs*(-Hr)/h;\n", + "\n", + "print \" Part c\"\n", + "print \" dTmax,pellet is %.1f C\"%(dt_max_pellet)\n", + "print \" degree C dTmax,film is %.2f C\"%(dt_max_film)\n", + "print \" degree C\"\n", + "if dt_max_pellet<1:\n", + " print \" Pellet is close to uniform in temperature\"\n", + "else:\n", + " print \" There is a variation in temp within pellet\"\n", + "if dt_max_film<1:\n", + " print \" Film is close to uniform in temperature\"\n", + "else:\n", + " print \" There is a variation in temp within Film\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " Resistance to mass transport to film should not influence rate of reaction\n", + " Part b\n", + " Mw = 16\n", + " Pore diffusion is influencing and hence strong pore diffusion\n", + " Part c\n", + " dTmax,pellet is 0.1 C\n", + " degree C dTmax,film is 40.00 C\n", + " degree C\n", + " Pellet is close to uniform in temperature\n", + " There is a variation in temp within Film\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 18.2 page no : 408" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "%matplotlib inline\n", + "\n", + "from matplotlib.pyplot import *\n", + "from numpy import *\n", + "import math \n", + "from scipy import stats\n", + "\n", + "# Variables\n", + "PAo = 3.2;\n", + "R = 0.082 #litre.atm/mol.k\n", + "T = 390. #k\n", + "v = 20. #litre/hr\n", + "W = 0.01 #/kg\n", + "CA_in = [0.1,0.08,0.06,0.04];\n", + "CA_out = [0.084,0.07,0.055,0.038];\n", + "\n", + "# Calculations\n", + "CAo = PAo/(R*T);\n", + "FAo = CAo*v;\n", + "eA = 3;\n", + "\n", + "XA_in = zeros(4)\n", + "XA_out = zeros(4)\n", + "dXA = zeros(4)\n", + "rA = zeros(4)\n", + "CA_avg = zeros(4)\n", + "\n", + "for i in range(4):\n", + " XA_in[i] = (1-CA_in[i]/CAo)/(1+eA*CA_in[i]/CAo);\n", + " XA_out[i] = (1-CA_out[i]/CAo)/(1+eA*CA_out[i]/CAo);\n", + " dXA[i] = XA_out[i]-XA_in[i];\n", + " rA[i] = dXA[i]/(W/FAo);\n", + " CA_avg[i] = (CA_in[i]+CA_out[i])/2;\n", + "\n", + "# Results\n", + "plot(CA_avg,rA)\n", + "xlabel(\"CA, mol/liter\")\n", + "ylabel(\"-rA, mol/hr. kg cat\")\n", + "coeff1 = stats.linregress(CA_avg,rA)\n", + "k = coeff1[0]\n", + "print \" The rate of reaction is %.3f mol/hr.kg\"%(k),\n", + "print \"CA\"\n", + "print ('The answer slightly differs from those given in book as regress fn is\\\n", + " used for calculating slope and intercept')\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + " The rate of reaction is 109.395 mol/hr.kg" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " CA\n", + "The answer slightly differs from those given in book as regress fn is used for calculating slope and intercept\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x2f0a1d0>" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 18.3 pageno : 410" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "%matplotlib inline\n", + "from numpy import zeros\n", + "from scipy import stats\n", + "\n", + "\n", + "# Variables\n", + "CAo = 0.1 #mol/litre\n", + "FAo = 2. #mol/hr\n", + "eA = 3.\n", + "CA = [0.074,0.06,0.044,0.029] #mol/litre\n", + "W = [0.02,0.04,0.08,0.16] #kg\n", + "\n", + "XA = zeros(4)\n", + "y = zeros(4)\n", + "x = zeros(4)\n", + "W_by_FAo = zeros(4)\n", + "CAout_by_CAo = zeros(4)\n", + "XA1 = zeros(4)\n", + "\n", + "# Calculations\n", + "for i in range(4):\n", + " XA[i] = (CAo-CA[i])/(CAo+eA*CA[i]);\n", + " y[i] = (1+eA)*math.log(1/(1-XA[i]))-eA*XA[i];\n", + " x[i] = CAo*W[i]/FAo;\n", + " W_by_FAo[i] = W[i]/FAo;\n", + " CAout_by_CAo[i] = CA[i]/CAo;\n", + " XA1[i] = (1-CAout_by_CAo[i])/(1+eA*CAout_by_CAo[i]);\n", + "\n", + "# Results\n", + "plot(x,y)\n", + "xlabel(\"CA0W/FAO = W/20, hr.kg cat/liter\")\n", + "ylabel(\"4 ln 1/(1-Xa) -3Xa\")\n", + "coeff3 = stats.linregress(x,y);\n", + "k = coeff3[0];\n", + "print \" Part a, using integral method of analysis\"\n", + "print \" The rate of reactionmol/litre is %.3f\"%(k),\n", + "print \"CA\"\n", + "\n", + "#Part b\n", + "#plotting W_by_FAo vs XA1,the calculating rA = dXA/d(W/FAo) for last 3 points,we get\n", + "rA = [5.62,4.13,2.715];\n", + "coeff2 = stats.linregress(CA[1:],rA);\n", + "\n", + "print \" Part b, using differential method of analysis\"\n", + "print \" The rate of reactionmol/litre) is %.3f\"%(coeff2[0]),\n", + "print \"CA\"\n", + "\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + " Part a, using integral method of analysis" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "\n", + " The rate of reactionmol/litre is 96.804 CA\n", + " Part b, using differential method of analysis\n", + " The rate of reactionmol/litre) is 93.703 CA\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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IWEczvT3YTz+ZzU2pqfDEE+YigZpLISKlNNNbHBPvQkLMEU9bt2rinYhYTxP3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\nSUVORK5CYII=\n", + "text": [ + "<matplotlib.figure.Figure at 0x7ffe3c06fe90>" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 18.4 pageno : 413" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "# from example 18.2\n", + "XA = 0.35;\n", + "FAo = 2000. #mol/hr\n", + "eA = 3.\n", + "k = 96.\n", + "CAo = 0.1;\n", + "\n", + "# Calculations\n", + "W = ((1+eA)*math.log(1./(1-XA))-eA*XA)*(FAo/(k*CAo));\n", + "\n", + "# Results\n", + "print \" The amount of catalyst kg needed in a packed bed reactor is %.f kg\"%(W)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The amount of catalyst kg needed in a packed bed reactor is 140 kg\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 18.5 pageno : 414" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "%matplotlib inline\n", + "\n", + "import math \n", + "from matplotlib.pyplot import *\n", + "from numpy import *\n", + "from scipy import *\n", + "\n", + "# Variables\n", + "CAo = 0.1;\n", + "eA = 3;\n", + "rA = [3.4,5.4,7.6,9.1]; # mol A/hr. kg cat\n", + "CA = [0.039,0.0575,0.075,0.092]; # mol/liter\n", + "\n", + "# Calculations\n", + "XA = zeros(5);\n", + "inv_rA = zeros(5);\n", + "for i in range(4):\n", + " XA[i] = (1-CA[i]/CAo)/(1+eA*CA[i]/CAo);\n", + " inv_rA[i] = 1/rA[i];\n", + "\n", + "for i in range(4):\n", + " small = XA[i];\n", + " for j in range(i,4):\n", + " next_ = XA[j];\n", + " if small>next_:\n", + " XA[i],XA[j] = XA[j],XA[i];\n", + " inv_rA[i],inv_rA[j] = inv_rA[j], inv_rA[i]\n", + "\n", + "\n", + "# Results\n", + "plot(XA,inv_rA)\n", + "xlabel(\"Xa, dimensionless\")\n", + "ylabel(\"-1/rA, hr.kg cat/mol\")\n", + "show()\n", + "XA[4] = 0.35\n", + "inv_rA[4] = 0.34;\n", + "Area = trapz(XA,inv_rA);\n", + "W = Area*2000.;\n", + "print \"Amount of catalyst needed is %.f kg cat\"%(W)\n", + "print ('The answer differs from those given in book as trapezoidal rule is used for calculating area')\n", + "\n", + "# Note : Answer differs because python trepz function works differnt than we do manually trepezoidal method." + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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hQ73Fe7t29o5ICMdVareVUoo2bdqwZ88eW8ZkNum2sp/8fFi0SO9sC3o8IyIC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\nOyIhhLA8SR4WtHcvDBkCTZr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+ "text": [ + "<matplotlib.figure.Figure at 0x7fa93d80a710>" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Amount of catalyst needed is 91 kg cat\n", + "The answer differs from those given in book as trapezoidal rule is used for calculating area\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 18.6 pageno : 416" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "XA = 0.35;\n", + "FAo = 2000. #mol/hr\n", + "CAo = 0.1 #mol/litre\n", + "eA = 3.\n", + "k = 96. # mol/kg cat\n", + "\n", + "# Calculations\n", + "CA = CAo*((1-XA)/(1+eA*XA))\n", + "rA = k*CA;\n", + "W = FAo*XA/rA;\n", + "\n", + "# Results\n", + "print \"The amount of catalyst neededkg, is %.f kg\"%(W)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "The amount of catalyst neededkg, is 230 kg\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch19.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch19.ipynb new file mode 100755 index 00000000..312fef16 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch19.ipynb @@ -0,0 +1,204 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 19 : The Packed Bed Catalytic Reactor" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 19.1 page no : 438" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "%matplotlib inline\n", + "\n", + "from matplotlib.pyplot import *\n", + "\n", + "# Variables\n", + "Cp = 40. #J/mol.k\n", + "Hr = 80000. #J/mol.k\n", + "FAo = 100. #mol/s\n", + "nA = 1.\n", + "nB = 7.\n", + "n = nA + nB\n", + "T1 = 300. #k\n", + "T2 = 600. #k\n", + "T3 = 800. #k\n", + "\n", + "# Calculations\n", + "m = Cp/Hr;\n", + "XA = [0.8,0.78,0.7,0.66,0.5,0.26,0.1,0];\n", + "inv_rA = [20,10,5,4.4,5,10,20,33];\n", + "\n", + "\n", + "plot(XA,inv_rA)\n", + "xlabel(\"Xa\")\n", + "ylabel(\"1/8 X 1/-rA\")\n", + "\n", + "print ('From the plot we can say that a recycle reactor should be used')\n", + "W = FAo*38.4\n", + "R = 1.;\n", + "Q1 = n*FAo*Cp*(T2-T1);\n", + "Q2 = n*FAo*Cp*(T1-T3);\n", + "\n", + "# Results\n", + "print \" The weight of catalyst needed is %.f kg\"%(W)\n", + "print \" The Recycle Ratio is %.f\"%(R)\n", + "print \" The heat exchange for feed is %.f MW\"%(Q1/10**6)\n", + "print \" The heat excahnge for the product is %.f MW\"%(Q2/10**6)\n", + "show()\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + "From the plot we can say that a recycle reactor should be used\n", + " The weight of catalyst needed is 3840 kg\n", + " The Recycle Ratio is 1\n", + " The heat exchange for feed is 10 MW\n", + " The heat excahnge for the product is -16 MW\n" + ] + }, + { + "output_type": "stream", + "stream": "stderr", + "text": [ + "WARNING: pylab import has clobbered these variables: ['draw_if_interactive']\n", + "`%pylab --no-import-all` prevents importing * from pylab and numpy\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x7ff34ba76ed0>" + ] + } + ], + "prompt_number": 4 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 19.2 page no : 440" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from matplotlib.pyplot import *\n", + "\n", + "# Variables\n", + "Cp = 40.\n", + "Hr = 80000.\n", + "m = Cp/Hr;\n", + "FAo = 100. #mol/s\n", + "print ('We should use a mixed flow reactor operating at optimum')\n", + "\n", + "# Calculations and Results\n", + "XA = [0.85,0.785,0.715,0.66,0.58,0.46];\n", + "inv_rAopt = [20,10,5,3.6,2,1];\n", + "plot(XA,inv_rAopt)\n", + "\n", + "area1 = 0.66*3.6;\n", + "area2 = (0.85-0.66)*20;\n", + "W1 = FAo*area1;\n", + "W2 = FAo*area2;\n", + "print \" The weight of catalyst needed for 1st bed is %.1f kg\"%(W1)\n", + "print \" The weight of catalyst needed for 2ndbed is %.1f kg\"%(W2)\n", + "\n", + "#Heat exchange\n", + "#For the first reactor\n", + "Q = (820-300)*Cp+0.66*(-Hr);\n", + "\n", + "#For 100 mol/s\n", + "Q1 = FAo*Q/10**6;#MW\n", + "print \" The amount of heat exchanged for 1st reactor is %.2f MW\"%(Q1)\n", + "\n", + "#For 2nd reactor\n", + "#To go from XA = 0.66 at 820 k to XA = 0.85 at 750 k\n", + "Q2 = FAo*((750-820)*Cp+(0.85-0.66)*(-Hr));\n", + "Q2 = Q2/10**6;\n", + "print \" The amount of heat exchanged for 2nd reactor is %.2f MW\"%(Q2)\n", + "\n", + "#For the exchanger needed to cool the exit stream from 750 k to 300 k\n", + "Q3 = FAo*Cp*(300. - 750);\n", + "Q3 = Q3/10**6;#MW\n", + "print \" The amount of heat exchanged for exchanger is %.2f MW\"%(Q3)\n", + "\n", + "show()\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "We should use a mixed flow reactor operating at optimum\n", + " The weight of catalyst needed for 1st bed is 237.6 kg" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "\n", + " The weight of catalyst needed for 2ndbed is 380.0 kg\n", + " The amount of heat exchanged for 1st reactor is -3.20 MW\n", + " The amount of heat exchanged for 2nd reactor is -1.80 MW\n", + " The amount of heat exchanged for exchanger is -1.80 MW\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x3959650>" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch2.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch2.ipynb new file mode 100755 index 00000000..70ba8482 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch2.ipynb @@ -0,0 +1,76 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 2 : Kinetics of Homogeneous Reactions" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 2.3 page no : 29" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "# Given\n", + "#t1 = 30 min ;T1 = 336 k;\n", + "#t2 = 15 sec ;T2 = 347 k;\n", + "# Converting t2 in min\n", + "t1 = 30. # milk heated (mins)\n", + "T1 = 336. # K based on t1\n", + "t2 = 0.25 # seconds \n", + "T2 = 347. # K based on t2\n", + "R = 8.314\n", + "\n", + "# Calculations\n", + "#math.log(t1/t2) = E(1/T1-1/T2)/R\n", + "E = (math.log(t1/t2)*R)/(1/T1-1/T2);\n", + "\n", + "# Results\n", + "print \"E is %d J/mol\"%(round(E,-3))\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "E is 422000 J/mol\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch20.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch20.ipynb new file mode 100755 index 00000000..9a87e997 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch20.ipynb @@ -0,0 +1,112 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 20 :\n", + "\n", + "Reactors with Suspended Solid \n", + "\n", + "Catalyst, Fluidized Reactors of \n", + "\n", + "Various Types" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 20.1 pageno : 460" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from numpy import linalg\n", + "\n", + "# Variables\n", + "uo = 0.3\n", + "umf = 0.03 #m/s\n", + "vo = 0.3*3.14159 #m3/s\n", + "d = 2. #m\n", + "db = 0.32; #dia of bubble(m)\n", + "emf = 0.5;\n", + "W = 7000. #kg\n", + "CAo = 100. #mol/m3\n", + "D = 20*10**-6; #m2/s\n", + "density = 2000. #kg/m3\n", + "k = 0.8;\n", + "alpha = 0.33;\n", + "g = 9.8\n", + "\n", + "# Calculations\n", + "#Using bubbling bed model\n", + "#Rise velocity of bubbles\n", + "ubr = 0.711*math.sqrt(g*db);\n", + "ub = uo-umf+ubr;\n", + "delta = uo/ub;\n", + "ef = 1-(1-emf)*(1-delta);\n", + "Kbc = 4.5*(umf/db)+5.85*(D**0.5)*(g**0.25)/(db**1.25);\n", + "Kce = 6.77*math.sqrt(emf*D*ubr/db**3);\n", + "fb = 0.001;\n", + "fc = delta*(1-emf)*((3*umf/emf)/(ubr-umf/emf)+alpha);\n", + "fe = (1-emf)*(1-delta)-fc-fb;\n", + "ft = fb+fe+fc;\n", + "A = 3.14*d*d/4;\n", + "Hbfb = W/((density*A)*(1-ef));\n", + "XA = 1- 0.6856948 #linalg.inv(math.exp(fb*k+(1/((1/(delta*Kbc))+1/((fc*k)+(1/((1/(delta*Kce))+(1/(fe*k)))))))*(Hbfb*ft/uo)/ft));\n", + "XA1 = 100*XA; #in percentage\n", + "\n", + "# Results\n", + "print \" Part a\"\n", + "print \" Conversion of reactant is %f \"%(XA1)\n", + "CA_avg = CAo*XA*vo*density/(k*W);\n", + "print \" Part b\"\n", + "print \" The proper mean concentratio (nmol/m3) of A seen by solid is %.f\"%(round(CA_avg))\n", + "XA1 = 1- 0.0511804 #linalg.inv(math.exp(k*ft*Hbfb/uo));\n", + "print \" Part c\"\n", + "print \" Conversion of reactant for packed bad is %f\"%(XA1)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " Conversion of reactant is 31.430520 \n", + " Part b\n", + " The proper mean concentratio (nmol/m3) of A seen by solid is 11\n", + " Part c\n", + " Conversion of reactant for packed bad is 0.948820\n" + ] + } + ], + "prompt_number": 9 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch21.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch21.ipynb new file mode 100755 index 00000000..2ca9ab81 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch21.ipynb @@ -0,0 +1,230 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 21 : The Rate and Performance Equations" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 21.1 page no : 486" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "%matplotlib inline\n", + "\n", + "import math \n", + "from numpy import *\n", + "from matplotlib.pyplot import *\n", + "from scipy import stats\n", + "\n", + "# Variables\n", + "t = [0,2,4,6]; # time\n", + "XA = [0.75,0.64,0.52,0.39]; # XA\n", + "t1 = 4000. #kg.s/m3\n", + "density_s = 1500. #kg/m3\n", + "De = 5.*10**-10;\n", + "d = 2.4*10**-3;\n", + "\n", + "# Calculations\n", + "y = zeros(4)\n", + "for i in range(4):\n", + " y[i] = math.log((1./(1-XA[i]))-1);\n", + "\n", + "plot(y,t)\n", + "ylabel(\"ln(CAO/CA -1)\")\n", + "\n", + "coeff = stats.linregress(t,y);\n", + "kd = coeff[0];\n", + "k = math.exp(coeff[1])/t1;\n", + "L = d/6;\n", + "Mt = L*math.sqrt(k*density_s/De);\n", + "#Assuming Runs were made in regime of strong resismath.tance to pore diffusion\n", + "\n", + "k1 = ((math.exp(coeff[1]))**2)*(L**2)*density_s/(t1*t1*De);\n", + "kd1 = -2*coeff[0];\n", + "Mt = L*math.sqrt(k1*density_s/De);\n", + "\n", + "# Results\n", + "print \" Rate equation in diffusion free regime with deactivation is %.2f m**3/kg.s\"%(k1)\n", + "print \" CA*a with -da/dthr-1 is %.2f a,hr**-1\"%(kd1)\n", + "\n", + "#In strong pore diffusion\n", + "k2 = k1*math.sqrt(De/(k1*density_s));\n", + "print \" CA*a**0.5/L with -da/dthr-1 is %.2f a,hr**-1\"%(kd1),\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + " Rate equation in diffusion free regime with deactivation is 0.27 m**3/kg.s\n", + " CA*a with -da/dthr-1 is 0.51 a,hr**-1\n", + " CA*a**0.5/L with -da/dthr-1 is 0.51 a,hr**-1\n" + ] + }, + { + "output_type": "stream", + "stream": "stderr", + "text": [ + "WARNING: pylab import has clobbered these variables: ['draw_if_interactive']\n", + "`%pylab --no-import-all` prevents importing * from pylab and numpy\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x7f7102416750>" + ] + } + ], + "prompt_number": 9 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 21.2 pageno : 492" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from scipy.integrate import quad \n", + "from matplotlib.pyplot import *\n", + "from numpy import *\n", + "\n", + "# Variables\n", + "PAo = 3. #atm\n", + "R = 82.06*10**-6 #m3.atm/mol.k\n", + "T = 730. #k\n", + "W = 1000. #kg\n", + "FAo = 5000. #mol/hr\n", + "\n", + "# Calculations\n", + "CAo = PAo/(R*T);\n", + "tau = W*CAo/FAo;\n", + "i = 0;\n", + "\n", + "a = zeros(25)\n", + "XA = zeros(25)\n", + "a1 = zeros(25)\n", + "XA1 = zeros(25)\n", + "a2 = zeros(25)\n", + "XA2 = zeros(25)\n", + "a3 = zeros(25)\n", + "XA3 = zeros(25)\n", + "a = linspace(0,120,25)\n", + "for t in xrange(0,120,5):\n", + " i = i+1;\n", + " #Part a\n", + " a[i] = 1-(8.3125*10**-3)*t;\n", + " XA[i] = (tau**2)*a[i]/(1+(tau**2)*a[i]);\n", + " #Part b\n", + " a1[i] = math.exp(-0.05*t);\n", + " XA1[i] = (tau**2)*a1[i]/(1+(tau**2)*a1[i]);\n", + " #Part c\n", + " a2[i] = 1/(1+3.325*t);\n", + " XA2[i] = (tau**2)*a2[i]/(1+(tau**2)*a2[i]);\n", + " #Part d\n", + " a3[i] = 1/(math.sqrt(1+1333*t));\n", + " XA3[i] = (tau**2)*a3[i]/(1+(tau**2)*a3[i]);\n", + "\n", + "t = linspace(0,120,25)\n", + "plot(t,XA,t,XA1,t,XA2,t,XA3)\n", + "suptitle(\"Decrease in conversion as a function of time for various deactivation orders.\")\n", + "xlabel(\"Time, days\")\n", + "ylabel(\"Xa\")\n", + "\n", + "def f13(t): \n", + "\t return ((100*(1-(8.3125*10**-3)*t))/(1+100*(1-(8.3125*10**-3)*t)))\n", + "\n", + "XA_avg = (1./120) * quad(f13,0,120)[0]\n", + "\n", + "\n", + "def f14(t): \n", + "\t return (100.*math.exp(-0.05*t))/(1+100*math.exp(-0.05*t))\n", + "\n", + "XA1_avg = (1./120)* quad(f14,0,120)[0]\n", + "\n", + "\n", + "def f15(t): \n", + "\t return ((100*(1./(1+3.325*t)))/(1+100*(1/(1+3.325*t))))\n", + "\n", + "XA2_avg = (1./120)* quad(f15,0,120)[0]\n", + "\n", + "\n", + "def f16(t): \n", + "\t return ((100*1./(math.sqrt(1+1333*t)))/(1+100*(1/math.sqrt(1+1333*t))))\n", + "\n", + "XA3_avg = (1./120)* quad(f16,0,120)[0]\n", + "\n", + "# Results\n", + "print \" for d = 0,the mean conversion is % f\"%(XA_avg)\n", + "print \" for d = 1,the mean conversion is % f\"%(XA1_avg)\n", + "print \" for d = 2,the mean conversion is % f\"%(XA2_avg)\n", + "print \" for d = 3,the mean conversion is % f\"%(XA3_avg)\n", + "\n", + "show()\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " for d = 0,the mean conversion is 0.955970\n", + " for d = 1,the mean conversion is 0.732280\n", + " for d = 2,the mean conversion is 0.400874\n", + " for d = 3,the mean conversion is 0.298840\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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UUzdnrZaL+cs9QKmInZur1K2TahxnB2fmdJ3D38/9zeYRmwHot6Yf7kvceXfv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\nlb9TUwsklWv/3969R0VZ7nsA/87lnQsXAUlAGW5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+ "text": [ + "<matplotlib.figure.Figure at 0x4215310>" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch22.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch22.ipynb new file mode 100755 index 00000000..ee78ccfc --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch22.ipynb @@ -0,0 +1,194 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 22 :\n", + "\n", + "G/L Reactions on Solid \n", + "\n", + "Catalysts: Trickle Beds, Slurry \n", + "\n", + "Reactors, and Three-Phase \n", + "\n", + "Fluidized Beds" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 22.1 pageno : 511" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "\n", + "# Variables\n", + "PA = 101325. #Pa\n", + "HA = 36845. #PA.m3.l/mol\n", + "CBo = 1000. #mol/m3\n", + "v = 10**-4 #m3*l/s\n", + "h = 5. #m\n", + "A = 0.1 #m2\n", + "\n", + "# Calculations\n", + "CA = PA/HA;\n", + "FBo = v*CBo;\n", + "Vr = A*h;\n", + "dp = 5*10**-3; #mcat\n", + "d_solid = 4500. #kg/m3cat\n", + "De = 8*10**-10; #m3l/mcat.s\n", + "n = 0.5;\n", + "b = 1.;\n", + "k = 2.35*10**-3;\n", + "L = dp/6.;\n", + "kai_overall = 0.02;\n", + "kac_ac = 0.05;\n", + "f = 0.6;\n", + "#For a half-order reaction\n", + "Mt = L*math.sqrt((n+1)*(k*d_solid*(CA)**(n-1))/(2*De));\n", + "E = 1/Mt;\n", + "rA = (1/((1/(kai_overall))+(1/(kac_ac))+(1/(k*b*(CA**(n-1))*E*f*d_solid))))*(PA/HA);\n", + "#From Material Balance\n", + "XB = b*rA*Vr/FBo;\n", + "\n", + "# Results\n", + "print \" The conversion of acetone is %.3f\"%(XB)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The conversion of acetone is 0.158\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 22.2 pageno : 513" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "%matplotlib inline\n", + "\n", + "import math \n", + "from matplotlib.pyplot import *\n", + "from numpy import *\n", + "\n", + "# Variables\n", + "PA = 14.6*101325; #Pa\n", + "HA = 148000.; # liquid\n", + "Vr = 2.;\n", + "Vl = Vr;\n", + "b = 1.;\n", + "fs = 0.0055;\n", + "\n", + "# Calculations\n", + "k = 5.*10**-5; #m6l/kg.molcat.s\n", + "dp = 5*10**-5; #mcat\n", + "kac = 4.4*10**-4;kai = 0.277; #m3l/m3.r.s\n", + "density = 1450.; #kg/m3\n", + "De = 5*10**-10; #m3l/mcat.s\n", + "L = dp/6; #for spherical particle\n", + "CA = PA/HA;\n", + "X = 0.9;\n", + "CBo = 2500.\n", + "CB = CBo*(1-X);\n", + "ac = 6*fs/dp;\n", + "K = kac*ac;\n", + "\n", + "CB = [2500,1000,250];\n", + "e = [0.19,0.29,0.5];\n", + "Mt = zeros(3)\n", + "rA = zeros(3)\n", + "inv_rA = zeros(3)\n", + "for i in range(3):\n", + " Mt[i] = L*math.sqrt(k*CB[i]*density/De);\n", + " rA[i] = CA/((1./kai)+(1./K)+(1./(k*density*e[i]*fs*CB[i])))\n", + " inv_rA[i] = 1/rA[i];\n", + "\n", + "# Results\n", + "plot(CB,inv_rA)\n", + "ylabel(\"1/-rA\")\n", + "Area = 3460.\n", + "t = Vl*Area/(b*Vr);\n", + "t = t/60. #min\n", + "print \" The time required for 90 percentage conversion of reactant is %.f\"%t,\n", + "print \"min\"\n", + "show()\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + " The time required for 90 percentage conversion of reactant is 58" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " min\n" + ] + }, + { + "output_type": "stream", + "stream": "stderr", + "text": [ + "WARNING: pylab import has clobbered these variables: ['draw_if_interactive', 'e']\n", + "`%pylab --no-import-all` prevents importing * from pylab and numpy\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x32eab90>" + ] + } + ], + "prompt_number": 4 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch23.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch23.ipynb new file mode 100755 index 00000000..5535664d --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch23.ipynb @@ -0,0 +1,104 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 23 :\n", + "\n", + "Fluid-Fluid Reactions: Kinetics" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 23.1 pageno : 536" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "\n", + "# Variables\n", + "k = 10.**6;\n", + "Kag_a = 0.01 #mol/hr. m**3. Pa\n", + "fl = 0.98;\n", + "Kal = 1.;\n", + "HA = 10.**5; # very low solubility\n", + "DAl = 10.**-6;\n", + "DBl = DAl;\n", + "PA = 5*10.**3 #Pa\n", + "CB = 100. #mol/m3\n", + "b = 2. \n", + "a = 20. #m2/m3\n", + "\n", + "# Calculations\n", + "Mh = math.sqrt(DAl*k*CB*CB)/Kal;\n", + "Ei = 1+(DBl*CB*HA/(b*DAl*PA));\n", + "E = 100.\n", + "print \" Part a\"\n", + "\n", + "res_total = (((1/(Kag_a))+(HA/(Kal*a*E))+(HA/(k*CB*CB*fl)))) #Total Resismath.tance\n", + "f_gas = (1/(Kag_a))/res_total; #fraction of resismath.tance in gas film\n", + "f_liq = (HA/(Kal*a*E))/res_total; #fraction of resismath.tance in liquid film\n", + "\n", + "\n", + "# Results\n", + "print \" Fraction of the resistance in the gas film is %f\"%(f_gas)\n", + "print \" Fraction of the resistance in the liquid film is %f\"%(f_liq)\n", + "print \" Part b\"\n", + "print \" The reaction zone is in the liquid film\"\n", + "print \" Part c\"\n", + "if Ei>5*Mh:\n", + " print \" We have pseudo 1st order reaction in the film\"\n", + "\n", + "rA = PA/(((1/(Kag_a))+(HA/(Kal*a*E))+(HA/(k*CB*CB*fl))));\n", + "print \" Part d\"\n", + "print \" The rate of reactionmol/m3.hr) is %f\"%(rA)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " Fraction of the resistance in the gas film is 0.666667\n", + " Fraction of the resistance in the liquid film is 0.333333\n", + " Part b\n", + " The reaction zone is in the liquid film\n", + " Part c\n", + " We have pseudo 1st order reaction in the film\n", + " Part d\n", + " The rate of reactionmol/m3.hr) is 33.333331\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch24.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch24.ipynb new file mode 100755 index 00000000..1766a982 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch24.ipynb @@ -0,0 +1,369 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 24 : Fluid-Fluid Reactors: Design" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 24.1 pageno : 551" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "kag_a = 0.32; # mol/hr.m**3 Pa\n", + "kal_a = 0.1 # hr\n", + "HA = 12.5 # Pa.m**3/mol\n", + "Fg = 10.**5 # mol/hr.m**2\n", + "Fl = 7.*10**5 # mol/hr.m**2\n", + "Ct = 56000.; #mol/m3\n", + "P = 10.**5; #Pa\n", + "\n", + "# Calculations\n", + "inv_Kag_a = 3.125+HA/(kal_a);\n", + "Gfilm_res = (3.125)/inv_Kag_a;\n", + "Lfilm_res = (HA/(kal_a))/inv_Kag_a;\n", + "Kag_a = 1/inv_Kag_a;\n", + "d = 20;\n", + "def f9(dp): \n", + "\t return 1./20\n", + "\n", + "h = (Fg/(P*Kag_a))* quad(f9,20,100)[0]\n", + "\n", + "# Results\n", + "print \" The height of the tower required for countercurrent operartions is %.1f \"%(h),\n", + "print \"m\"\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The height of the tower required for countercurrent operartions is 512.5 m\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 24.2 pageno : 554" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "Fg = 10.**5; \n", + "P = 10.**5;\n", + "Fg_by_Acs = 10.**5 #(Fg/Acs)\n", + "PA1 = 20;PA2 = 100.;\n", + "kag_a = 0.32;\n", + "\n", + "# Calculations\n", + "def f10(PA): \n", + "\t return 1./(0.32*PA)\n", + "\n", + "h = (Fg_by_Acs/P)* quad(f10,PA1,PA2)[0]\n", + "\n", + "# Results\n", + "print \" The height of the tower is %.2f \"%(h),\n", + "print \"m\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The height of the tower is 5.03 m\n" + ] + } + ], + "prompt_number": 4 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 24.3 pageno : 555" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "\n", + "# from example 24.2\n", + "Fg = 10.**5;\n", + "P = 10.**5;\n", + "PA1 = 20.\n", + "PA2 = 100.;\n", + "HA = 12.5;\n", + "kaga = 0.32\n", + "kla = 0.1;\n", + "\n", + "# Calculations\n", + "rA = 420./((1./kaga)+(HA/kla));\n", + "\n", + "def f8(PA): \n", + "\t return 1./rA\n", + "\n", + "h = (Fg/P)* quad(f8,PA1,PA2)[0]\n", + "\n", + "# Results\n", + "print \"The height of the tower is %.1f\"%(h),\n", + "print \"m\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "The height of the tower is 24.4 m\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 24.4 page no : 557" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "\n", + "# from example 24.2\n", + "PA1 = 20.\n", + "PA2 = 100. #Pa\n", + "Fg_by_Acs = 10.**5;\n", + "P = 10.**5;\n", + "HA = 12.5;\n", + "kaga = 0.32\n", + "kla = 0.1;\n", + "PA = 39.5 #Pa\n", + "\n", + "# Calculations\n", + "def f11(P): \n", + "\t return 1./(kaga*P)\n", + "\n", + "def f22(P):\n", + " return (1/kaga+HA/kla)/1620\n", + "\n", + "h = (Fg_by_Acs/P)*( quad(f11,PA1,PA)[0] + quad(f22,PA,PA2)[0])\n", + "\n", + "# Results\n", + "print \"The height of the tower is %.2f\"%(h),\n", + "print \"m\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "The height of the tower is 6.91 m\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 24.5 pageno : 558" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "\n", + "# from 24.2\n", + "Fg = 10.**5;\n", + "P = 10.**5;\n", + "Fg_by_Acs = 10.**5 #(Fg/Acs)\n", + "PA1 = 20.\n", + "PA2 = 100.\n", + "kag_a = 0.32;\n", + "\n", + "# Calculations\n", + "def f0(PA): \n", + "\t return 1./(PA/3.125)\n", + "\n", + "h = (Fg_by_Acs/P)* quad(f0,PA1,PA2)[0]\n", + "\n", + "# Results\n", + "print \" The height of the tower is %.2f \"%(h),\n", + "print \"m\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The height of the tower is 5.03 m\n" + ] + } + ], + "prompt_number": 8 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 24.6 pageno : 560" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "kag_a = 0.72; # mol/hr.m**3 Pa\n", + "kal_a = 144.; # hr**-1\n", + "HA = 1000.; # Pa m**3/mol\n", + "Fg = 9000. #mol/hr\n", + "fl = 0.9\n", + "b = 1\n", + "Vr = 1.62 #m3\n", + "DA = 3.6*10**-6 #m2/hr\n", + "a = 100. #m2/m3\n", + "k = 2.6*10**5; #m3/mol.hr\n", + "DB = DA\n", + "P = 10**5\n", + "PA = 1000. #Pa\n", + "kal = kal_a/a;\n", + "#At the start\n", + "CBo = 555.6;\n", + "\n", + "# Calculations\n", + "Mh = (math.sqrt(DB*k*CBo))/kal;\n", + "#Min value of EAi\n", + "Ei = 1+(CBo*HA/PA);\n", + "if Ei>Mh:\n", + " E = Mh;\n", + "\n", + "rA1 = PA/((P*Vr/Fg)+(1/kag_a)+(HA/(kal_a*E))+(HA/(k*fl*CBo)));\n", + "#At the end\n", + "CBf = 55.6;\n", + "Mh = (math.sqrt(DB*k*CBf))/kal;\n", + "#Min value of EAi\n", + "Ei = 1+(CBf*HA/PA);\n", + "if Ei>Mh:\n", + " E = Mh;\n", + "\n", + "rA2 = PA/((P*Vr/Fg)+(1/kag_a)+(HA/(kal_a*E))+(HA/(k*fl*CBf)));\n", + "#Average rate of reaction\n", + "rA_avg = (rA1+rA2)/2;\n", + "\n", + "def f7(CB): \n", + "\t return 1./rA_avg\n", + "\n", + "t = (fl/b)* quad(f7,CBf,CBo)[0]\n", + "\n", + "# Results\n", + "print \" Part a\"\n", + "print \" The run time needed is %.2f\"%t,\n", + "print \"hr\"\n", + "#The min time required is\n", + "tmin = Vr*(CBo-CBf)/(Fg*(PA/(P-PA)));\n", + "print \" The minimum time required is %.2f\"%(tmin),\n", + "print \"hr\"\n", + "#Fraction of reacmath.tant which passes through the math.tank unreacted is\n", + "f = (t-tmin)/tmin;\n", + "print \" Part b\"\n", + "print \" Fraction of reacmath.tant which passes through the math.tank unreacted is %.3f\"%(f)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " The run time needed is 9.13 hr\n", + " The minimum time required is 8.91 hr\n", + " Part b\n", + " Fraction of reacmath.tant which passes through the math.tank unreacted is 0.025\n" + ] + } + ], + "prompt_number": 11 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch26.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch26.ipynb new file mode 100755 index 00000000..cb1d9f92 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch26.ipynb @@ -0,0 +1,214 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 26 :\n", + "\n", + "Fluid-Particle Reactors: Design" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 26.1 pageno : 592" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "#Lets say F(Ri)/F = F_ri\n", + "\n", + "# Variables\n", + "F_50 = 0.3\n", + "F_100 = 0.4\n", + "F_200 = 0.3;\n", + "t_50 = 5.\n", + "t_100 = 10.\n", + "t_200 = 20.\n", + "tp = 8.\n", + "\n", + "# Calculations\n", + "a = ((1-(tp/t_50))**3)*F_50\n", + "b = ((1-(tp/t_100))**3)*F_100\n", + "c = ((1-(tp/t_200))**3)*F_200;\n", + "g = [a,b,c];\n", + "sum1 = 0;\n", + "for p in range(3):\n", + " if g[p]>0:\n", + " sum1 = sum1+g[p];\n", + "f_converted = 1-sum1;\n", + "\n", + "# Results\n", + "print \" The fraction of solid converted equals %.1f %%\"%(f_converted*100)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The fraction of solid converted equals 93.2 %\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 26.2 pageno : 597" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "t_avg = 60. # min\n", + "t = 20. #min\n", + "\n", + "# Calculations\n", + "unconverted = ((1./4)*(t/t_avg))-((1./20)*(t/t_avg)**2)+((1./120)*(t/t_avg)**3);\n", + "unconverted1 = ((1./5)*(t/t_avg))-((19./420)*(t/t_avg)**2)+((41./4620)*(t/t_avg)**3);\n", + "c_avg = (unconverted+unconverted1)/2;\n", + "\n", + "# Results\n", + "print \"Fraction of original sulfide ore remain unconverted is %.2f\"%(c_avg)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Fraction of original sulfide ore remain unconverted is 0.07\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 26.3 page no : 600" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "F = 1000. #gm/min\n", + "W = 10000. #gm\n", + "\n", + "# Calculations\n", + "t_avg = W/F;\n", + "F_50 = 300.\n", + "F_100 = 400.\n", + "F_200 = 300. #gm/min\n", + "t_50 = 5.\n", + "t_100 = 10.\n", + "t_200 = 20. #min\n", + "\n", + "unconverted = ((((1./4)*(t_50/t_avg))-((1./20)*(t_50/t_avg)**2)+ ((1./120)*(t_50/t_avg)**3))*(F_50/F))+((((1./4)*(t_100/t_avg))-((1./20)*(t_100/t_avg)**2)+((1./120)*(t_50/t_avg)**3))*(F_100/F))+((((1./4)*(t_200/t_avg))-((1./20)*(t_200/t_avg)**2)+((1./120) *(t_50/t_avg)**3))*(F_200/F))\n", + "converted = 1-unconverted;\n", + "\n", + "# Results\n", + "print \"The mean conversion of soild is %f\"%(converted)\n", + "print \" The answer slightly differs from those given in book as we have considered \\\n", + "only significant terms in infinite series\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "The mean conversion of soild is 0.795208\n", + " The answer slightly differs from those given in book as we have considered only significant terms in infinite series\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 26.4 pageno : 601" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "t1 = 1. #hr\n", + "t2 = t1/0.1 \n", + "a = 0.\n", + "r = 1 #ton/hr\n", + "# Calculations\n", + "while a<=1:\n", + " x = (1./4)*(a)-((1./20)*(a)**2)+((1./120)*(a)**3);\n", + " if x >0.099 and x<0.1005:\n", + " r = a;\n", + " a += .0001\n", + "\n", + "FBo = 1. #tons/hr\n", + "t_avg = t2/r;\n", + "W = t_avg*FBo;\n", + "\n", + "# Results\n", + "print \" The needed weight of bed is %.f\"%(W),\n", + "print \"tons\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The needed weight of bed is 23 tons\n" + ] + } + ], + "prompt_number": 7 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch29.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch29.ipynb new file mode 100755 index 00000000..be59a530 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch29.ipynb @@ -0,0 +1,93 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 29 :\n", + "\n", + "Substrate-Limiting\n", + "\n", + "Microbial Fermentation" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 29.3 pageno : 639" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "\n", + "# Variables\n", + "CAo = 6. # glucose solution\n", + "CM = 0.4 #kg/m3\n", + "V = 1. #m3\n", + "k = 4.\n", + "\n", + "# Calculations and Results\n", + "N = math.sqrt(1+(CAo/CM));\n", + "kt_op = N/(N-1);\n", + "C_by_A = 0.1;\n", + "t_op = kt_op/k;\n", + "v_op = V/t_op;\n", + "\n", + "#The feed rate of glumath.cose\n", + "FAo = v_op*CAo;\n", + "print \" The feed rate of glumath.cose is %.1f\"%(FAo) ,\n", + "print \"kg/hr\"\n", + "\n", + "#Max consumption rate of glumath.cose is\n", + "XA = N/(N+1);\n", + "c_max = FAo*XA;\n", + "print \" Max consumption rate of glumath.cose is %.1f \"%(c_max),\n", + "print \"kg/hr\"\n", + "\n", + "#Max production rate of E.coli is\n", + "Cc_op = (C_by_A)*CAo*N/(N+1);\n", + "Fcmax = v_op*Cc_op;\n", + "print \" Max production rate of E.coli is %.2f\"%(Fcmax),\n", + "print \"kg/hr\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The feed rate of glumath.cose is 18.0 kg/hr\n", + " Max consumption rate of glumath.cose is 14.4 kg/hr\n", + " Max production rate of E.coli is 1.44 kg/hr\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch3.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch3.ipynb new file mode 100755 index 00000000..4dda3df4 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch3.ipynb @@ -0,0 +1,256 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 3 : Interpretation of Batch Reactor Data" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 3.1 page no : 60" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "%matplotlib inline\n", + "\n", + "import math \n", + "from numpy import *\n", + "from matplotlib.pyplot import *\n", + "from scipy import stats\n", + "\n", + "# Variables\n", + "#Given\n", + "t = [0, 20, 40 ,60, 120 ,180, 300]; # time\n", + "C_A = [10 ,8, 6, 5, 3, 2, 1]; # concentration\n", + "CAo = 10.;\n", + "k = zeros(7)\n", + "CA_inv = zeros(7)\n", + "\n", + "# Calculations\n", + "#Guesmath.sing 1st order kinetics\n", + "for i in range(7):\n", + " k[i] = math.log(CAo/C_A[i]);\n", + " CA_inv[i] = 1/C_A[i];\n", + "\n", + "T = array([18.5,23,35]);\n", + "CAo = array([10,5,2]);\n", + "CA = zeros(3)\n", + "log_Tf = zeros(3)\n", + "log_CAo = zeros(3)\n", + "\n", + "for i in range(3):\n", + " CA[i] = 0.8*CAo[i];\n", + " log_Tf[i] = math.log10(T[i]);\n", + " log_CAo[i] = math.log10(CAo[i]);\n", + "\n", + "# Results\n", + "plot(log_CAo,log_Tf)\n", + "plot(log_CAo,log_Tf,\"go\")\n", + "xlabel(\"Ln CAO\")\n", + "ylabel(\"log r\")\n", + "#plot(log_Tf,log_CAo)\n", + "#coeff1 = linalg.lstsq(log_CAo,log_Tf);\n", + "slope, intercept, r_value, p_value, std_err = stats.linregress(log_CAo,log_Tf)\n", + "coeff1 = stats.linregress(log_CAo,log_Tf)\n", + "n = 1-coeff1[0];\n", + "print \"From graph we get slope and intercept for calculating rate eqn\"\n", + "k1 = ((0.8**(1-n))-1)*(10.**(1-n))/(18.5*(n-1));\n", + "print \" The rate equation is given by %.3f\"%(k1),\n", + "print \"CA**1.4 mol/litre.sec\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + "From graph we get slope and intercept for calculating rate eqn" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "\n", + " The rate equation is given by 0.005 CA**1.4 mol/litre.sec\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x33a3310>" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 3.2 page no : 65" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "%matplotlib inline\n", + "\n", + "import math\n", + "# Variables\n", + "CA = array([10,8,6,5,3,2,1]); # concentration\n", + "T = array([0,20,40,60,120,180,300]); # time\n", + "y = array([-0.1333,-0.1031,-0.0658,-0.0410,-0.0238,-0.0108,-0.0065]); # slope\n", + "\n", + "log_y = zeros(7)\n", + "log_CA = zeros(7)\n", + "\n", + "# Calculations\n", + "for i in range(7):\n", + " log_y[i] = log10(complex(y[i]));\n", + " log_CA[i] = log10(CA[i]);\n", + "\n", + "\n", + "# Results\n", + "plot(log_CA,log_y)\n", + "plot(log_CA,log_y,\"go\")\n", + "xlabel(\"log10 CA\")\n", + "ylabel(\"log10 (-dCA/dt)\")\n", + "show()\n", + "coeff1 = stats.linregress(log_CA,log_y);\n", + "n = coeff1[0];\n", + "k = -10**(coeff1[1]);\n", + "print \" After doing linear regression, the slope and intercept of the graph is %.0f, %.0f\"%(-coeff1[1],coeff1[0])\n", + "print \" The rate equation is therefore given by %.3f\"%(-k),\n", + "print \"CA**1.375 mol/litre.sec\"\n", + "print ('The answer slightly differs from those given in book as regress fn is used for \\\n", + " calculating slope and intercept')\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n" + ] + }, + { + "output_type": "stream", + "stream": "stderr", + "text": [ + "WARNING: pylab import has clobbered these variables: ['draw_if_interactive']\n", + "`%pylab --no-import-all` prevents importing * from pylab and numpy\n", + "-c:14: ComplexWarning: Casting complex values to real discards the imaginary part\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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jR1tRrriYzz6DO+6A996Du+6yuhqR+kWr3Ipb+fhjSEw0Fx688UarqxFxX1rl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\nunX89NNP7Nixg6KiIoKCgrj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+ "text": [ + "<matplotlib.figure.Figure at 0x365aa90>" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " After doing linear regression, the slope and intercept of the graph is 2, 1\n", + " The rate equation is therefore given by 0.005 CA**1.375 mol/litre.sec\n", + "The answer slightly differs from those given in book as regress fn is used for calculating slope and intercept\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 3.4 page no : 73" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "\n", + "# Variables\n", + "k1 = 2.3 # temperatures\n", + "k2 = 2.3\n", + "T1 = 400. # K\n", + "T2 = 500. # K\n", + "\n", + "# Calculations\n", + "R = 82.06*10**-6;\n", + "R1 = 8.314\n", + "E = (math.log(k2/k1)*R)/(1./T1-1./T2)\n", + "\n", + "# Results\n", + "print \"using pressure units is %.0f EJ/mol\"%(E)\n", + "\n", + "#pA = CA*RT\n", + "#-rA = 2.3(RT)**2*CA**2\n", + "k1 = 2.3*(R*T1)**2\n", + "k2 = 2.3*(R*T2)**2\n", + "E = (math.log(k2/k1)*R1)/(1./T1-1./T2)\n", + "print \"using concentration units is %.f J/mol\"%(E)\n", + "\n", + "# Answers might be different because of Rounding error" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "using pressure units is 0 EJ/mol\n", + "using concentration units is 7421 J/mol\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch30.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch30.ipynb new file mode 100755 index 00000000..2dd771a6 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch30.ipynb @@ -0,0 +1,90 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 30 :\n", + "\n", + "Product-Limiting Microbial \n", + "\n", + "Fermentation" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 30.1 pageno : 651" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "import math \n", + "\n", + "# Variables\n", + "k = math.sqrt(3) #hr**-1\n", + "n = 1.\n", + "V = 30. #m3\n", + "CR = 0.12 #kgalc/kgsol\n", + "density = 1000. #kg/m3\n", + "\n", + "# Calculations and Results\n", + "CR = CR*density;\n", + "CR_opt = CR/2;\n", + "alcohol_per = CR_opt*100/density #PErcentage of alcohol\n", + "\n", + "print \" The Percentage of alchol in cocktail is %f\"%(alcohol_per)\n", + "\n", + "kt = 1.\n", + "t = kt/k;\n", + "t_opt = 2*t;\n", + "v_opt = V/t_opt;\n", + "\n", + "print \" The Optimum feed rate is %f\"%(v_opt),\n", + "print \" m3/hr\"\n", + "\n", + "#The production rate of alcohol \n", + "FR = v_opt*CR_opt;\n", + "print \" The production rate of alcohol is %f \"%(FR),\n", + "print \" kgalc/hr\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The Percentage of alchol in cocktail is 6.000000\n", + " The Optimum feed rate is 25.980762 m3/hr\n", + " The production rate of alcohol is 1558.845727 kgalc/hr\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch4.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch4.ipynb new file mode 100755 index 00000000..cd660b67 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch4.ipynb @@ -0,0 +1,81 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 4 : Introduction to Reactor Design" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 4.1 page no : 88" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "a = 1.\n", + "b = 3.\n", + "c = 6.\n", + "#Initial concentrations\n", + "CAo = 100. # feed\n", + "CBo = 200. # feed\n", + "Cio = 100. # feed\n", + "#Final concentrations\n", + "CA = 40. # reacter exit\n", + "\n", + "# Calculations\n", + "# Find CB,XA,XB\n", + "ea = (6.-4.)/4;\n", + "XA = (CAo-CA)/(CAo+ea*CA);\n", + "eb = (ea*CBo)/(b*CAo);\n", + "XB = b*CAo*XA/CBo;\n", + "CB = CBo*(1-XB)/(1+eb*XB);\n", + "\n", + "# Results\n", + "print \"The final concentration of BCB is %.f\"%(CB)\n", + "print \" XA and XB are %.2f ,%.2f\"%(XA,XB)\n", + " \n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "The final concentration of BCB is 40\n", + " XA and XB are 0.50 ,0.75\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch5.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch5.ipynb new file mode 100755 index 00000000..2801cf57 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch5.ipynb @@ -0,0 +1,324 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 5 : Ideal Reactors for a Single Reaction" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 5.1 page no : 96" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "#Concentrations in mol/litre\n", + "CAo = 0.1 # liquid\n", + "CBo = 0.01 # liquid\n", + "Cco = 0. # liquid\n", + "CAf = 0.02 # outlet stream\n", + "CBf = 0.03 # outlet stream\n", + "Ccf = 0.04; # outlet stream\n", + "#Volume in litre\n", + "V = 1.;\n", + "#Volumetric flow rate(l/min)\n", + "v = 1.;\n", + "CA = CAf;CB = CBf;Cc = Ccf;\n", + "\n", + "# Calculations\n", + "#Rate of reaction(mol/litre.min)\n", + "rA = (CAo-CA)/(V/v);\n", + "rB = (CBo-CB)/(V/v);\n", + "rc = (Cco-Cc)/(V/v);\n", + "\n", + "# Results\n", + "print \"rate of reaction of A is %.2f mol/litre.min\"%(rA)\n", + "print \"rate of reaction of B is %.2f mol/litre.min\"%(rB)\n", + "print \"rate of reaction of C is %.2f mol/litre.min\"%(rc)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "rate of reaction of A is 0.08 mol/litre.min\n", + "rate of reaction of B is -0.02 mol/litre.min\n", + "rate of reaction of C is -0.04 mol/litre.min\n" + ] + } + ], + "prompt_number": 4 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 5.2 page no : 97" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "%matplotlib inline\n", + "\n", + "import math \n", + "from numpy import *\n", + "from matplotlib.pyplot import *\n", + "from scipy import stats\n", + "\n", + "# Variables\n", + "vo = array([10,3,1.2,0.5]) #Volumetric flow rates(litre/hr)\n", + "CA = array([85.7,66.7,50,33.4]) #Concentrations (millimol/litre)\n", + "CAo = 100.;\n", + "V = 0.1; #Volume(litre)\n", + "e = (1.-2.)/2; #Expansion factor is\n", + "#Initialization\n", + "XA = zeros(4);\n", + "rA = zeros(4);\n", + "m = zeros(4);\n", + "n = zeros(4);\n", + "\n", + "# Calculations\n", + "#Relation between concentration and conversion\n", + "for i in range(4):\n", + " XA[i] = (1-CA[i]/CAo)/(1+e*CA[i]/CAo);\n", + " rA[i] = vo[i]*CAo*XA[i]/V;\n", + " m[i] = math.log10(CA[i]);\n", + " n[i] = math.log10(rA[i]);\n", + "\n", + "# Results\n", + "#For nth order plot between n & m should give a straight line\n", + "plot(m,n)\n", + "xlabel(\"log CA\")\n", + "ylabel(\"log (-rA)\")\n", + "show()\n", + "coefs = stats.linregress(m,n);\n", + "print coefs\n", + "print \"Intercept of the graph is %.2f\"%(coefs[1])\n", + "print \"Slope of the graph is %.2f\"%(coefs[0])\n", + "k = 10**coefs[1]\n", + "n = coefs[0]\n", + "print \" Taking n = 2, rate of equation is %.2f millimol/litre.hr\"%(k),\n", + "print \"CA**2 \"\n", + "print ('The sol slightly differ from that given in book because regress fn is used to calculate the slope')\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n" + ] + }, + { + "output_type": "stream", + "stream": "stderr", + "text": [ + "WARNING: pylab import has clobbered these variables: ['rc', 'draw_if_interactive', 'e']\n", + "`%pylab --no-import-all` prevents importing * from pylab and numpy\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x29b4650>" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "(1.9569709616766851, -0.39508420521305565, 0.99852626739620765, 0.001473732603792355, 0.075209753597987913)\n", + "Intercept of the graph is -0.40\n", + "Slope of the graph is 1.96\n", + " Taking n = 2, rate of equation is 0.40 millimol/litre.hr CA**2 \n", + "The sol slightly differ from that given in book because regress fn is used to calculate the slope\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 5.3 page no : 99" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "'''\n", + "Note : The sol varies from book as the value of CB taken in book at end is wrong\n", + "'''\n", + "\n", + "import math \n", + "\n", + "# Variables\n", + "CAo = 1.4\n", + "CBo = 0.8\n", + "CRo = 0.\n", + "#Volume(litre)\n", + "V = 6.\n", + "\n", + "# Calculations\n", + "#For 75% conversion of B\n", + "#From stoichiometry of equation A+2B-->R\n", + "CA = 1.4-(0.75*0.8)/2.;\n", + "CB = 0.8-(0.75*0.8);\n", + "CR = (0.75*0.8)/2.;\n", + "#From the Given rate equation(mol/litre.min)\n", + "rB = 2*(12.5*CA*CB*CB-1.5*CR);\n", + "#Volumetric flow rate is given by\n", + "v = V*rB/(CBo-CB);\n", + "\n", + "# Results\n", + "print \" volumetric flow rate into and out of the reactor is %.1f litre/min\"%(v)" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " volumetric flow rate into and out of the reactor is 2.0 litre/min\n" + ] + } + ], + "prompt_number": 6 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 5.4 page no : 104" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "eA = (4-2.)/2;\n", + "CAo = 0.0625; # mol/liter\n", + "xAo = 0.\n", + "xAf = 0.8 # conversion\n", + "k = 0.01;\n", + "\n", + "# Calculations\n", + "def f1(xA): \n", + "\t return math.sqrt((1+xA)/(1-xA))\n", + "\n", + "X = quad(f1,xAo,xAf)[0]\n", + "t = math.sqrt(CAo)*X/k;\n", + "\n", + "# Results\n", + "print \" Space timesec needed is %.2f sec\"%(t)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Space timesec needed is 33.18 sec\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 5.5 page no : 106" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "T = 922. #Temperature(kelvin)\n", + "P = 460000.; # kPA\n", + "FAo = 40. # pure phosphine\n", + "k = 10.\n", + "R = 8.314;\n", + "\n", + "# Calculations\n", + "CAo = P/(R*T); # mol/m3\n", + "e = (7-4)/4.;\n", + "XA = 0.8;\n", + "\n", + "#The volume of plug flow reactor is given by\n", + "V = FAo*((1+e)*math.log(1./(1-XA))-e*XA)/(k*CAo);\n", + "\n", + "# Results\n", + "print \" volume of reactor is %.3f m**3\"%(V)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " volume of reactor is 0.148 m**3\n" + ] + } + ], + "prompt_number": 9 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch6.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch6.ipynb new file mode 100755 index 00000000..08544933 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch6.ipynb @@ -0,0 +1,233 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 6 : Design for Single Reactions" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 6.1 page no : 125" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "V1 = 50. # volume liters\n", + "V2 = 30. # volume liters\n", + "V3 = 40.; # volume liters\n", + "\n", + "# Calculations\n", + "VD = V1+V2;\n", + "VE = V3;\n", + "m = VE/VD\n", + "fr_D = 1./(1+m);\n", + "\n", + "# Results\n", + "print \" Fraction of feed going to branch D is %.3f \"%(fr_D)" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Fraction of feed going to branch D is 0.667 \n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 6.2 page no : 129" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "kCot = 90. # reactant\n", + "kCot = 180. \n", + "X = 97.4; # conversion\n", + "\n", + "print \" Part a\"\n", + "print \" The conversion in percentage is %.2f \"%(X)\n", + "#For 90% Conversion & N = 2.from graph\n", + "kCot = 27.5;\n", + "\n", + "# Calculations\n", + "ratio = 90*2/27.5;\n", + "\n", + "# Results\n", + "print \" Part b\"\n", + "print \" Treatment rate can be increased by %.1f \"%(ratio)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " The conversion in percentage is 97.40 \n", + " Part b\n", + " Treatment rate can be increased by 6.5 \n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 6.3 pageno : 144" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "%matplotlib inline\n", + "\n", + "import math \n", + "from numpy import *\n", + "from matplotlib.pyplot import *\n", + "\n", + "# Variables\n", + "CAo = array([2,5,6,6,11,14,16,24]); #mmol/m3\n", + "CA = array([0.5,3,1,2,6,10,8,4]) #mmol/m3\n", + "t = array([30,1,50,8,4,20,20,4]) #min\n", + "vo = 0.1 #m3/min\n", + "\n", + "# Calculations\n", + "inv_rA = zeros(8)\n", + "for i in range(8):\n", + " inv_rA[i] = t[i]/(CAo[i]-CA[i]);\n", + "\n", + "for i in range(8):\n", + " for j in range(i,8):\n", + " if CA[i]>CA[j]:\n", + " temp = CA[i];\n", + " CA[i] = CA[j];\n", + " CA[j] = temp;\n", + " temp1 = inv_rA[i];\n", + " inv_rA[i] = inv_rA[j];\n", + " inv_rA[j] = temp1;\n", + "\n", + "# Results\n", + "plot(CA,inv_rA)\n", + "plot(CA,inv_rA,\"go\")\n", + "suptitle(\"Arrangement with smallest volume\")\n", + "xlabel(\"CA, m mol/m**3\")\n", + "ylabel(\"-1/ra, m**3.min/m mol\")\n", + "print ('From the graph,we can see that we should use plug flow with recycle')\n", + "CAin = 6.6;#mmol/m3\n", + "R = (10-6.6)/(6.6-1);\n", + "#V = t*vo = area*vo\n", + "V = (10-1)*1.2*vo;\n", + "vr = vo*R;\n", + "print \" Part a\"\n", + "print \" The vol of reactor is %.2f m**3\"%(V)\n", + "print \" The recycle flow rate is %.4f \"%(vr),\n", + "print \"m3/min\"\n", + "\n", + "#Part b,from fig\n", + "t = (10-1)*10;\n", + "t1 = (10-2.6)*0.8;\n", + "t2 = (2.6-1)*10;\n", + "#For 1 math.tank\n", + "V = t*vo;\n", + "#For 2 math.tank\n", + "V1 = t1*vo;\n", + "V2 = t2*vo;\n", + "Vt = V1+V2;\n", + "print \" Part b\"\n", + "print \" For 1 tank volume is %.2f m**3\"%(V)\n", + "print \" For 2 tank the volume is %.2f m**3\"%(Vt)\n", + "\n", + "print \" Part c\"\n", + "print (' We should use mixed flow followed by plug flow')\n", + "#For MFR\n", + "tm = (10-4)*0.2;\n", + "Vm = tm*vo;\n", + "#For PFR\n", + "tp = 5.8;#by graphical integration\n", + "Vp = tp*vo;\n", + "Vtotal = Vp+Vm;\n", + "print \" For MFR volume is %.2f m**3\"%(Vm)\n", + "print \" For PFR volume is %.2f m**3\"%(Vp)\n", + "print \" Total volume is %.2f m**3\"%(Vtotal),\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + "From the graph,we can see that we should use plug flow with recycle\n", + " Part a\n", + " The vol of reactor is 1.08 m**3\n", + " The recycle flow rate is 0.0607 m3/min\n", + " Part b\n", + " For 1 tank volume is 9.00 m**3\n", + " For 2 tank the volume is 2.19 m**3\n", + " Part c\n", + " We should use mixed flow followed by plug flow\n", + " For MFR volume is 0.12 m**3\n", + " For PFR volume is 0.58 m**3\n", + " Total volume is 0.70 m**3\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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h4uICPz8/7baYmBi4urpCLpdDLpcjJSXFGKc2iC1/IiIjJf9p06bVSO4ymQx//etfkZOT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\nHjt2DPPmzcP169exbds2vPv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+ "text": [ + "<matplotlib.figure.Figure at 0x1e37810>" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch7.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch7.ipynb new file mode 100755 index 00000000..6785eea5 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch7.ipynb @@ -0,0 +1,233 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 7 : Design for Parallel Reactions" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 7.2 page no : 159" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "#Initial Concentration(mol/litre)eactant in combined feed\n", + "CAo = 10.\n", + "CBo = 10. \n", + "XA = 0.9; # conversion\n", + "CAf = CAo*(1-XA);\n", + "CA = CAf;\n", + "\n", + "# Calculations\n", + "def f4(CA): \n", + "\t return 1./(1+CA**0.5)\n", + "\n", + "Qp = (-1./(CAo-CAf))* quad(f4,CAo,CAf)[0]\n", + "\n", + "CRf = 9*Qp;\n", + "CSf = 9*(1-Qp)\n", + "# Results\n", + "print \" Part a\"\n", + "print \" For Plug Flow\"\n", + "print \" Concentration of R in the product stream is %.2f mol/litre\"%(CRf)\n", + "print \" Csf is %.2f mol/litre\"%(CSf)\n", + "\n", + "Qm = CA/(CA+CA**1.5);\n", + "CRf = 9*Qm;\n", + "Csf = 9*(1-Qm)\n", + "print \" Part b\"\n", + "print \" For Mixed Flow\"\n", + "print \" Concentration of R in the product stream is %.2f mol/litre \"%(CRf)\n", + "print \" Csf is %.2f mol/litre\"%(Csf)\n", + "\n", + "CAo = 19.\n", + "CB = 1;\n", + "\n", + "def f5(CA): \n", + "\t return CA/(CA+CB**1.5)\n", + "\n", + "Q = -1./(CAo-CAf)* quad(f5,CAo,CAf)[0]\n", + "CRf = 9*Q;\n", + "Csf = 9*(1-Q)\n", + "print \" Part c\"\n", + "print \" For Plug flow A Mixed flow B\"\n", + "print \" Concentration of R in the product stream is %.2f mol/litre\"%(CRf)\n", + "print \" Csf is %.2f mol/litre\"%(Csf)\n", + "print ('The result for plug flow varies as there seems to be typographical error in integration done in book')\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " For Plug Flow\n", + " Concentration of R in the product stream is 2.86 mol/litre\n", + " Csf is 6.14 mol/litre\n", + " Part b\n", + " For Mixed Flow\n", + " Concentration of R in the product stream is 4.50 mol/litre \n", + " Csf is 4.50 mol/litre\n", + " Part c\n", + " For Plug flow A Mixed flow B\n", + " Concentration of R in the product stream is 7.85 mol/litre\n", + " Csf is 1.15 mol/litre\n", + "The result for plug flow varies as there seems to be typographical error in integration done in book\n" + ] + } + ], + "prompt_number": 2 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 7.3 page no : 162" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "CAo = 2; # decomposition of A\n", + "CA = 0.5;\n", + "CAf = 0.;\n", + "\n", + "Csf = (CAo-CA)*2*CA/(1+CA)**2;\n", + "\n", + "print \" Part a\"\n", + "print \" For Mixed Flow Reactor\"\n", + "print \" Maximum expected Cs is %.3f\"%(Csf)\n", + "\n", + "# Calculations\n", + "def f12(CA): \n", + "\t return 2*CA/(1+CA)**2\n", + "\n", + "Csf = -1* quad(f12,CAo,CAf)[0]\n", + "\n", + "# Results\n", + "print \" Part b\"\n", + "print \" For Plug Flow\"\n", + "print \" Maximum expected concentration of S is %.3f \"%(Csf)\n", + "\n", + "CA = 1.;\n", + "Csf = (CAo-CA)*2*CA/(1+CA)**2;\n", + "\n", + "print \"Part c\"\n", + "print \" For MFR with separation and recycle\" \n", + "print \" Concentration of Csf is %.2f\"%(Csf)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " For Mixed Flow Reactor\n", + " Maximum expected Cs is 0.667\n", + " Part b\n", + " For Plug Flow\n", + " Maximum expected concentration of S is 0.864 \n", + "Part c\n", + " For MFR with separation and recycle\n", + " Concentration of Csf is 0.50\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 7.4 page no : 164" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "from scipy.integrate import quad \n", + "\n", + "# Variables\n", + "CAo = 2. # based on example 7.3\n", + "CA = 1.\n", + "Q = 0.5\n", + "\n", + "# Calculations\n", + "Cs1 = Q*(CAo-CA);\n", + "\n", + "def f6(CA): \n", + "\t return 2*CA/(1+CA)**2\n", + "\n", + "Cs2 = -1* quad(f6,1,0)[0]\n", + "\n", + "#Total amount of CS formed is\n", + "Cs = Cs1+Cs2;\n", + "\n", + "# Results\n", + "print \"Mixed flow followed by plug flow would be best\"\n", + "print \" Total amount of CS formed is %.3f mol/litre\"%(Cs)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Mixed flow followed by plug flow would be best\n", + " Total amount of CS formed is 0.886 mol/litre\n" + ] + } + ], + "prompt_number": 5 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [], + "prompt_number": 5 + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch8.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch8.ipynb new file mode 100755 index 00000000..c66d684b --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch8.ipynb @@ -0,0 +1,101 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 8 : Potpourri of Multiple Reactions" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 8.3 page no : 198" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "CAo = 185. \n", + "CA = 100.\n", + "t = 30.\n", + "\n", + "# Calculations\n", + "K123 = math.log(CAo/CA)/t;\n", + "m1 = 2.;\n", + "k2 = m1/CAo;\n", + "\n", + "##From the initial rate of formation of R\n", + "m2 = 1.3;\n", + "k1 = m2/CAo;\n", + "k3 = K123-k1-k2;\n", + "\n", + "k4 = 0.0001\n", + "while k4 <= 0.1:\n", + " Csmax = CAo*(k1/K123)*((K123/k4)**(k4/(k4-K123)));\n", + " if Csmax>31.8 and Csmax<32.2:\n", + " break\n", + " k4 += 0.0001\n", + " \n", + "k5 = 0.001\n", + "#similarly for T\n", + "while k5 <= 0.2:\n", + " Ctmax = CAo*(k3/K123)*((K123/k5)**(k5/(k5-K123)));\n", + " if Ctmax>9.95 and Ctmax<10.08:\n", + " break\n", + " k5 += .0001\n", + "\n", + "# Results\n", + "print \" The rate constants are\"\n", + "print \" k1 = %.4f min**-1\"%(k1)\n", + "print \" k2 = %.4f min**-1\"%(k2)\n", + "print \" k3 = %.4f min**-1\"%(k3)\n", + "print \" k4 = %.4f min**-1\"%(k4)\n", + "print \" k5 = %.4f min**-1\"%(k5)\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The rate constants are\n", + " k1 = 0.0070 min**-1\n", + " k2 = 0.0108 min**-1\n", + " k3 = 0.0027 min**-1\n", + " k4 = 0.0099 min**-1\n", + " k5 = 0.0157 min**-1\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
\ No newline at end of file diff --git a/Chemical_Reaction_Engineering_by_O._Levenspiel/ch9.ipynb b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch9.ipynb new file mode 100755 index 00000000..17320691 --- /dev/null +++ b/Chemical_Reaction_Engineering_by_O._Levenspiel/ch9.ipynb @@ -0,0 +1,405 @@ +{ + "metadata": { + "name": "" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 9 : Temperature and Pressure Effects" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.1 page no : 209" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables\n", + "CpA = 35. # j/mol.K\n", + "CpB = 45. # j/mol.K\n", + "CpR = 70. # j/mol.K\n", + "T1 = 25. # C\n", + "T2 = 1025. # C\n", + "Hr = -50000.\n", + "\n", + "# Calculations\n", + "#Enthalpy balance for 1mol A,1 mol B,2 mol R\n", + "nA = 1.\n", + "nB = 1.\n", + "nR = 2.\n", + "dH = nA*CpA*(T1-T2)+nB*CpB*(T1-T2)+(Hr)+nR*CpR*(T2-T1);\n", + "\n", + "# Results\n", + "print \" dHJ at temperature 1025C is %.f \"%(dH)\n", + "if dH>0 :\n", + " print \"Reaction is Exothermic\"\n", + "else:\n", + " print \"Reaction is endothermic at 1025OC\"\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " dHJ at temperature 1025C is 10000 \n", + "Reaction is Exothermic\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.2 page no : 213" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "%matplotlib inline\n", + "\n", + "import math \n", + "from matplotlib.pyplot import *\n", + "from numpy import *\n", + "\n", + "Ho = -75300. # J/mol\n", + "Go = -14130. # J/mol\n", + "R = 8.3214\n", + "T1 = 298.\n", + "\n", + "# Calculations\n", + "#With all specific heais alike,dCp = 0\n", + "Hr = -Ho;\n", + "K298 = math.exp(-Go/(R*T1));\n", + "\n", + "\n", + "#Taking different values of T\n", + "T1 = array([2,15,25,35,45,55,65,75,85,95]) #degree celcius\n", + "T = array([278,288,298,308,318,328,338,348,358,368]) #kelvin\n", + "\n", + "XAe = zeros(10)\n", + "\n", + "for i in range(10):\n", + " K = K298*math.exp((Hr/R)*((1./T[i])-(1./298)));\n", + " XAe[i] = K/(K+1);\n", + "\n", + "# Results\n", + "plot(T1,XAe)\n", + "xlabel(\"Temperature, C\")\n", + "ylabel(\"XAe\")\n", + "print (\" From the graph we see temp must stay below 78 C if conversion of 75% or above is expected\")\n", + "show()\n", + "\n", + "\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Populating the interactive namespace from numpy and matplotlib\n", + " From the graph we see temp must stay below 78 C if conversion of 75% or above is expected" + ] + }, + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "\n" + ] + }, + { + "output_type": "stream", + "stream": "stderr", + "text": [ + "WARNING: pylab import has clobbered these variables: ['draw_if_interactive']\n", + "`%pylab --no-import-all` prevents importing * from pylab and numpy\n" + ] + }, + { + "metadata": {}, + "output_type": "display_data", + "png": 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+ "text": [ + "<matplotlib.figure.Figure at 0x31ac650>" + ] + } + ], + "prompt_number": 8 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.3 page no : 217" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "import math \n", + "\n", + "# Variables \n", + "\n", + "# from example 9.2\n", + "XA = 0.581; \n", + "t = 1. #min\n", + "XAe = 0.89;\n", + "XAe1 = 0.993;\n", + "T1 = 338.\n", + "T2 = 298.\n", + "R = 8.314\n", + "\n", + "\n", + "# Calculations\n", + "k1_338 = -(XAe/t)*math.log(1-(XA/XAe));\n", + "XA1 = 0.6;\n", + "t1 = 10. #min\n", + "\n", + "k1_298 = -(XAe1/t1)*math.log(1-(XA1/XAe1));\n", + "E1 = (R*math.log(k1_338/k1_298))*(T1*T2)/(T1-T2)\n", + "ko = k1_338/(math.exp(-E1/(R*T1)))\n", + "\n", + "# Results\n", + "print \" The rate constants are k = exp[75300/RT-24.7] min-1\"\n", + "print \" k1 = exp[17.2-48900/RT] min-1\"\n", + "print \" k2 = exp[41.9-123800/RT] min-1 \"\n", + "print \" E1 = %.2f\"%E1\n", + "print \" K0 = %.2f\"%ko" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The rate constants are k = exp[75300/RT-24.7] min-1\n", + " k1 = exp[17.2-48900/RT] min-1\n", + " k2 = exp[41.9-123800/RT] min-1 \n", + " E1 = 48679.81\n", + " K0 = 31411847.30\n" + ] + } + ], + "prompt_number": 3 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.4 page no : 229" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "CAo = 4. #mol/litre\n", + "FAo = 1000. #mol/min\n", + "A = 0.405 #litre/mol.min\n", + "\n", + "# Calculations\n", + "t = CAo*A;\n", + "V = FAo*A;\n", + "\n", + "# Results\n", + "print \" Part a\"\n", + "print \" The space time needed is %.2f min\"%(t)\n", + "print \" The Volume needed is %.f litres\"%(V)\n", + "\n", + "\n", + "# Note : We do not have value of 'rA'. so part B can not be calculated and plotted" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " The space time needed is 1.62 min\n", + " The Volume needed is 405 litres\n" + ] + } + ], + "prompt_number": 10 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.5 pageno : 231" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "CAo = 4. # mol/liter\n", + "FAo = 1000. # mol/min\n", + "XA = 0.8; # %\n", + "Cp = 250. #cal/molA.K\n", + "Hr = 18000. #cal/molA\n", + "rA = 0.4;\n", + "\n", + "# Calculations and Results\n", + "V = FAo*XA/rA;\n", + "\n", + "print \" Part a\"\n", + "print \" The size of reactorlitres) needed is %.f litres\"%(V)\n", + "\n", + "slope = Cp/Hr;\n", + "#Using graph\n", + "Qab1 = Cp*20; #cal/molA\n", + "Qab = Qab1*1000; #cal/min\n", + "Qab = Qab*0.000070; #KW\n", + "\n", + "print \" Part b\"\n", + "print \" Heat Duty of precooler is %.2f kW\"%(Qab)\n", + "\n", + "Qce1 = Cp*37; #cal/molA fed\n", + "Qce = Qce1*1000; #cal/min\n", + "Qce = Qce*0.000070; #KW\n", + "\n", + "print \" Heat Duty of postcooler is %.2f kW\"%(Qce)\n", + "\n", + "# answers may vary because of rounding error." + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " Part a\n", + " The size of reactorlitres) needed is 2000 litres\n", + " Part b\n", + " Heat Duty of precooler is 350.00 kW\n", + " Heat Duty of postcooler is 647.50 kW\n" + ] + } + ], + "prompt_number": 10 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.6 pageno : 233" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "FAo = 1000. #mol/min\n", + "Area = 1.72;\n", + "\n", + "# Calculations\n", + "V = FAo*Area;\n", + "\n", + "# Results\n", + "print \" The volume of adiabatic plug flow reactor is %.f litres\"%(V),\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The volume of adiabatic plug flow reactor is 1720 litres\n" + ] + } + ], + "prompt_number": 12 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Example 9.7 page no : 234" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "# Variables\n", + "FAo = 1000. #mol/min\n", + "Area = (0.8-0)*1.5;\n", + "\n", + "# Calculations\n", + "V = FAo*Area;\n", + "\n", + "# Results\n", + "print \" The volume required is %.f litres\"%(V),\n" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + " The volume required is 1200 litres\n" + ] + } + ], + "prompt_number": 13 + }, + { + "cell_type": "code", + "collapsed": false, + "input": [], + "language": "python", + "metadata": {}, + "outputs": [] + } + ], + "metadata": {} + } + ] +}
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