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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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+ "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": {} + } + ] +}
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