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author: Thomas Stephen Lee 2015-09-04 22:04:10 +0530
committer: Thomas Stephen Lee 2015-09-04 22:04:10 +0530
commit: 41f1f72e9502f5c3de6ca16b303803dfcf1df594 (patch)
tree: f4bf726a3e3ce5d7d9ee3781cbacfe3116115a2c /Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel
parent: 9c9779ba21b9bedde88e1e8216f9e3b4f8650b0e (diff)
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diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/README.txt b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/README.txt
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+Contributed By: Dolar Khachariya
+Course: mtech
+College/Institute/Organization: Indian Institute of Engineering Bombay
+Department/Designation: Electrical engineering
+Book Title: Fluidization Engineering
+Author: K. Daizo And O. Levenspiel
+Publisher: Butterworth-Heinemann, Massachusetts
+Year of publication: 1991
+Isbn: 8131200353
+Edition: 2nd
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch10.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch10.ipynb
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+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:89c91579d721ed0f833b399593203d4eb19421ab1695bc830f1be612e46bd826"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 10 : Gas Dispersion and Gas Interchange in Bubbling Beds"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "%matplotlib inline"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Welcome to pylab, a matplotlib-based Python environment [backend: module://IPython.zmq.pylab.backend_inline].\n",
+        "For more information, type 'help(pylab)'.\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 253\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "from numpy import *\n",
+      "%matplotlib inline\n",
+      "#Variable declaration\n",
+      "umf=[0.01,0.045];     #Velocity at minimum fluidization condition in m/s\n",
+      "ephsilonmf=[0.5,0.5]; #Void fraction at minimum fluidization condition\n",
+      "D=[2E-5,7E-5];        #Diffusion coefficient of gas in m**2/s\n",
+      "g=9.81;               #Acceleration due to gravity in m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "db=[5.,10.,15.,20.];\n",
+      "n=len(umf);\n",
+      "m=len(db)\n",
+      "Kbc = zeros((n,m))\n",
+      "Kce = zeros((n,m))\n",
+      "Kbe = zeros((n,m))\n",
+      "    \n",
+      "for i in range(n):\n",
+      "    for j in range(m):\n",
+      "            Kbc[i][j]=4.5*(umf[i]/db[j])+5.85*((D[i]**0.5*g**0.25)/db[j]**(5.0/4));#Gas interchange coefficient between bubble and cloud from Eqn.(27)\n",
+      "            Kce[i][j]=6.77*((D[i]*ephsilonmf[i]*0.711*(g*db[j])**0.5)/db[j]**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(34)\n",
+      "            Kbe[i][j]=(Kbc[i][j]*Kce[i][j])/(Kbc[i][j]+Kce[i][j]);#Gas interchange coefficient between bubble and emulsion from Eqn.(14)\n",
+      "\n",
+      "#OUTPUT\n",
+      "i=0;\n",
+      "j=0;\n",
+      "k=0;\n",
+      "while k<m*n:\n",
+      "    print '\\t\\tKbc for fine particles and He',\n",
+      "    print '\\tKbc for coarse particles and ozone',\n",
+      "    print '\\tKbe for fine particles and He',\n",
+      "    print '\\tKbe for coarse particles and ozone'\n",
+      "    j = 0\n",
+      "    while j<m:\n",
+      "        print 'db=%fm'%(db[j]*10**-2);\n",
+      "        while i<n:\n",
+      "            print '\\t%f'%Kbc[i][j],\n",
+      "            print '\\t\\t\\t%f'%Kbe[i][j],\n",
+      "            i=i+1;   \n",
+      "            k=k+1;\n",
+      "            print '\\t\\t\\t',\n",
+      "        i=0;\n",
+      "        j=j+1;\n",
+      "import numpy\n",
+      "import matplotlib.pyplot as plt\n",
+      "a = numpy.matrix(Kbe)\n",
+      "b = numpy.matrix(Kbc)\n",
+      "db = array(db).T\n",
+      "Kbe=a.T\n",
+      "Kbc=b.T\n",
+      "\n",
+      "plt.plot(db,Kbc,db,Kbe)\n",
+      "#plt.plot(db,Kbe);\n",
+      "#Note : Python does not have plot2d function. so we can plot it \n",
+      "#plt.title('Plot of Kbc,Kbe vs db','db');\n",
+      "plt.show()\n",
+      "print 'Comparing the points with the plot of Kbc,Kbe vs db in Fig.(12), we can conlcude the following:'\n",
+      "print 'Kbc for fine particles and helium: line 2 in Fig.(12)'\n",
+      "print 'Kbc for coarser particles and ozone: line 3 in Fig.(12)'\n",
+      "print 'Kbe for fine particles and helium: line 4 in Fig.(12)'\n",
+      "print 'Kbe for coarser particles and ozone: line 5 in Fig.(12)'\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Welcome to pylab, a matplotlib-based Python environment [backend: module://IPython.zmq.pylab.backend_inline].\n",
+        "For more information, type 'help(pylab)'.\n"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\t\tKbc for fine particles and He \tKbc for coarse particles and ozone \tKbe for fine particles and He \tKbe for coarse particles and ozone\n",
+        "db=0.050000m\n",
+        "\t0.015193 \t\t\t0.003335 \t\t\t\t0.052085 \t\t\t0.006930 \t\t\tdb=0.100000m\n",
+        "\t0.007104 \t\t\t0.001434 \t\t\t\t0.025121 \t\t\t0.002964 \t\t\tdb=0.150000m\n",
+        "\t0.004568 \t\t\t0.000875 \t\t\t\t0.016434 \t\t\t0.001803 \t\t\tdb=0.200000m\n",
+        "\t0.003345 \t\t\t0.000616 \t\t\t\t0.012173 \t\t\t0.001266 \t\t\t"
+       ]
+      },
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": 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dO2fNAg4cEE/b8IMfAL/+tXgiN4NB6rREZOu6XLMPDAzErl274OnpiYiICJw8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\nRU5ErkJggg==\n"
+      },
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Comparing the points with the plot of Kbc,Kbe vs db in Fig.(12), we can conlcude the following:\n",
+        "Kbc for fine particles and helium: line 2 in Fig.(12)\n",
+        "Kbc for coarser particles and ozone: line 3 in Fig.(12)\n",
+        "Kbe for fine particles and helium: line 4 in Fig.(12)\n",
+        "Kbe for coarser particles and ozone: line 5 in Fig.(12)\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 254\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "D=0.69;         #Diffusion coefficient of gas in cm**2/s\n",
+      "umf=1.0;        #Velocity at minimum fluidization condition in cm/s\n",
+      "ephsilonmf=0.5; #Void fraction at minimum fluidization condition\n",
+      "db=[5,15];      #Equilibrium bubble size in cm\n",
+      "g=980;          #Acceleration due to gravity in cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(db);\n",
+      "i=0;\n",
+      "Kbc = [0.,0.]\n",
+      "Kce = [0.,0.]\n",
+      "Kbe = [0.,0.]\n",
+      "e = [0.,0.]\n",
+      "while i<n:\n",
+      "    Kbc[i]=4.5*(umf/db[i])+5.85*((D**0.5*g**0.25)/db[i]**(5/4));#Gas interchange coefficient between bubble and cloud from Eqn.(27)\n",
+      "    Kce[i]=6.77*((D*ephsilonmf*0.711*(g*db[i])**0.5)/db[i]**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(34)\n",
+      "    Kbe[i]=(Kbc[i]*Kce[i])/(Kbc[i]+Kce[i]);#Gas interchange coefficient between bubble and emulsion from Eqn.(14)\n",
+      "    e[i]=(Kce[i]-Kbe[i])/Kbe[i];#Error when minor resistance is ignored\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'db(cm)',\n",
+      "print '\\t\\tCalculated Kbc',\n",
+      "print '\\tCalculated Kce',\n",
+      "print '\\t\\tKbe from Eqn.(14)',\n",
+      "print '\\tErron when minor resistance is ignored (in percentage)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%db[i],\n",
+      "    print '\\t%f'%Kbc[i],\n",
+      "    print '\\t%f'%Kce[i],\n",
+      "    print '\\t\\t%f'%Kbe[i],\n",
+      "    print '\\t\\t%f'%(e[i]*100);\n",
+      "    i=i+1;   \n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "db(cm) \t\tCalculated Kbc \tCalculated Kce \t\tKbe from Eqn.(14) \tErron when minor resistance is ignored (in percentage)\n",
+        "5.000000 \t6.337721 \t2.509152 \t\t1.797506 \t\t39.590766\n",
+        "15.000000 \t2.112574 \t0.635514 \t\t0.488547 \t\t30.082477\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 255\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "Kbe=[0.028,0.05];  #Reported range for gas interchange coefficient between bubble and emulsion\n",
+      "uo=0.30;           #Superficial gas velocity in m/s\n",
+      "db=0.13;           #Equilibrium bubble size in m\n",
+      "m=7;\n",
+      "ephsilonmf=0.5;    #Void fraction at minimum fluidization condition\n",
+      "umf=0.0018;        #Velocity at minimum fluidization condition in m/s\n",
+      "D=[9E-6,22E-6];    #Diffusion coefficient of gas in m**2/s\n",
+      "g=9.81;            #Acceleration due to gravity in m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(Kbe);\n",
+      "i=0;\n",
+      "Kbem = [0,0]\n",
+      "Kbc = [0,0]\n",
+      "Kce = [0,0]\n",
+      "#Kbe = [0,0]\n",
+      "c = [0,0]\n",
+      "\n",
+      "while i<n:\n",
+      "    Kbem[i]=(6.0/db)*Kbe[i];#Gas interchange coefficient between bubble and emulsion from Eqn.(19)\n",
+      "    Kbc[i]=4.5*(umf/db)+5.85*((D[i]**0.5*g**0.25)/db**(5.0/4));#Gas interchange coefficient between bubble and cloud from Eqn.(27)\n",
+      "    Kce[i]=6.77*((D[i]*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(34)\n",
+      "    Kbe[i]=(Kbc[i]*Kce[i])/(Kbc[i]+Kce[i]);#Gas interchange coefficient between bubble and emulsion from Eqn.(14)\n",
+      "    c[i]=(Kbem[i]/Kbe[i]);\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Kbe from Eqn.(19)',\n",
+      "print '\\tKbc from Eqn.(27)',\n",
+      "print '\\tKce from Eqn.(34)',\n",
+      "print '\\tKbe from Eqn.(14)',\n",
+      "print '\\tComparison of Kbe from Eqn.(19) and that from Eqn.(14)'\n",
+      "i=0\n",
+      "while i<n:\n",
+      "    print '%f'%Kbem[i],\n",
+      "    print '\\t\\t%f'%Kbc[i],\n",
+      "    print '\\t\\t%f'%Kce[i],\n",
+      "    print '\\t\\t%f'%Kbe[i],\n",
+      "    print '\\t\\t%f'%c[i]\n",
+      "    i=i+1;   \n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Kbe from Eqn.(19) \tKbc from Eqn.(27) \tKce from Eqn.(34) \tKbe from Eqn.(14) \tComparison of Kbe from Eqn.(19) and that from Eqn.(14)\n",
+        "1.292308 \t\t0.460200 \t\t0.274548 \t\t0.171959 \t\t7.515188\n",
+        "2.307692 \t\t0.684401 \t\t0.429248 \t\t0.263797 \t\t8.747978\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch11.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch11.ipynb
new file mode 100755
index 00000000..48b679d6
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch11.ipynb
@@ -0,0 +1,356 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:69d28aca1d8ec525f15842df275d6e6c6108139c968df651029692a500222ce7"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter  11  : Particle to Gas Mass and Heat Transfer"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "%matplotlib inline"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Welcome to pylab, a matplotlib-based Python environment [backend: module://IPython.zmq.pylab.backend_inline].\n",
+        "For more information, type 'help(pylab)'.\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 265\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "db=0.37;         #Equilibrium bubble size in cm\n",
+      "dp=0.028;        #Particle size in cm\n",
+      "rhos=1.06;       #Density of solids in g/cc\n",
+      "ephsilonmf=0.5;  #Void fraction at minimum fluidization condition\n",
+      "phis=0.4;        #Sphericity of solids\n",
+      "gammab=0.005;    #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "rhog=1.18E-3;    #Density of air in g/cc\n",
+      "myu=1.8E-4;      #Viscosity of gas in g/cm s\n",
+      "D=0.065;         #Diffusion coefficient of gas in cm**2/s\n",
+      "Sc=2.35;         #Schmidt number\n",
+      "etad=1;          #Adsorption efficiency factor\n",
+      "y=1;\n",
+      "umf=1.21;        #Velocity at minimum fluidization condition in cm/s\n",
+      "ut=69;           #Terminal velocity in cm/s\n",
+      "g=980;           #Acceleration due to gravity in square cm/s**2\n",
+      "uo=[10,20,30,40,50];#Superficial gas velocity in cm/s\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(uo);\n",
+      "i=0;\n",
+      "Rept=(dp*ut*rhog)/myu;\n",
+      "Shstar=2+(0.6*(Rept**0.5)*(Sc**(1/3)));#Sherwood no. from Eqn.(1)\n",
+      "Kbc=4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of the bubble\n",
+      "x = [0,0,0,0,0]\n",
+      "Shbed = [0,0,0,0,0]\n",
+      "Rep = [0,0,0,0,0]\n",
+      "while i<n:\n",
+      "    x[i]=(uo[i]-umf)/(ubr*(1-ephsilonmf));#The term delta/(1-epshilonf) after simplification\n",
+      "    Shbed[i]=x[i]*((gammab*Shstar*etad)+((phis*dp**2*y)/(6*D))*Kbc);#Sherwood no. from Eqn.(11)\n",
+      "    Rep[i]=(dp*uo[i]*rhog)/myu;#Reynolds of the particle\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The desired result is the relationship between Shbed and Rep  The points gives a straight line of the form y=mx+c'\n",
+      "print 'Rep',\n",
+      "print '\\t\\tShbed'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%Rep[i],\n",
+      "    print '\\t%f'%Shbed[i]\n",
+      "    i=i+1;\n",
+      "import matplotlib.pyplot as plt\n",
+      "plt.plot(Rep,Shbed);\n",
+      "plt.xlabel(\"Rep\");\n",
+      "plt.ylabel(\"Shbed\");\n",
+      "\n",
+      "plt.show()"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Populating the interactive namespace from numpy and matplotlib\n",
+        "The desired result is the relationship between Shbed and Rep  The points gives a straight line of the form y=mx+c\n",
+        "Rep \t\tShbed\n",
+        "1.835556 \t0.065762\n",
+        "3.671111 \t0.140576\n",
+        "5.506667 \t0.215391\n",
+        "7.342222 \t0.290206\n",
+        "9.177778 \t0.365020\n"
+       ]
+      },
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": 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RlJR0Rnn9weLFMHEijB5t3b+hXTu7E4mIPygsLKSwsPCMx3u9QDjOYjLck7HH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\niDRIBUJERBqkAiEiIg36/9fGcNvjU2I2AAAAAElFTkSuQmCC\n",
+       "text": [
+        "<matplotlib.figure.Figure at 0x2b26690>"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 267"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "\n",
+      "#INPUT\n",
+      "umf=0.12            #Velocity at minimum fluidization condition in cm/s\n",
+      "uo=40.;              #Superficial gas velocity in cm/s\n",
+      "ub=120;             #Velocity of the bubble in cm/s\n",
+      "D=0.7;              #Diffusion coefficient of gas in cm**2/s\n",
+      "abkbe1=1.;           #Bubble-emuslion interchange coefficient for non absorbing particles(m=0)\n",
+      "abkbe2=18.;          #Bubble-emuslion interchange coefficient for highly absorbing particles(m=infinity)\n",
+      "g=980.;              #Acceleration due to gravity in square cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "#For non absorbing particles m=0,etad=0\n",
+      "Kbc=(ub/uo)*(abkbe1);\n",
+      "dbguess=2;#Guess value of db\n",
+      "def solver_func(db):        #Function defined for solving the system\n",
+      "    return abkbe1-(uo/ub)*(4.5*(umf/db)+5.85*(D**0.5*g**0.25)/(db**(5/4.)));#Eqn.(10.27)\n",
+      "\n",
+      "d=fsolve(solver_func,dbguess)\n",
+      "#For highly absorbing particles m=infinity, etad=1\n",
+      "M=abkbe2-(uo/ub)*Kbc;\n",
+      "#For intermediate condition\n",
+      "alpha=100.;\n",
+      "m=10.;\n",
+      "etad=1./(1+(alpha/m));#Fitted adsorption efficiency factor from Eqn.(23)\n",
+      "abkbe3=M*etad+(uo/ub)*Kbc;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'For non absorbing particles:\\tDiameter of bubble=%fcm\\tBubble-cloud interchange coefficient=%fs**-1'%(d,Kbc);\n",
+      "print 'For highly absorbing partilces:\\tM=%f'%(M);\n",
+      "print 'For intermediate condition:\\tFitted adsorption efficiency factor:%f\\tBubble-emuslion interchange coefficient:%fs**-1'%(etad,abkbe3);\n",
+      "\n",
+      "#====================================END OF PROGRAM ======================================================"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "For non absorbing particles:\tDiameter of bubble=6.010032cm\tBubble-cloud interchange coefficient=3.000000s**-1\n",
+        "For highly absorbing partilces:\tM=17.000000\n",
+        "For intermediate condition:\tFitted adsorption efficiency factor:0.090909\tBubble-emuslion interchange coefficient:2.545455s**-1\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 273\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "rhos=1.3;                #Density of solids in g/cc\n",
+      "phis=0.806;              #Sphericity of solids\n",
+      "gammab=0.001;            #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "rhog=1.18E-3;            #Density of air in g/cc\n",
+      "Pr=0.69;                 #Prandtl number\n",
+      "myu=1.8E-4;              #Viscosity of gas in g/cm s\n",
+      "Cpg=1.00;                #Specific heat capacity of gas in J/g K\n",
+      "ephsilonmf=0.45;         #Void fraction at minimum fluidization condition\n",
+      "kg=2.61E-4;              #Thermal concuctivity of gas in W/cm k\n",
+      "dp=0.036;                #Particle size in cm\n",
+      "umf=6.5;                 #Velocity at minimum fluidization condition in cm/s\n",
+      "ut=150.;                 #Terminal velocity in cm/s\n",
+      "db=0.4;                  #Equilibrium bubble size in cm\n",
+      "etah=1;                  #Efficiency of heat transfer\n",
+      "uo=[10.,20.,30.,40.,50.];#Superficial gas velocity in cm/s\n",
+      "g=980.;                  #Acceleration due to gravity in square cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "Nustar=2+(((dp*ut*rhog)/myu)**0.5*Pr**(1./3));#Nusselt no. from Eqn.(25)\n",
+      "Hbc=4.5*(umf*rhog*Cpg/db)+5.85*((kg*rhog*Cpg)**0.5*g**0.25/db**(5./4));#Total heat interchange across the bubble-cloud boundary from Eqn.(32)\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of the bubble from Eqn.(6.7)\n",
+      "n=len(uo);\n",
+      "i=0;\n",
+      "x = [0,0,0,0,0]\n",
+      "Nubed = [0,0,0,0,0]\n",
+      "Rep = [0,0,0,0,0]\n",
+      "\n",
+      "while i<n:\n",
+      "    x[i]=(uo[i]-umf)/(ubr*(1-ephsilonmf));#The term delta/(1-epshilonf) after simplification\n",
+      "    Nubed[i]=x[i]*(gammab*Nustar*etah+(phis*dp**2/(6*kg))*Hbc);#Nusselt no. from Eqn.(36)\n",
+      "    Rep[i]=(dp*uo[i]*rhog)/myu;#Reynolds of the particle\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The desired result is the relationship between Nubed and Rep which is in the form of a straight line y=mx+c'\n",
+      "print 'Rep',\n",
+      "print '\\t\\tNubed'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%Rep[i],\n",
+      "    print '\\t%f'%Nubed[i]\n",
+      "    i=i+1;\n",
+      "import matplotlib.pyplot as plt\n",
+      "plt.plot(Rep,Nubed);\n",
+      "plt.xlabel(\"Rep\");\n",
+      "plt.ylabel(\"Nubed\");\n",
+      "plt.show()\n",
+      " "
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The desired result is the relationship between Nubed and Rep which is in the form of a straight line y=mx+c\n",
+        "Rep \t\tNubed\n",
+        "2.360000 \t0.046518\n",
+        "4.720000 \t0.179427\n",
+        "7.080000 \t0.312335\n",
+        "9.440000 \t0.445244\n",
+        "11.800000 \t0.578152\n"
+       ]
+      },
+      {
+       "metadata": {},
+       "output_type": "display_data",
+       "png": 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TIhARCXBKBCIiAc4riSAvL4+oqCgiIyNJT0+vc8z9999PZGQkPXv2pKioyBth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\nEYiIBDglAhGRAKdEICIS4JQIREQC3P8HJOZBYJAptYQAAAAASUVORK5CYII=\n",
+       "text": [
+        "<matplotlib.figure.Figure at 0x269c250>"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 274\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "rhog=1.2;       #Density of air in kg/m**3\n",
+      "myu=1.8E-5;     #Viscosity of gas in kg/m s\n",
+      "kg=2.6E-2;      #Thermal concuctivity of gas in W/m k\n",
+      "dp=1E-4;        #Particle size in m\n",
+      "rhos=8920;      #Density of solids in kg/m**3\n",
+      "Cps=390;        #Specific heat capacity of the solid in J/kg K\n",
+      "ephsilonf=0.5;  #Void fraction of the fluidized bed\n",
+      "umf=0.1;        #Velocity at minimum fluidization condition in m/s\n",
+      "uo=0.1;         #Superficial gas velocity in m/s\n",
+      "pi=3.14\n",
+      "\n",
+      "#CALCULATION\n",
+      "to=0;                 #Initial temperature of the bed\n",
+      "T=100;                #Temperature of the bed\n",
+      "t=0.99*T;             #Particle temperature i.e. when it approaches 1% of the bed temperature\n",
+      "mp=(pi/6)*dp**3*rhos; #Mass of the particle\n",
+      "A=pi*dp**2;           #Surface area of the particle\n",
+      "Rep=(dp*uo*rhog)/myu; #Reynold's no. of the particle\n",
+      "Nubed=0.0178;         #Nusselt no. from Fig.(6)\n",
+      "hbed1=(Nubed*kg)/dp;  #Heat transfer coefficient of the bed\n",
+      "t1=(mp*Cps/(hbed1*A))*math.log((T-to)/(T-t));#Time needed for the particle approach 1 percentage of the bed temperature in case(a)\n",
+      "hbed2=140*hbed1;#Since from Fig.(6) Nup is 140 times Nubed\n",
+      "t2=(mp*Cps/(hbed2*A))*math.log((T-to)/(T-t));#Time needed for the particle approach 1 percentage of the bed temperature in case(b)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Case(a):Using the whole bed coefficient from Fig.(6)'\n",
+      "print '\\tTime needed for the particle approach 1 percentage of the bed temperature is %.0fs'%t1\n",
+      "print 'Case(b):Uisng the single-particle coefficient of Eqn.(25),also shown in Fig.(6)'\n",
+      "print '\\tTime needed for the particle approach 1 percentage of the bed temperature is %.2fs'%t2"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Case(a):Using the whole bed coefficient from Fig.(6)\n",
+        "\tTime needed for the particle approach 1 percentage of the bed temperature is 58s\n",
+        "Case(b):Uisng the single-particle coefficient of Eqn.(25),also shown in Fig.(6)\n",
+        "\tTime needed for the particle approach 1 percentage of the bed temperature is 0.41s\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch12.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch12.ipynb
new file mode 100755
index 00000000..1fc80a09
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch12.ipynb
@@ -0,0 +1,396 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:3cabb972e9b40cc3c2621280c95233b4046eb8d671e52d74d499a7e149a3d9aa"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 12 : Conversion of Gas in Catalytic Reactions"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 293\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "Kr=10.;          #rate constant in m**3 gas/m**3 cat s\n",
+      "D=2E-5;          #Diffusion coefficient of gas in m**2/s\n",
+      "dpbar=68.;       #Average partilce size in micrometers\n",
+      "ephsilonm=0.5;   #Void fraction of fixed bed\n",
+      "gammab=0.005;    #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "ephsilonmf=0.55; #Void fraction at minimum fluidization condition\n",
+      "umf=0.006;       #Velocity at minimum fluidization condition in m/s\n",
+      "db=0.04;         #Equilibrium bubble size in m\n",
+      "Lm=0.7;          #Length of the bed in m\n",
+      "uo=0.1;          #Superficial gas velocity in m/s\n",
+      "dbed=0.26;       #Diameter of the bed in m\n",
+      "g=9.81;          #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub=uo-umf+ubr;#Velocity of bubbles in bubbling beds in Eqn.(6.8)\n",
+      "Kbc=4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5./4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "Kce=6.77*((D*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "delta=uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "gammac=(1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "ephsilonf=1-(1-delta)*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "Lf=(1-ephsilonm)*Lm/(1-ephsilonf);#Length of fixed bed from Eqn.(6.19)\n",
+      "Krtou=Kr*Lm*(1-ephsilonm)/uo;#Dimensionless reaction rate group from Eqn.(5)\n",
+      "Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));#Raction rate for fluidized bed from Eqn.(14)\n",
+      "XA=math.exp(-1*Kf*Lf/ub);#Conversion from Eqn.(16)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The dimnesionless reaction rate group: %f'%Krtou\n",
+      "print 'The reaction rate for fluidized bed: %fs**-1'%Kf\n",
+      "print 'Conversion: %f'%XA\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The dimnesionless reaction rate group: 35.000000\n",
+        "The reaction rate for fluidized bed: 1.979872s**-1\n",
+        "Conversion: 0.030056\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 298\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "umf=0.005;        #Velocity at minimum fluidization condition in m/s\n",
+      "ephsilonm=0.52;   #Void fraction of fixed bed\n",
+      "ephsilonmf=0.57;  #Void fraction at minimum fluidization condition\n",
+      "DA=8.1E-6;        #Diffusion coefficient of gas in m**2/s\n",
+      "DR=8.4E-6;        #Diffusion coefficient of gas in m**2/s\n",
+      "Lm=5;             #Length of the bed in m\n",
+      "dte=1;            #Diameter of tube in m\n",
+      "Kr1=1.5;          #rate constant in m**3 gas/m**3 cat s\n",
+      "Kr3=0.01;         #rate constant in m**3 gas/m**3 cat s\n",
+      "gammab=0.005;     #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "uo=0.45;          #Superficial gas velocity in m/s\n",
+      "db=0.05;          #Equilibrium bubble size in m from Fig.(6.8)\n",
+      "ub=1.5;           #Velocity of bubbles in bubbling bed in m/s from Fig.(6.11(a))\n",
+      "g=9.81;           #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "KbcA=4.5*(umf/db)+5.85*((DA**0.5*g**0.25)/db**(5.0/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "KceA=6.77*((DA*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "KbcR=4.5*(umf/db)+5.85*((DR**0.5*g**0.25)/db**(5./4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "KceR=6.77*((DR*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "delta=uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "gammac=(1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "ephsilonf=1-(1-delta)*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "Lf=(1-ephsilonm)*Lm/(1-ephsilonf);#Length of fixed bed from Eqn.(6.19)\n",
+      "Krtou=Kr1*Lm*(1-ephsilonm)/uo;#Dimensionless reaction rate group from Eqn.(5)\n",
+      "Kr12=Kr1;#Since the reactions are a special case of Denbigh scheme\n",
+      "Kr34=Kr3;\n",
+      "Kf1=(gammab*Kr12+1/((1/KbcA)+(1/(gammac*Kr12+1/((1/KceA)+(1/(gammae*Kr12)))))))*(delta/(1-ephsilonf));#Rate of reaction 1 for fluidized bed from Eqn.(14)\n",
+      "Kf3=(gammab*Kr34+1/((1/KbcR)+(1/(gammac*Kr34+1/((1/KceR)+(1/(gammae*Kr34)))))))*(delta/(1-ephsilonf));#Rate of reaction 2 for fluidized bed from Eqn.(14)\n",
+      "Kf12=Kf1;\n",
+      "Kf34=Kf3;\n",
+      "KfA=((KbcR*KceA/gammac**2+(Kr12+KceA/gammac+KceA/gammae)* \\\n",
+      "    (Kr34+KceR/gammac+KceR/gammae))*delta*KbcA*Kr12*Kr34/ \\\n",
+      "    (1-ephsilonf))/(((Kr12+KbcA/gammac)*(Kr12+KceA/gammae)+Kr12*KceA/gammac) \\\n",
+      "        *((Kr34+KbcR/gammac)*(Kr34+KceR/gammae)+Kr34*KceR/gammac));\n",
+      "            #Rate of raection with respect to A from Eqn.(35)\n",
+      "KfAR=Kr1/Kr12*Kf12-KfA;#Rate of reaction from Eqn.(34)\n",
+      "tou=Lf*(1-ephsilonf)/uo;#Residence time from Eqn.(5)\n",
+      "XA=1-math.exp(-Kf1*tou);#Conversion of A from Eqn.(26)\n",
+      "XR=1-((KfAR/(Kf12-Kf34))*(math.exp(-Kf34*tou)-math.exp(-Kf12*tou)));#Conversion of R from Eqn.(27)\n",
+      "SR=(1-XR)/XA;#Selectivity of R\n",
+      "\n",
+      "#OUTPUT\n",
+      "\n",
+      "print 'Rate of reaction 1 for fluidized bed:%.4f'%Kf1\n",
+      "print 'Rate of reaction 2 for fluidized bed:%.4f'%Kf3\n",
+      "print 'Rate of reaction 1 with respect to A:%.4f'%KfA\n",
+      "print 'The Conversion of Napthalene:%.0f percentage'%(XA*100);\n",
+      "print 'The selectivity of Phthalic anhydride:%.0f percentage'%(SR*100);\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Rate of reaction 1 for fluidized bed:0.6007\n",
+        "Rate of reaction 2 for fluidized bed:0.0099\n",
+        "Rate of reaction 1 with respect to A:0.0058\n",
+        "The Conversion of Napthalene:96 percentage\n",
+        "The selectivity of Phthalic anhydride:95 percentage\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 302\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "Kr=3.;           #rate constant in m**3 gas/m**3 cat s\n",
+      "db=0.12;         #Equilibrium bubble size in m\n",
+      "D=9E-5;          #Diffusion coefficient of gas in m**2/s\n",
+      "dpbar=68;        #Average partilce size in micrometers\n",
+      "ephsilonm=0.42;  #Void fraction of fixed bed\n",
+      "uo=0.4;          #Superficial gas velocity in m/s\n",
+      "Lm=0.8;          #Length of the bed in m\n",
+      "ephsilonmf=0.45; #Void fraction at minimum fluidization condition\n",
+      "umf=0.21;        #Velocity at minimum fluidization condition in m/s\n",
+      "gammab=0;        #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "g=9.81;          #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "ubr=0.711*(g*db)**0.5;  #Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub=uo-umf+ubr;          #Velocity of bubbles in bubbling beds in Eqn.(6.8)\n",
+      "ubstar=ub+3*umf;        #Rise velocity of the bubble gas from Eqn.(45)\n",
+      "delta=(uo-umf)/(ub+umf);#Fraction of bed in bubbles from Eqn.(6.46)\n",
+      "Kbe=4.5*(umf/db);       #Interchange coefficient between bubble and emulsion from Eqn.(47)\n",
+      "Lf=Lm*(1-ephsilonm)/((1-delta)*(1-ephsilonmf));#Length of fixed bed\n",
+      "phi=((Kr/Kbe)**2*((1-ephsilonmf)-gammab*(umf/ubstar))**2+ \\\n",
+      "        ((delta/(1-delta))+umf/ubstar)**2+2*(Kr/Kbe)*((1-ephsilonmf) \\\n",
+      "            -gammab*(umf/ubstar))*((delta/(1-delta))-umf/ubstar))**0.5;\n",
+      "            #From Eqn.(52)\n",
+      "            \n",
+      "q1=0.5*Kr/umf*((1-ephsilonmf)+gammab*(umf/ubstar))+0.5*Kbe/umf* \\\n",
+      "        (((delta/(1-delta))+umf/ubstar)-phi);#From Eqn.(50)\n",
+      "q2=0.5*Kr/umf*((1-ephsilonmf)+gammab*(umf/ubstar))+0.5*Kbe/umf* \\\n",
+      "        (((delta/(1-delta))+umf/ubstar)+phi);#From Eqn.(50)\n",
+      "        \n",
+      "si1=0.5-0.5*((1-delta)/delta)*(umf/ubstar-Kr/Kbe*((1-ephsilonmf)- \\\n",
+      "        gammab*(umf/ubstar))-phi);#From Eqn.(51)\n",
+      "si2=0.5-0.5*((1-delta)/delta)*(umf/ubstar-Kr/Kbe*((1-ephsilonmf)- \\\n",
+      "        gammab*(umf/ubstar))+phi);#From Eqn.(51)\n",
+      "XA=1-(delta/(1-delta))*(1/(uo*phi))*((1-si2)*(si1*delta*ubstar+ \\\n",
+      "        (1-delta)*umf)*math.exp(-q1*Lf)+(si1-1)* \\\n",
+      "        (si2*delta*ubstar+(1-delta)*umf)*math.exp(-q2*Lf));\n",
+      "        #Conversion from Eqn.(49)\n",
+      "        \n",
+      "Krtou=Kr*Lm*(1-ephsilonm)/uo;#Dimensionless reaction rate group from Eqn.(5)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'COmparing the values of 1-XA = %f and Krtou = %f with Fig.(6), \\\n",
+      "we can conlcude that this operating condition is shown as point \\\n",
+      "A in Fig.(3)'%(1-XA,Krtou);\n",
+      "print 'Line 2 gives the locus of conversions for different values of the \\\n",
+      "reaction rate group for this fluidized contacting'\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "COmparing the values of 1-XA = 0.113843 and Krtou = 3.480000 with Fig.(6), we can conlcude that this operating condition is shown as point A in Fig.(3)\n",
+        "Line 2 gives the locus of conversions for different values of the reaction rate group for this fluidized contacting\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 305\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "uo=0.25;        #Superficial gas velocity in m/s\n",
+      "db=0.025;       #Equilibrium bubble size in m\n",
+      "Kr=1.5;         #rate constant in m**3 gas/m**3 cat s\n",
+      "umf=0.21;       #Velocity at minimum fluidization condition in m/s\n",
+      "Lm=0.8;         #Length of the bed in m\n",
+      "ephsilonm=0.42; #Void fraction of fixed bed\n",
+      "g=9.81;         #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub=uo-umf+ubr;#Velocity of bubbles in bubbling beds in Eqn.(6.8)\n",
+      "delta=(uo-umf)/(ub+2*umf);#Fraction of bed in bubbles from Eqn.(55) since ub/umf<<1 \n",
+      "XA=1-math.exp(-Kr*Lm*((1-ephsilonm)/uo)*(umf/uo)*(1-delta));#Conversion from Eqn.(57)\n",
+      "Krtou=Kr*Lm*(1-ephsilonm)/uo;#Dimensionless reaction rate group from Eqn.(5)\n",
+      "\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Comparing the values of 1-XA = %f and Krtou = %f with Fig.(6), \\\n",
+      "we can conlcude that this operating condition is shown \\\n",
+      "as point B in Fig.(3)'%(1-XA,Krtou);\n",
+      "print 'Line 3 gives the locus of conversions for different values \\\n",
+      "of the reaction rate group for this fluidized contacting'\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Comparing the values of 1-XA = 0.108243 and Krtou = 2.784000 with Fig.(6), we can conlcude that this operating condition is shown as point B in Fig.(3)\n",
+        "Line 3 gives the locus of conversions for different values of the reaction rate group for this fluidized contacting\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 5, Page 307\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "uo=0.3;          #Superficial gas velocity in m/s\n",
+      "Lf=1.1;          #Length of fixed bed in m\n",
+      "Hf=1.2;          #Length of freeboard in m\n",
+      "db=0.04;         #Equilibrium bubble size in m\n",
+      "umf=0.006;       #Velocity at minimum fluidization condition in m/s\n",
+      "ephsilonmf=0.55; #Void fraction at minimum fluidization condition\n",
+      "gammab=0.005;    #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "Kr=10.;          #rate constant in m**3 gas/m**3 cat s\n",
+      "D=2E-5;          #Diffusion coefficient of gas in m**2/s\n",
+      "g=9.81;          #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub=uo-umf+ubr;#Velocity of bubbles in bubbling beds in Eqn.(6.8)\n",
+      "Kbc=4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5./4));\n",
+      "#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "\n",
+      "Kce=6.77*((D*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;\n",
+      "#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "\n",
+      "delta=uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "ephsilonf=1-(1-delta)*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "gammac=(1-ephsilonmf)*((3.0/(ubr*ephsilonmf/umf-1))+fw);\n",
+      "#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "\n",
+      "gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;\n",
+      "#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "\n",
+      "Kf=(gammab*Kr)+1.0/((1.0/Kbc)+(1.0/(gammac*Kr+1.0/((1.0/Kce)+(1.0/(gammae*Kr))))));\n",
+      "#Raction rate for fluidized bed from Eqn.(14)\n",
+      "\n",
+      "XA=1-math.exp(-1*Kf*Lf/ub);#Conversion at the top of dense bed from Eqn.(16)\n",
+      "etabed=(Kf*delta)/(Kr*(1-ephsilonf));#Reactor efficiency from Eqn.(22)\n",
+      "a=0.6/uo  #Since uoa = 0.6s**-1 from Fig.(5)\n",
+      "adash=6.62; #From Fig.(5)\n",
+      "XA1=1-1.0/(math.exp(((1-ephsilonf)*Kr/(uo*a))*((1-math.exp(-a*Hf))- \\\n",
+      "    ((1-etabed)/(1+(adash/a)))*(1-math.exp(-(a+adash)*Hf)))));#Conversion from Eqn.(64)\n",
+      "XA2=1-(1.0-XA1)*(1.0-XA);#Conversion at the exit from Eqn.(64)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The conversion:'\n",
+      "print '\\tAt the top pf the dense bed: %d percentage'%(XA1*100)\n",
+      "print '\\tAt the reactor exit: %d percentage'%(XA2*100);\n",
+      "\n",
+      "#Disclaimer: The value of kf deviate from the one given in textbook, where as it is close to the value obtained by manual calculation. \n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The conversion:\n",
+        "\tAt the top pf the dense bed: 96 percentage\n",
+        "\tAt the reactor exit: 99 percentage\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch13.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch13.ipynb
new file mode 100755
index 00000000..18536015
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch13.ipynb
@@ -0,0 +1,308 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:a97460b196d7b42e945dcfefc11684cc1c39c5847f8b0bdc9e3f6cdcd94bfcc3"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Chapter 13 : Heat Transfer between Fluidized Beds and Surfaces"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 331\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dp=57.0;         #Particle size in micrometer\n",
+      "rhos=940.0;      #Density of solids in kg/m**3\n",
+      "Cps=828.0;       #Specific heat capacity of the solid in J/kg K\n",
+      "ks=0.20;         #Thermal conductivity of solids in W/m k\n",
+      "kg=0.035;        #Thermal concuctivity of gas in W/m k\n",
+      "umf=0.006;       #Velocity at minimum fluidization condition in m/s\n",
+      "ephsilonmf=0.476;#Void fraction at minimum fluidization condition\n",
+      "do1=0.0254;      #Outside diameter of tube in m\n",
+      "L=1;\n",
+      "uo=[0.05,0.1,0.2,0.35];#Superficial gas velocity in m/s\n",
+      "nw=[2.,3.1,3.4,3.5];   #Bubble frequency in s**-1\n",
+      "g=9.81;                #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "\n",
+      "#CALCULATION\n",
+      "dte=4.*do1*L/2.*L;     #Hydraulic diameter from Eqn.(6.13)\n",
+      "db=(1+1.5)*0.5*dte;    #Rise velocity of the bubble\n",
+      "ubr=0.711*(g*db)**0.5; #Rise velocity of bubble from Eqn.(6.7)\n",
+      "phib=0.19;#From Fig.(15) for ks/kg=5.7\n",
+      "ke=ephsilonmf*kg+(1-ephsilonmf)*ks*(1/((phib*(ks/kg))+(2/3.0)))\n",
+      "    #Effective thermal conductivity of bed from Eqn.(3) \n",
+      "    \n",
+      "n=len(uo);\n",
+      "i=0;\n",
+      "ub = [0,0,0,0]\n",
+      "delta = [0,0,0,0]\n",
+      "h = [0,0,0,0]\n",
+      "while i<n:\n",
+      "    ub[i]=uo[i]-umf+ubr; #Velocity of bubbles in bubbling beds in Eqn.(6.8)\n",
+      "    delta[i]=uo[i]/ub[i];#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "    h[i]=1.13*(ke*rhos*(1-ephsilonmf)*Cps*nw[i]*(1-delta[i]))**0.5;\n",
+      "        #Heat transfer coefficinet from Eqn.(18)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Superficial gas velocity(m/s)',\n",
+      "print '\\tHeat transfer coefficient(W/m**2 k)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%uo[i],\n",
+      "    print '\\t\\t\\t%f'%h[i]\n",
+      "    i=i+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Superficial gas velocity(m/s) \tHeat transfer coefficient(W/m**2 k)\n",
+        "0.050000 \t\t\t270.297375\n",
+        "0.100000 \t\t\t323.421769\n",
+        "0.200000 \t\t\t315.487604\n",
+        "0.350000 \t\t\t292.370761\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 332\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dp=80.;              #Particle size in micrometer\n",
+      "rhos=2550.;          #Density of solids in kg/m**3\n",
+      "Cps=756.;            #Specific heat capacity of the solid in J/kg K\n",
+      "ks=1.21;             #Thermal conductivity of solids in W/m k\n",
+      "kg=[0.005,0.02,0.2]; #Thermal concuctivity of gas in W/m k\n",
+      "ephsilonmf=0.476;    #Void fraction at minimum fluidization condition\n",
+      "\n",
+      "#CALCULATION\n",
+      "delta=0.5*(0.1+0.3);#For a gently fluidized bed\n",
+      "nw=3.;#Bubble frequency in s**-1 from Fig.(5.12) at about 30cm above the distributor\n",
+      "n=len(kg);\n",
+      "i=0;\n",
+      "x = [0,0,0]\n",
+      "while i<n:\n",
+      "    x[i]=ks/kg[i];#To find different values of ks/kg\n",
+      "    i=i+1;\n",
+      "\n",
+      "phib=[0.08,0.10,0.20];#From Fig.(15) for different values of ks/kg\n",
+      "i=0;\n",
+      "ke = [0,0,0]\n",
+      "h1 =[0,0,0]\n",
+      "while i<n:\n",
+      "    ke[i]=ephsilonmf*kg[i]+(1-ephsilonmf)*ks*(1/((phib[i]*(ks/kg[i]))+(2.0/3)))\n",
+      "    #Effective thermal conductivity of bed from Eqn.(3)\n",
+      "    \n",
+      "    h1[i]=1.13*(ke[i]*rhos*(1-ephsilonmf)*Cps*nw*(1-delta))**0.5;#Heat transfer coefficinet from Eqn.(18)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Thermal conductivity of Gas(W/m K))',\n",
+      "print '\\tMax. heat transfer coefficient(W/m**2 k)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%kg[i],\n",
+      "    print '\\t\\t\\t\\t%d'%h1[i]\n",
+      "    i=i+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Thermal conductivity of Gas(W/m K)) \tMax. heat transfer coefficient(W/m**2 k)\n",
+        "0.005000 \t\t\t\t324\n",
+        "0.020000 \t\t\t\t567\n",
+        "0.200000 \t\t\t\t1157\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 332\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "rhos=2700.;        #Density of solids in kg/m**3\n",
+      "Cps=755.;          #Specific heat capacity of the solid in J/kg K\n",
+      "ks=1.2;            #Thermal conductivity of solids in W/m k\n",
+      "kg=0.028;          #Thermal concuctivity of gas in W/m k\n",
+      "ephsilonmf=0.476;  #Void fraction at minimum fluidization condition\n",
+      "dp1=10E-3;         #Particle size for which h=hmax in m\n",
+      "hmax=250.;         #Max. heat transfer coefficient in W/m**2 K \n",
+      "nw=5.;             #Bubble frequency in s**-1\n",
+      "delta=0.1;         #Fraction of bed in bubbles\n",
+      "deltaw=0.1;        #Fraction of bed in bubbles in wall region\n",
+      "dp=2E-3;           #Diameter of particle in m\n",
+      "\n",
+      "#CALCULATION\n",
+      "x=ks/kg;\n",
+      "phib=0.11;\n",
+      "phiw=0.17;\n",
+      "ke=ephsilonmf*kg+(1-ephsilonmf)*ks*(1/((phib*(ks/kg))+(2.0/3)));\n",
+      "#Effective thermal conductivity of bed from Eqn.(3)\n",
+      "\n",
+      "hpacket=1.13*(ke*rhos*(1-ephsilonmf)*Cps*nw/(1-deltaw))**0.5;\n",
+      "#Heat transfer coefficient for the packet of emulsion from Eqn.(11)\n",
+      "\n",
+      "ephsilonw=ephsilonmf;#Void fraction in the wall region\n",
+      "\n",
+      "kew=ephsilonw*kg+(1-ephsilonw)*ks*((phiw*(ks/kg)+(1.0/3))**-1);\n",
+      "#Effective thermal conductivity in the wall region with stagnant gas from Eqn.(4)\n",
+      "\n",
+      "y=(2*kew/dp1)+(hmax*hpacket)/(((1-deltaw)*hpacket)-hmax);\n",
+      "#Calculating the term alphaw*Cpg*rhog*uo from Eqn.(16) by rearranging it\n",
+      "\n",
+      "h=(1-deltaw)/((2*kew/dp+y*(dp/dp1)**0.5)**-1+hpacket**-1);\n",
+      "#Heat transfer coeeficient from Eqn.(11) by using the value of y \n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The heat transfer coefficient for paricle size of %fm = %fW/m**2 K'%(dp,h);\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The heat transfer coefficient for paricle size of 0.002000m = 194.873869W/m**2 K\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 334\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "Hf=4.0;   #Height of freeboard in m\n",
+      "uo=2.4;   #Superficial gas velocity in m/s\n",
+      "ho=350.0; #Heat transfer coefficient at the bottom of freeboard region in W/m**2 K\n",
+      "hg=20.0;  #Heat transfer coefficient in equivalent gas stream, but free of solids in W/m**2 K\n",
+      "\n",
+      "#CALCULATION\n",
+      "zf=[0,0.5,1,1.5,2,2.5,3,3.5,Hf];#Height above the top of the dense bubbling fluidized bed\n",
+      "hr=0;#Assuming heat transfer due to radiation is negligible\n",
+      "a=1.5/uo;#Since decay coefficient from Fig.(7.12), a*uo=1.5s**-1 \n",
+      "n=len(zf);\n",
+      "i=0;\n",
+      "h = []\n",
+      "while i<n:\n",
+      "    h.append((hr+hg)+(ho-hr-hg)*math.exp(-a*zf[i]/2.0));#Heat transfer coefficient from Eqn.(24) for zf=Hf\n",
+      "    i=i+1;\n",
+      "\n",
+      "hbar=(hr+hg)+2*(ho-hr-hg)*(1-math.exp(-a*Hf/2.0))/(a*Hf);#Mean heat transfer coefficient for the 4-m high freeboard from Eqn.(26)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The required relationship is h(W/m**2 K) vs. zf(m) as in Fig.(9a)'\n",
+      "print 'Height above the dense bubbling fluidized bed(m))',\n",
+      "print '\\tHeat transfer coefficient(W/m**2 k)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%zf[i],\n",
+      "    print '\\t\\t\\t\\t\\t\\t%f'%h[i]\n",
+      "    i=i+1;\n",
+      "\n",
+      "print '\\nThe mean heat transfer coefficient for the 4-m high freeboard =%d W/m**2 K'%hbar\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The required relationship is h(W/m**2 K) vs. zf(m) as in Fig.(9a)\n",
+        "Height above the dense bubbling fluidized bed(m)) \tHeat transfer coefficient(W/m**2 k)\n",
+        "0.000000 \t\t\t\t\t\t350.000000\n",
+        "0.500000 \t\t\t\t\t\t302.263958\n",
+        "1.000000 \t\t\t\t\t\t261.433158\n",
+        "1.500000 \t\t\t\t\t\t226.508723\n",
+        "2.000000 \t\t\t\t\t\t196.636271\n",
+        "2.500000 \t\t\t\t\t\t171.085009\n",
+        "3.000000 \t\t\t\t\t\t149.229857\n",
+        "3.500000 \t\t\t\t\t\t130.536154\n",
+        "4.000000 \t\t\t\t\t\t114.546583\n",
+        "\n",
+        "The mean heat transfer coefficient for the 4-m high freeboard =208 W/m**2 K\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch14.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch14.ipynb
new file mode 100755
index 00000000..24a0ffbb
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch14.ipynb
@@ -0,0 +1,416 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:a7839feeb371e4231dbf99a0d3738674ff633956f5fb373aea54d56b513c13f8"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 14 : The RTD and Size Distribution of Solids in Fluidized Beds"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 343"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "\n",
+      "#INPUT\n",
+      "Fo=2.7;                         #Feed rate in kg/min\n",
+      "Fof=0.9;                        #Feed rate of fines in feed in kg/min\n",
+      "Foc=1.8;                        #Feed rate of coarse in feed in kg/min\n",
+      "W=17.;                           #Bed weight in kg\n",
+      "kf=0.8;                         #Elutriation of fines in min**-1\n",
+      "kc=0.0125;                      #Elutriation of coarse in min**-1\n",
+      "\n",
+      "#CALCULATION\n",
+      "F1guess=1;                      #Guess value of F1\n",
+      "def solver_func(F1):            #Function defined for solving the system\n",
+      "    return F1-(Fof/(1.+(W/F1)*kf))-(Foc/(1.+(W/F1)*kc));#Eqn.(17)\n",
+      "\n",
+      "F1=fsolve(solver_func,F1guess)\n",
+      "F1f=Fof/(1.+(W/F1)*kf);          #Flow rate of fines in entrained streams from Eqn.(16)\n",
+      "F1c=Foc/(1.+(W/F1)*kc);          #Flow rate of coarse in entrained streams from Eqn.(16)\n",
+      "F2f=Fof-F1f;                    #Flow rate of fines in overflow streams from Eqn.(9)\n",
+      "F2c=Foc-F1c;                    #Flow rate of coarse in overflow streams from Eqn.(9)\n",
+      "tbarf=1./((F1/W)+kf);            #Mean residence time of fines from Eqn.(12)\n",
+      "tbarc=1./((F1/W)+kc);            #Mean residence time of coarse from Eqn.(12)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Flow rate in entrained stream:\\tFines:%fkg/min\\tCoarse:%fkg/min'%(F1f,F1c);\n",
+      "print 'Flow rate in overflow stream:\\tFines:%fkg/min\\tCoarse:%fkg/min'%(F2f,F2c);\n",
+      "print 'Mean residence time:\\tFines:%fmins\\tCoarse:%fmins'%(tbarf,tbarc);\n",
+      "\n",
+      "#====================================END OF PROGRAM ======================================================"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Flow rate in entrained stream:\tFines:0.100000kg/min\tCoarse:1.600000kg/min\n",
+        "Flow rate in overflow stream:\tFines:0.800000kg/min\tCoarse:0.200000kg/min\n",
+        "Mean residence time:\tFines:1.111111mins\tCoarse:8.888889mins\n"
+       ]
+      }
+     ],
+     "prompt_number": 30
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 344\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "\n",
+      "import math\n",
+      "from numpy import linspace,array,zeros\n",
+      "from scipy.optimize import fsolve\n",
+      "from matplotlib.pyplot import *\n",
+      "%matplotlib inline\n",
+      "#Variable declaration\n",
+      "dt=4.;          #Diameter of reactor in m\n",
+      "ephsilonm=0.4; #Void fraction of static bed\n",
+      "rhos=2500.;     #Density of solid in the bed in kg/m**3\n",
+      "Lm=1.2;        #Height of static bed in m\n",
+      "Fo=3000;       #Feed rate in kg/hr\n",
+      "beta1=1.2;     #Increase in density of solids\n",
+      "dp=array([3,4,5,6,7,8,9,10,11,12,3,14,16,18,20,22,24,26,28,30])*10**-2;#Size of particles in mm\n",
+      "po=[0,0.3,0.8,1.3,1.9,2.6,3.5,4.4,5.7,6.7,7.5,7.8,7.5,6.3,5.0,3.6,2.4,1.3,0.5,0];#Size distribution of solids in mm**-1\n",
+      "k=array([0,10,9.75,9.5,8.75,7.5,6.0,4.38,2.62,1.20,0.325,0,0,0,0,0,0,0,0,0])*10**-4;#Elutriation constant in s**-1\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "W=(pi/4*dt**2)*Lm*(1-ephsilonm)*rhos;#Weight of solids in bed\n",
+      "n=len(dp);\n",
+      "i=0;\n",
+      "F1guess=1000.;#Guess value for F1\n",
+      "F1c=linspace(2510,2700,10);\n",
+      "F1 = zeros(n)\n",
+      "x = zeros(n)\n",
+      "c = zeros(n)\n",
+      "a = zeros(n)\n",
+      "while i<n:\n",
+      "    if k[i]==0:\n",
+      "        x[i]=0\n",
+      "        #break \n",
+      "    else:\n",
+      "        x[i]=0#(float(po[i])/(W*k[i]/float(F1)))*math.log(1.+(W*k[i]/F1));         \n",
+      "    def solver_func(Fo):\n",
+      "        return F1/(Lm*Fo)-x[i];\n",
+      "\n",
+      "    F1[i] = fsolve(solver_func,F1guess);#Using inbuilt function fsolve for solving Eqn.(20) for F1\n",
+      "    #c[i]=F1c[i]/(Lm*Fo);\n",
+      "    if F1[i]==0:\n",
+      "        a[i]=0;\n",
+      "    else:\n",
+      "        a[i]=(po[i]/(W*k[i]/F1[i]))*math.log(1+(W*k[i]/F1[i]));\n",
+      "\n",
+      "    i=i+1;\n",
+      "\n",
+      "#plot(F1,c);\n",
+      "\n",
+      "#xtitle('F1 vs a,c','F1','a,c');\n",
+      "F1n=2500.;#The point were both the curves meet\n",
+      "F2=beta1*Fo-F1n;#Flow rate of the second leaving stream\n",
+      "j=0;\n",
+      "m=len(dp);\n",
+      "p1 = zeros(m)\n",
+      "p2 = zeros(m)\n",
+      "tbar = zeros(m)\n",
+      "while j<m:\n",
+      "    p1[j]=(1./F1n)*((Fo*po[j])/(1.+(W/F1n)*k[j]));#Size distribution of stream 1 in mm**-1 from Eqn.(16)\n",
+      "    p2[j]=k[j]*W*p1[j]/F2;#Size distribution of stream 2 in mm**-1 from Eqn.(7)\n",
+      "    if p1[j]==0 and p2[j]==0:\n",
+      "        tbar[j]=0;\n",
+      "    elif p1[j]==0:\n",
+      "        tbar[j]=(W*p1[j])/(F2*p2[j]);\n",
+      "    elif  p2[j]==0:\n",
+      "        tbar[j]=(W*p1[j])/(F1n*p1[j]);\n",
+      "    else:\n",
+      "        tbar[j]=(W*p1[j])/(F1n*p1[j]+F2*p2[j]);#Average time in hr from Eqn.(11)\n",
+      "    j=j+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Flow rate of stream 1:%fkg/hr'%F1n\n",
+      "print 'Flow rate of stream 2:%fkg/hr'%F2\n",
+      "j=0;\n",
+      "print 'tbar(hr)'\n",
+      "while j<m:\n",
+      "    print '%f'%tbar[j]\n",
+      "    j=j+1;\n",
+      "\n",
+      "#DISCLAIMER: The value obtained for tbar is deviating highly\n",
+      "#form the one given in textbook. However, the value obtained by manual calculation is close to #\n",
+      "#the   ones obtained from the program."
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Populating the interactive namespace from numpy and matplotlib\n",
+        "Flow rate of stream 1:2500.000000kg/hr"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Flow rate of stream 2:1100.000000kg/hr\n",
+        "tbar(hr)\n",
+        "0.000000\n",
+        "8.962153\n",
+        "8.964162\n",
+        "8.966171\n",
+        "8.972205\n",
+        "8.982279\n",
+        "8.994397\n",
+        "9.007522\n",
+        "9.021824\n",
+        "9.033397\n",
+        "9.040543\n",
+        "9.043200\n",
+        "9.043200\n",
+        "9.043200\n",
+        "9.043200\n",
+        "9.043200\n",
+        "9.043200\n",
+        "9.043200\n",
+        "9.043200\n",
+        "0.000000\n"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stderr",
+       "text": [
+        "WARNING: pylab import has clobbered these variables: ['draw_if_interactive', 'pi']\n",
+        "`%pylab --no-import-all` prevents importing * from pylab and numpy\n"
+       ]
+      }
+     ],
+     "prompt_number": 7
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 351\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dp=1;  #Particle size in mm\n",
+      "Fo=10; #Feed rate in kg/min\n",
+      "k=0.1; #Particle shrinkage rate in mm/min\n",
+      "\n",
+      "#CALCULATION\n",
+      "R=k/2;             #Particle shrinkage rate in terms of radius\n",
+      "W=(Fo*dp/2)/(4*R); #Bed weight from Eqn.(42)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Weight of bed:%d kg' %W\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Weight of bed:25 kg\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 352\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "#Variable declaration\n",
+      "dpi=[1.05,0.95,0.85,0.75,0.65,0.55,0.45,0.35,0.25,0.15,0.05]; #Mean size in mm\n",
+      "Fo=[0,0.5,3.5,8.8,13.5,17.0,18.2,17.0,13.5,7.3,0]#*10**-2  #Feed rate in kg/s\n",
+      "for i in range(len(Fo)):\n",
+      "    Fo[i] = Fo[i] * 10**-2\n",
+      "k=[0,0,0,0,0,0,0,0,2.0,12.5,62.5]#*10**-5;#Elutriation constant in s**-1\n",
+      "for i in range(len(k)):\n",
+      "    k[i] = k[i] * 10**-5\n",
+      "\n",
+      "R=-1.58*10**-5;#Rate of particle shrinkage in mm/s\n",
+      "deldpi=0.1;#Size intervals in mm\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(dpi);\n",
+      "m=1;#Starting with the largest value size interval that contains solids\n",
+      "W = [0]\n",
+      "while m<n-1:\n",
+      "    W.append((Fo[m]-R*W[m-1]/deldpi)/(k[m]-R/deldpi-3*R/dpi[m]));#From Eqn.(33)\n",
+      "    m=m+1;\n",
+      "\n",
+      "Wt=sum(W);#Total sum\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nTotal mass in the bed:%fkg'%Wt\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Total mass in the bed:7168.981263kg\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 5, Page 353\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "dpi=[0.17,0.15,0.13,0.11,0.09,0.07,0.05,0.03,0.01];#Mean size of particles in mm\n",
+      "a=[0,0.95,2.45,5.2,10.1,23.2,35.65,20.0,2.45]#*10**-2;#Feed composition Fo(dpi)/Fo\n",
+      "for i in range(len(a)):\n",
+      "    a[i] = a[i] * 10**-2\n",
+      "\n",
+      "y=[0,0,0,0,0,0,0.625,10.225,159.25]#*10**-6;#Elutriation and cyclone efficiency k(dpi)(1-eta(dpi))\n",
+      "for i in range(len(y)):\n",
+      "    y[i] = y[i] * 10**-6\n",
+      "\n",
+      "\n",
+      "F=0.01;          #Rate at which solids are withdrawn in kg/s\n",
+      "W=40000;         #Weight of bed in kg\n",
+      "dp1=0.11         #Initial size in mm\n",
+      "dp2=0.085;       #Size after shrinking in mm\n",
+      "dpmin=0.01;      #Minimum size in mm\n",
+      "deldpi=2*10**-2; #Size inerval in mm\n",
+      "t=20.8;          #Time in days\n",
+      "si=1;\n",
+      "\n",
+      "#CALCULATION\n",
+      "kdash=math.log((dp1-dpmin)/(dp2-dpmin))/(t*24*3600);#Rate of particle shrinkage from Eqn.(24)\n",
+      "n=len(dpi);\n",
+      "m=1;\n",
+      "Fo=0.05;#Initial value of Fo\n",
+      "F1 = [0];\n",
+      "s=0;\n",
+      "c=0;\n",
+      "t=1E-6;\n",
+      "R = [0]\n",
+      "x = [0]\n",
+      "F1 = [0]\n",
+      "while m<n:\n",
+      "    R.append(-kdash*(dpi[m]-dpmin));#Rate of size change\n",
+      "    x.append((a[m]*Fo-W*R[m-1]*F1[m-1]/deldpi)/(F+(W*y[m])-(W*R[m]/deldpi)-3*W*R[m]/dpi[m]));#Eqn.(34)\n",
+      "    F1.append(x[m]*F);\n",
+      "    c=c+x[m];\n",
+      "    m=m+1;\n",
+      "    if abs(c-1)<t:\n",
+      "        break\n",
+      "    Fo=Fo+0.0001;#Incrementing Fo\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Feed rate with deldpi=%fmm is %fg/hr'%(deldpi,Fo);\n",
+      "i=0;\n",
+      "print 'Bed composition'\n",
+      "for i in x:\n",
+      "    print '%f'%(i*100)\n",
+      "    i=i+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Feed rate with deldpi=0.020000mm is 0.050800g/hr\n",
+        "Bed composition\n",
+        "0.000000\n",
+        "0.652911\n",
+        "1.859952\n",
+        "4.400781\n",
+        "9.668999\n",
+        "25.654298\n",
+        "28.575890\n",
+        "2.317749\n",
+        "0.019493\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch15.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch15.ipynb
new file mode 100755
index 00000000..09c02451
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch15.ipynb
@@ -0,0 +1,294 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:b0605e72f5da8476b3859cf3dc90196dcbe80cabc58b8c8d37cf5b28482c7ee1"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 15 : Circulation Systems"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 369\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "thalf=1;   #Half life of catalyst in s\n",
+      "F=960;     #Feed rate of oil in tons/day\n",
+      "W=50;      #Weight of the bed in tons\n",
+      "a=0.5;     #Activity after time equal to half life\n",
+      "abar=0.01; #Average activity of the catalyst\n",
+      "\n",
+      "#CALCULATION\n",
+      "Ka=-math.log(a)/thalf;#Rate constant is s**-1, assuming I order kinetics from Eqn.(12)\n",
+      "Fs=Ka*W*abar/(1-abar);#Circulation rate of solids from Eqn.(16)\n",
+      "x=(Fs*60*60*24.0)/F;  #Circulation rate per feed of oil\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nSolid recirculation per feed of oil =%ftons of solid circulated/ton feed oil'%x\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Solid recirculation per feed of oil =31.506690tons of solid circulated/ton feed oil\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 370\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "#Variable declaration\n",
+      "deltaHr1=1260.;                               #Enthalpy change during endothermic reaction in kJ/kg\n",
+      "deltaHr2=-33900.;                             #Enthal[y change during exothermic reaction in kJ/kg\n",
+      "H1=703.;                                      #Enthalpy of feed oil in kJ/kg\n",
+      "T1=260.;                                      #Temperature of feed oil in degree celcius\n",
+      "H3=1419.;                                     #Enthalpy of cracked product in kJ/kg\n",
+      "T3=500.;                                      #Temperature of cracked product in degree celcius\n",
+      "Ta=20.;                                       #Temperature of entering air in degree celcius\n",
+      "Cpa=1.09;                                     #Specific heat of entering air in kJ/kg K\n",
+      "Cpf=1.05;                                     #Specific heat of flue gases in kJ/kg K\n",
+      "Cps=1.01;                                     #Specific heat of solids in kJ/kg K\n",
+      "Cpv=3.01;                                     #Specific heat of vaporized feed in kJ/kg K\n",
+      "T4=[520.,540.,560.,580.,600.,620.,640.,660.]; #Temperature of flue gas in degree celcius\n",
+      "V=22.4;                                       #Volume of 1 mole of Carbon dioxide gas in N-m**3\n",
+      "M=12.;                                        #Molecular weight of carbon in kg\n",
+      "rho=1.293;                                    #Density of carbon dioxide gas in kg/N-m**3\n",
+      "xa=0.21;                                      #Mass fraction of oxygen in air\n",
+      "betac=0.07;                                   #Mass fraction of carbon\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(T4);\n",
+      "i=0;\n",
+      "x1 = [0,0,0,0,0,0,0,0]\n",
+      "x2 = [0,0,0,0,0,0,0,0]\n",
+      "excess_air = [0,0,0,0,0,0,0,0]\n",
+      "\n",
+      "x2min=betac*(V*rho/(M*xa));#Minimum amount of air required for complete combustion\n",
+      "while i<n:\n",
+      "    x1[i]=(deltaHr1+0.93*H3-H1)/(Cps*(T4[i]-T3));#Fs/F1 by simplifying the overall energy balance\n",
+      "    x2[i]=((0.07*(-deltaHr2)-(deltaHr1+0.93*H3-H1))/(Cpf*(T4[i]-Ta)))-0.07;#F2/F1 by simplifying the energy balance for regenerator\n",
+      "    if x2[i]>x2min:\n",
+      "        excess_air[i]=(x2[i]-x2min)/x2min; #Excess air used\n",
+      "    else:\n",
+      "        excess_air[i]=0;\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT    \n",
+      "print 'T4(degree celcius)',\n",
+      "print '\\tFs/F1',\n",
+      "print '\\t\\tF2/F1',\n",
+      "print '\\t\\tExcess air(percentage)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%T4[i],\n",
+      "    print '\\t\\t%f'%x1[i],\n",
+      "    print '\\t%f'%x2[i],\n",
+      "    print '\\t%f'%(excess_air[i]*100);\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Disclaimer: The values of F2/F1 obtained by manual calculation has close correspondance to the ones obtained as the output, whereas it deviates largely from the values given in textbook.\n",
+      "\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "T4(degree celcius) \tFs/F1 \t\tF2/F1 \t\tExcess air(percentage)\n",
+        "520.000000 \t\t92.904455 \t0.875390 \t8.807235\n",
+        "540.000000 \t\t46.452228 \t0.839029 \t4.287699\n",
+        "560.000000 \t\t30.968152 \t0.805362 \t0.102944\n",
+        "580.000000 \t\t23.226114 \t0.774099 \t0.000000\n",
+        "600.000000 \t\t18.580891 \t0.744992 \t0.000000\n",
+        "620.000000 \t\t15.484076 \t0.717825 \t0.000000\n",
+        "640.000000 \t\t13.272065 \t0.692412 \t0.000000\n",
+        "660.000000 \t\t11.613057 \t0.668586 \t0.000000\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 379\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "Fs=100.;        #Solid flowrate in kg/s\n",
+      "ephsilon1=0.55;\n",
+      "ephsilon2=0.5;\n",
+      "p1=120.;         #Pressure at upper level in kPa\n",
+      "rhos=1000.;      #Density of solid in kg/m**3\n",
+      "rhog=1.;         #Density of gas in kg/m**3\n",
+      "gc=1.;           #Conversion factor\n",
+      "g=9.81;          #Acceleration due to gravity in m/s**2\n",
+      "di=0.34;         #Diameter of downcomer in m\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "x=(ephsilon1/ephsilon2)*((1-ephsilon2)/(1-ephsilon1));#To find pressure at lower level using Eqn.(30)\n",
+      "p2=x*p1;#Pressure at lower level using Eqn.(30)\n",
+      "deltap=p2-p1;\n",
+      "ephsilonbar=0.5*(ephsilon1+ephsilon2);\n",
+      "deltah=(deltap*10**3*gc)/(rhos*(1-ephsilonbar)*g);#Static head height from Eqn.(28)\n",
+      "At=0.25*pi*di**2;#Area of downcomer\n",
+      "Gs=Fs/At;#Flux of solids in downcomer\n",
+      "Gg=Gs*(ephsilon1/(1-ephsilon1))*(rhog/rhos)*(x-1);#Required gas aeration rate from Eqn.(31)\n",
+      "Fg=Gg*At;#Flow rate of gas required\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nThe required flow rate of gas required for location of %fm below downcomer is %.4fkg/s'%(deltah,Fg)\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "The required flow rate of gas required for location of 5.722768m below downcomer is 0.0272kg/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 380\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "Fs=600;#Solid circulation rate in kg/s\n",
+      "dpbar=60;#Mean size of solids in micrometer\n",
+      "pA=120;#Pressure in vessel A in kPa\n",
+      "pB=180;#Pressure in vessel B in kPa\n",
+      "LfA=8;#Bed height in vessel A in m\n",
+      "LfB=8;#Bed height in vessel B i m\n",
+      "#Bulk densities in kg/m**3\n",
+      "rho12=100;\n",
+      "rho34=400;\n",
+      "rho45=550;\n",
+      "rho67=200;\n",
+      "rho78=200;\n",
+      "rho910=400;\n",
+      "rho1011=400;\n",
+      "rho1112=550;\n",
+      "rho13=100;\n",
+      "deltapdA=7;#Pressure drop across the distributor in regenerator in kPa\n",
+      "deltapdB=8;#Pressure drop across the distributor in reactor in kPa\n",
+      "deltap12=(9+4);#Friction loss and pressure difference required to accelerate the solids in transfer lines in kPa\n",
+      "deltap78=(15+3);#Friction loss and pressure difference required to accelerate the solids in transfer lines in kPa\n",
+      "deltap45=20;#Friction loss across the reactor's stripper downcomer in kPa\n",
+      "deltap1112=4;#Friction loss across the regenerator's downcomer in kPa\n",
+      "deltapvA=5;#Pressure drop assigned for the control valve in regenerator in kPa\n",
+      "deltapvB=15;#Pressure drop assigned for the control valve in reactor in kPa\n",
+      "deltah12=15;#Height of the riser in m\n",
+      "deltah86=30;#Height of the riser in m\n",
+      "deltah1011=7;#Height difference h10-h11 in m\n",
+      "g=9.81;#Acceleration due to gravity in m/s**2\n",
+      "gc=1;#Conversion factor\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "Gs=900;#From Fig.(8), to find dt\n",
+      "dt=math.sqrt((4/math.pi)*Fs/Gs);#Diameter of the downcomer\n",
+      "#Height of downcomer A from Eqn.(7)\n",
+      "deltahA=(1/(rho1112*g))*((pB-pA)*gc*(10**3)+(deltap12+deltapdB+deltap1112+deltapvA)*gc*10**3-rho12*g*(-deltah12)-rho34*g*(-LfB)-rho1011*g*deltah1011);\n",
+      "#Height of downcomer B from Eqn.(8)\n",
+      "deltahB=(1/(rho45*g))*(-(pB-pA)*gc*10**3+(deltap45+deltapvB+deltap78+deltapdA)*gc*10**3+rho78*g*deltah86+rho910*g*LfA)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Height of downcomer for:'\n",
+      "print '\\tRegenerator:%d m'%deltahA\n",
+      "print '\\tReactor:%.1f m'%deltahB\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Height of downcomer for:\n",
+        "\tRegenerator:20 m\n",
+        "\tReactor:16.7 m\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch16.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch16.ipynb
new file mode 100755
index 00000000..e835e890
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch16.ipynb
@@ -0,0 +1,428 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:1a37ab741ccda7f67c7de1085d3807de9fa5a11a3111916ad9502a04f1c58721"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 16 : Design for Physical Operations"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 404\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "T=1000.;       #Operating temperature of calciner in degree celcius\n",
+      "deltaHr=1795.; #Heat of reaction in kJ/kg\n",
+      "M1=0.1;        #Molecular weight of Calcium carbonate in kg/mol\n",
+      "M2=0.056;      #Molecular weight of CaO in kg/mol\n",
+      "M3=0.044;      #Molecular weight of Carbon dioxide  in kg/mol\n",
+      "M4=0.029;      #Molecular weight of Air in kg/mol\n",
+      "M5=0.029;      #Molecular weight of Combustion gas in kg/mol\n",
+      "Cp1=1.13;      #Specific heat of Calcium carbonate in kJ/kg K\n",
+      "Cp2=0.88;      #Specific heat of CaO in kJ/kg K\n",
+      "Cp3=1.13;      #Specific heat of Carbon dioxide in kJ/kg K\n",
+      "Cp4=1.00;      #Specific heat of Air in kJ/kg K\n",
+      "Cp5=1.13;      #Specific heat of Calcium carbonate in kJ/kg K\n",
+      "Tf=20.;        #Temperature of feed in degree celcius\n",
+      "ma=15.;        #Air required per kg of fuel in kg\n",
+      "Hc=41800.;     #Net combustion heat of fuel in kJ/kg\n",
+      "Tpi=20.;       #Initial temperature of solids in degree C\n",
+      "Tgi=1000.;     #Initial temperature of gas in degree C\n",
+      "\n",
+      "#CALCULATION\n",
+      "mc=1;#Based on 1 kg of Calcium carbonate\n",
+      "B=(1/(Hc-(ma+mc)*Cp5*(T-Tpi)))*(M3*Cp3*(T-Tf)+M2*Cp2*(T-Tf)+deltaHr)#Fuel consumption(kg fuel/kg calcium carbonate)\n",
+      "B1=B*M3/M2;#Fuel consumption(kg fuel/kg Cao)\n",
+      "H=Hc*B1;#Heat required for calcination\n",
+      "eta=deltaHr/(B*Hc);#Thermal efficiency\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Fuel consumption:%f kg fuel/kg Cao'%B1\n",
+      "print 'Heat requirement for calcination:%f kJ/kg Cao'%H\n",
+      "print 'Thermal efficiency:%f percentage'%(eta*100)\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Fuel consumption:0.061731 kg fuel/kg Cao\n",
+        "Heat requirement for calcination:2580.366029 kJ/kg Cao\n",
+        "Thermal efficiency:54.657251 percentage\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 405\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "from scipy.optimize import fsolve\n",
+      "import math\n",
+      "\n",
+      "#INPUT\n",
+      "F = 400.        #Feed rate of Calcium carbonate in tons/day\n",
+      "T = 1000.       #Operating temperature of calciner in degree celcius\n",
+      "deltaHr = 1795.#Heat of reaction in kJ/kg\n",
+      "M1 = 0.1        #Molecular weight of Calcium carbonate in kg/mol\n",
+      "M2 = 0.056     #Molecular weight of CaO in kg/mol\n",
+      "M3 = 0.044     #Molecular weight of Carbon dioxide  in kg/mol\n",
+      "M4 = 0.029    #Molecular weight of Air in kg/mol\n",
+      "M5 = 0.029    #Molecular weight of Combustion gas in kg/mol\n",
+      "Cp1 = 1.13    #Specific heat of Calcium carbonate in kJ/kg K\n",
+      "Cp2 = 0.88    #Specific heat of CaO in kJ/kg K\n",
+      "Cp3 = 1.13   #Specific heat of Carbon dioxide in kJ/kg K\n",
+      "Cp4 = 1.00    #Specific heat of Air in kJ/kg K\n",
+      "Cp5 = 1.17    #Specific heat of Combustion gas in kJ/kg K\n",
+      "Tf = 20.     #Temperature of feed in degree celcius\n",
+      "ma = 15.    #Air required per kg of fuel in kg\n",
+      "uo = 0.8    #Superficial gas velocity in m/s\n",
+      "Hc = 41800.   #Net combustion heat of fuel in kJ/kg\n",
+      "Tpi = 20.     #Initial temperature of solids in degree C\n",
+      "Tgi = 1000.   #Initial temperature of gas in degree C\n",
+      "rhoa = 1.293    #Density of air in kg/m**3\n",
+      "pi = 3.14\n",
+      "\n",
+      "#CALCULATION\n",
+      "mc = 1.         #Based on 1 kg of Calcium carbonate\n",
+      "Bguess = 2.     #Guess value of B\n",
+      "def solver_func(B):         #Function defined for solving the system\n",
+      "    phi = ((ma+mc)*Cp5*B+(M3*Cp3))/Cp1\n",
+      "    T3 = (Tpi+(phi+phi**2+phi**3)*Tgi)/(1+phi+phi**2+phi**3)\n",
+      "    phiplus = 30.6*B\n",
+      "    Tr = (T+Tpi*phiplus)/(1+phiplus)\n",
+      "    return Hc*B+Cp3*(T3-Tpi)+ma*B*Cp4*(Tr-20)-(ma+mc)*Cp5*(T-Tpi)-M3*Cp3*(T-Tpi)-M2*Cp2*(T-Tpi)-deltaHr\n",
+      "    #fn = (1/20800)*(2470-T3-13.34*(Tr-20))\n",
+      "\n",
+      "B = fsolve(solver_func,1E-6)#Using inbuilt function fsolve for solving Eqn.(23) for tou\n",
+      "phi = ((ma+mc)*Cp5*B+(M3*Cp3))/Cp1\n",
+      "#Temperature of various stages\n",
+      "T1 = (Tpi+(phi)*Tgi)/(1+phi)\n",
+      "T2 = (Tpi+(phi+phi**2)*Tgi)/(1+phi+phi**2)\n",
+      "T3 = (Tpi+(phi+phi**2+phi**3)*Tgi)/(1+phi+phi**2+phi**3)\n",
+      "phiplus = 30.6*B\n",
+      "Tr = (T+Tpi*phiplus)/(1+phiplus)\n",
+      "eta = deltaHr/(B*Hc)           #Thermal efficiency\n",
+      "H = B*Hc/M2                    #Heat requirement\n",
+      "#For lower heat recovery section\n",
+      "Ql = (F*10**3/(24*3600))*B*ma/(rhoa*(273/(Tr+273)))#Volumetric flow rate of gas in the lower heat recovery section\n",
+      "dtl = math.sqrt(4/pi*Ql/uo)#Diameter of lower bed\n",
+      "#For calcination section\n",
+      "Qc = (F*10**3/(24*3600))*B*ma/(rhoa*(273/(T+273)))#Volumetric flow rate of gas in the calcination section\n",
+      "dtc = math.sqrt(4/pi*Qc/uo)#Diameter of calcination section\n",
+      "#For I stage\n",
+      "Q1 = (F*10**3/(24*3600))*B*ma/(rhoa*(273/(T1+273)))#Volumetric flow rate of gas in the I stage\n",
+      "dt1 = math.sqrt(4/pi*Q1/uo)#Diameter of I stage\n",
+      "#For II stage\n",
+      "Q2 = (F*10**3/(24*3600))*B*ma/(rhoa*(273/(T2+273)))#Volumetric flow rate of gas in the II stage\n",
+      "dt2 = math.sqrt(4/pi*Q2/uo)#Diameter of II stage\n",
+      "#For III stage\n",
+      "Q3 = (F*10**3/(24*3600))*B*ma/(rhoa*(273/(T3+273)))#Volumetric flow rate of gas in the III stage\n",
+      "dt3 = math.sqrt(4/pi*Q3/uo)#Diameter of III stage\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nDiameter of lower bed:%fm'%(dtl)\n",
+      "print '\\nDiameter of calcination section:%fm'%(dtc)\n",
+      "print '\\nBed no.\\t\\t1\\t2\\t\\t3'\n",
+      "print '\\nDiameter(m)%f\\t%f\\t%f'%(dt1,dt2,dt3)\n",
+      "\n",
+      "#The value of diameter of each section is largely deviating from the values in the textbook. This is because the fuel consumption B have not been included in the energy balance equation. And the value of molecular weight is wrong by one decimal point.\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Diameter of lower bed:7.097814m\n",
+        "\n",
+        "Diameter of calcination section:13.351483m\n",
+        "\n",
+        "Bed no.\t\t1\t2\t\t3\n",
+        "\n",
+        "Diameter(m)12.728715\t13.270865\t13.340712\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 413\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "T=20;         #Temeprature in degree C\n",
+      "M=0.018;      #Molecular weight of water in kg/mol\n",
+      "Q=10;         #Flow rate of dry air in m**3/s\n",
+      "R=82.06E-6;   #Universal gas constant\n",
+      "pi=0.0001;    #Initial moisture content in atm\n",
+      "pj=0.01;      #Final moisture content in atm\n",
+      "\n",
+      "#CALCULATION\n",
+      "a=Q*(273+T)/273;  #Term At*uo\n",
+      "b=a*M/(R*(T+273));#Term C*At*uo\n",
+      "#The value of slope can be found only by graphical mehtod. Hence it has been taken directly from the book(Page no.414,Fig.E3)\n",
+      "m=10.2;\n",
+      "Fo=b/m;           #Flow rate of solids\n",
+      "Q3=(b/Fo)*(pj-pi);#Moisture content of leaving solids\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nMoisture content of leaving solids:%.3f kg H2O/kg dry solids'%Q3\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Moisture content of leaving solids:0.101 kg H2O/kg dry solids\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 422\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "\n",
+      "\n",
+      "\n",
+      "#INPUT\n",
+      "Qfi = 0.20          #Initial moisture fraction\n",
+      "Qfbar = 0.04        #Average final moisture fraction\n",
+      "rhos = 2000.        #Density of solid in kg/m**3\n",
+      "Cps = 0.84          #Specific heat of solids in kJ/kg K\n",
+      "Fo = 7.6E-4         #Flow rate of solids in kg/m**3\n",
+      "Tsi = 20.            #Inital temperature of solids in degree C\n",
+      "rhog = 1.            #Density of gas in kg/m**3\n",
+      "Cpg = 1             #Specific heat of gas in kJ/kg K\n",
+      "uo = 0.3            #Superficial gas velocity in m/s\n",
+      "Tgi = 200           #Initial temperature of gas in degee C\n",
+      "L = 2370            #Enthalpy of liquid in kJ/kg\n",
+      "Cpl = 4.2           #Specific heat of liquid in kJ/kg K\n",
+      "dt = 0.1            #Diameter of reactor in m\n",
+      "Lm = 0.1            #Length of fixed bed in m\n",
+      "ephsilonm = 0.45    #Void fraction of fixed bed\n",
+      "pi = 3.14\n",
+      "Fo1 = 1             #Feed rate for commercial-scale reactor in kg/s\n",
+      "\n",
+      "#CALCULATION\n",
+      "#(a)Bed temperature\n",
+      "Teguess = 50#Guess value of Te\n",
+      "def solver_func(Te):#Function defined for solving the system\n",
+      "    return (pi/4.)*dt**2*uo*rhog*Cpg*(Tgi-Te)-Fo*(Qfi-Qfbar)*(L+Cpl*(Te-Tsi))-Fo*Cps*(Te-Tsi)\n",
+      "\n",
+      "Te = fsolve(solver_func,Teguess)\n",
+      "\n",
+      "#(b)Drying time for a particle\n",
+      "xguess = 2#Guess value of x, ie term tou/tbar\n",
+      "def solver_func1(x):        #Function defined for solving the system\n",
+      "    return 1-(Qfbar/Qfi)-(1-math.exp(-x))/x\n",
+      "\n",
+      "\n",
+      "x = fsolve(solver_func1,xguess)\n",
+      "W = (pi/4.)*dt**2*Lm*(1-ephsilonm)*rhos#Weight of soilds in bed\n",
+      "tbar = W/Fo#Mean residence time of solids from Eqn.(59)\n",
+      "tou = tbar*x#Time for complete drying of a particle\n",
+      "\n",
+      "#(c)Commercial-scale dryer\n",
+      "W1 = Fo1*tbar\n",
+      "Atguess = 5#Guess value of area\n",
+      "def  solver_func3(At):          #Function defined for solving the system\n",
+      "    return  At*uo*rhog*Cpg*(Tgi-Te)-Fo1*(Qfi-Qfbar)*(L+Cpl*(Te-Tsi))-Fo1*Cps*(Te-Tsi)\n",
+      "\n",
+      "At = fsolve(solver_func3,Atguess)\n",
+      "dt1 = math.sqrt(4/pi*At)#Diameter of commercial-scale dryer\n",
+      "Q1 = At*uo*rhog#Flow rate necessary for the operation\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Bed temperature:%f degree C'%(Te)\n",
+      "print 'Time for complete drying of particle:%fs'%(tou)\n",
+      "print 'Flow rate of gas necessary for Commercial-scale dryer:%fkg/s'%(Q1)\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Bed temperature:58.728126 degree C\n",
+        "Time for complete drying of particle:527.431202s\n",
+        "Flow rate of gas necessary for Commercial-scale dryer:3.098684kg/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 5, Page 425\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable Declaration\n",
+      "rhos=1600.;     #Density of solid in kg/m**3\n",
+      "Cps=1.25;       #Specific heat of solids in kJ/kg K\n",
+      "Fo=0.5;         #Flow rate of solids in kg/s\n",
+      "Tsi=20.;        #Inital temperature of solids in degree C\n",
+      "Qwi=1.;         #Initial moisture fraction in water\n",
+      "Qwf=0.2;        #Final moisture fraction in water\n",
+      "Qhi=1.1;        #Initial moisture fraction in heptane\n",
+      "Qhf=0.1;        #Final moisture fraction in heptane\n",
+      "Tgi=240.;       #Initial temperature of gas in degee C\n",
+      "Te=110.;        #Bed temperature in degree C\n",
+      "ephsilonm=0.45; #Void fraction of fixed bed\n",
+      "ephsilonf=0.75; #Void fraction of fluidized bed\n",
+      "uo=0.6;         #Superficial gas velocity in m/s\n",
+      "di=0.08;        #Diameter of tubes in m\n",
+      "li=0.2;         #Pitch for square arrangement\n",
+      "hw=400.;        #Heat transfer coefficient in W/m**2 K\n",
+      "Tc=238.;        #Temperature at which steam condenses in degree C\n",
+      "#Specific heats in kJ/kg K\n",
+      "Cwl=4.18;       #Water liquid\n",
+      "Cwv=1.92;       #Water vapor\n",
+      "Chl=2.05;       #Heptane liquid\n",
+      "Chv=1.67;       #Heptane vapor\n",
+      "#Latent heat of vaporization in kJ/kg\n",
+      "Lw=2260.;       #Water\n",
+      "Lh=326.;        #Heptane\n",
+      "#Density of vapor in kg/m**3 at operating conditions\n",
+      "rhow=0.56;      #Water\n",
+      "rhoh=3.1;       #Heptane\n",
+      "Lf=1.5;         #Length of fixed bed in m\n",
+      "t=140.;         #Half-life of heptane in s\n",
+      "L=1.5;          #Length of tubes in heat exchanger\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#(a) Dryer without Internals\n",
+      "xw=(Qwi-Qwf)/(Qhi-Qhf);                #Water-heptane weight ratio\n",
+      "xv=((Qwi-Qwf)/18.)/((Qhi-Qhf)/100.);   #Water-heptane volume ratio\n",
+      "T=(Qwi-Qwf)/18.+(Qhi-Qhf)/100.;        #Total volume\n",
+      "rhogbar=((Qwi-Qwf)/18.)/T*rhow+((Qhi-Qhf)/100.)/T*rhoh;           #Mean density of the vapor mixture\n",
+      "Cpgbar=(((Qwi-Qwf)/18.)/T)*rhow*Cwv+(((Qhi-Qhf)/100.)/T)*rhoh*Cwv;#Mean specific heat of vapor mixture\n",
+      "#Volumetric flow of recycle gas to the dryer in m**3/s from Eqn.(53)\n",
+      "x=(Cpgbar*(Tgi-Te))**-1*(Fo*(Qwi-Qwf)*(Lw+Cwl*(Te-Tsi))+Fo*(Qhi-Qhf)*(Lh+Chl*(Te-Tsi))+Fo*(Cps*(Te-Tsi)));\n",
+      "r=Fo*((Qwi-Qwf)/rhow+(Qhi-Qhf)/rhoh); #Rate of formation of vapor in bed\n",
+      "uo1=uo*(x/(x+r));                     #Superficial velocity just above the distributor\n",
+      "At=x/uo1;                             #Cross-sectional area of bed\n",
+      "dt=math.sqrt(4./pi*At);               #Diameter of bed\n",
+      "B=-math.log(Qwf/Qwi)/t;               #Bed height from Eqn.(63)\n",
+      "tbar=((Qhi/Qhf)-1)/B;                 #Mean residence time of solids\n",
+      "W=Fo*tbar;                            #Weight of bed\n",
+      "Lm=W/(At*(1-ephsilonm)*rhos);         #Static bed height\n",
+      "Lf=(Lm*(1-ephsilonm))/(1-ephsilonf);  #Height of fluidized bed\n",
+      "\n",
+      "#(b) Dryer with internal heaters\n",
+      "f=1/8.0;                 #Flow rate is 1/8th the flow rate of recirculation gas as in part (a)\n",
+      "x1=f*x;                  #Volumetric flow of recycle gas to the dryer in m**3/s from Eqn.(53)\n",
+      "uo2=uo*(x1/float(x1+r)); #Superficial velocity just above the distributor\n",
+      "Abed=x1/uo2;             #Cross-sectional area of bed\n",
+      "q=(Fo*(Qwi-Qwf)*(Lw+Cwl*(Te-Tsi))+Fo*(Qhi-Qhf)*(Lh+Chl*(Te-Tsi))+Fo*(Cps*(Te-Tsi)))-Abed*uo2*Cpgbar*(Tgi-Te);#Heat to be added from energy balance of Eqn.(53)\n",
+      "Aw=q*10**3/(hw*(Tc-Te));#Total surface area of heat exchanger tubes\n",
+      "Lt=Aw/(pi*di);          #Total length of tubes\n",
+      "Nt=Lt/L;                #Total number of tubes\n",
+      "Atubes=Nt*(pi/4*di**2); #Total cross-sectional area of tubes\n",
+      "Atotal=Abed+Atubes;     #Total cross-sectional area of tube filled dryer\n",
+      "d=math.sqrt(Atotal*pi/4.);#Diameter of vessel\n",
+      "li=math.sqrt(Atotal/Nt);  #Pitch for square array of tubes\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\t\\t\\tBed diameter(m)\\tRecycle vapor flow(m**3/s)'\n",
+      "print 'Without internal heater\\t%f\\t%f'%(dt,x)\n",
+      "print 'With heating tubes\\t%f\\t%f'%(d,x1)\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\t\t\tBed diameter(m)\tRecycle vapor flow(m**3/s)\n",
+        "Without internal heater\t3.630144\t5.331235\n",
+        "With heating tubes\t1.503916\t0.666404\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch17.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch17.ipynb
new file mode 100755
index 00000000..77951e94
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch17.ipynb
@@ -0,0 +1,446 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:82e0373b19da96ab8fd50304caf9cd3e08cf8bad10412b0998bf9110f7a5ae63"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 17 : Design of Catalytic Reactors"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 434\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dt=[0.081,0.205,3.6]; #Reactor diameter for the three reactors in m\n",
+      "dte=[0.04,0.12,0.70]; #Equivalent diameters for the three reactors in m\n",
+      "db=[0.05,0.057,0.07]; #Estimated bubble size in the three reactors in m\n",
+      "Kr1=1.3889;           #Kinet1ic constant for Reaction 1 in s**-1\n",
+      "Kr2=0.6111;           #Kinetic constant for Reaction 2 in s**-1\n",
+      "Kr3=0.022;            #Kinetic constant for Reaction 3 in s**-1\n",
+      "dp=60.;               #Particle size in micrometer\n",
+      "ephsilonm=0.50;       #Void fraction of fixed bed\n",
+      "ephsilonmf=0.55;      #Void fraction at minimum fluidized condition\n",
+      "umf=0.006;            #Velocity at minimum fluidization condition in m/s\n",
+      "D=2E-5;               #Diffusion coefficient of gas in m**2/s\n",
+      "gammab=0.005;         #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "uo=0.2;               #Superficial gas velocity in m/s\n",
+      "XA=0.9;               #Conversion\n",
+      "g=9.81;               #Acceleration due to gravity in square m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "Kr12=Kr1+Kr2;\n",
+      "n=len(dt);\n",
+      "i=0;\n",
+      "ubr = [0,0,0]\n",
+      "ub = [0,0,0]\n",
+      "delta = [0,0,0]\n",
+      "ephsilonf = [0,0,0]\n",
+      "gammac = [0,0,0]\n",
+      "gammae = [0,0,0]\n",
+      "Kbc = [0,0,0]\n",
+      "Kce = [0,0,0]\n",
+      "Kf12 = [0,0,0]\n",
+      "Kf3 = [0,0,0]\n",
+      "KfA = [0,0,0]\n",
+      "KfAR = [0,0,0]\n",
+      "KfAR1 = [0,0,0]\n",
+      "tou = [0,0,0]\n",
+      "y = [0,0,0]\n",
+      "SR = [0,0,0]\n",
+      "XA1 = [0,0,0]\n",
+      "y1 = [0,0,0]\n",
+      "y2 = [0,0,0]\n",
+      "tou2 = [0,0,0]\n",
+      "Lf = [0,0,0]\n",
+      "Lm = [0,0,0]\n",
+      "XA2 = [0,0,0]\n",
+      "\n",
+      "import math\n",
+      "while i<n:\n",
+      "    #Preliminary Calcualtions\n",
+      "    ubr[i]=0.711*(g*db[i])**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "    ub[i]=1.55*((uo-umf)+14.1*(db[i]+0.005))*dte[i]**0.32+ubr[i];#Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)\n",
+      "    delta[i]=uo/ub[i];#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "    ephsilonf[i]=1-(1-delta[i])*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "    fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "    gammac[i]=(1-ephsilonmf)*((3/(ubr[i]*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "    gammae[i]=((1-ephsilonmf)*((1-delta[i])/delta[i]))-gammab-gammac[i];#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "    Kbc[i]=4.5*(umf/db[i])+5.85*((D**0.5*g**0.25)/db[i]**(5/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "    Kce[i]=6.77*((D*ephsilonmf*0.711*(g*db[i])**0.5)/db[i]**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "    #Effective rate constant from Eqn.(12.32)\n",
+      "    Kf12[i]=(gammab*Kr12+1/((1/Kbc[i])+(1/(gammac[i]*Kr12+1/((1/Kce[i])+(1/(gammae[i]*Kr12)))))))*(delta[i]/(1-ephsilonf[i]));\n",
+      "    #Rate of reaction 2 for fluidized bed from Eqn.(12.14)\n",
+      "    Kf3[i]=(gammab*Kr3+1/((1/Kbc[i])+(1/(gammac[i]*Kr3+1/((1/Kce[i])+(1/(gammae[i]*Kr3)))))))*(delta[i]/(1-ephsilonf[i]));\n",
+      "    #Rate of raection with respect to A from Eqn.(12.35)\n",
+      "    KfA[i]=((Kbc[i]*Kce[i]/gammac[i]**2+(Kr12+Kce[i]/gammac[i]+Kce[i]/ \\\n",
+      "    gammae[i])*(Kr3+Kce[i]/gammac[i]+Kce[i]/gammae[i]))*delta[i]*Kbc[i] \\\n",
+      "    *Kr12*Kr3/(1-ephsilonf[i]))/(((Kr12+Kbc[i]/gammac[i])* \\\n",
+      "    (Kr12+Kce[i]/gammae[i])+Kr12*Kce[i]/gammac[i])*((Kr3+Kbc[i]/gammac[i])* \\\n",
+      "    (Kr3+Kce[i]/gammae[i])+Kr3*Kce[i]/gammac[i]));\n",
+      "    KfAR[i]=((Kr1/Kr12)*Kf12[i])-KfA[i];#Rate of reaction from Eqn.(12.34)\n",
+      "    KfAR1[i]=((Kr1/Kr12)*Kf12[i]);#Since KfA is small\n",
+      "    #(b)Relate Selectivity with conversion in three reactors\n",
+      "    x=-math.log(1-XA);#The term Kf12*tou in Eqn.(12.26)\n",
+      "    tou[i]=x/Kf12[i];#Residence time from Eqn.(12.26)\n",
+      "    y[i]=(KfAR1[i]/(Kf3[i]-Kf12[i]))*(math.exp(-x)-math.exp(-tou[i]*Kf3[i]));#CR/CAi from Eqn.(12.27)\n",
+      "    SR[i]=y[i]/XA;#Selectivity of R\n",
+      "    #(c)Relate exit composition to space time\n",
+      "    tou1=5;#Space time in s\n",
+      "    XA1[i]=1-math.exp(-Kf12[i]*tou1);#Conversion from Eqn.(12.26)\n",
+      "    y1[i]=((KfAR1[i]/(Kf12[i]-Kf3[i]))*(math.exp(-Kf3[i]*tou1)-math.exp(-Kf12[i]*tou1)));#CR/CAi R from Eqn.(12.27)\n",
+      "    #(d)Calculate height of bed needed to maximize production\n",
+      "    y2[i]=(KfAR1[i]/Kf12[i])*(Kf12[i]/Kf3[i])**(Kf3[i]/(Kf3[i]-Kf12[i]));#CRmax/CAi R from Eqn.(12.37)\n",
+      "    tou2[i]=math.log(Kf3[i]/Kf12[i])/(Kf3[i]-Kf12[i]);#Space time from Eqn.(38)\n",
+      "    Lf[i]=(uo/(1-ephsilonf[i]))*tou2[i];#Length of bed at fully fluidized condition from Eqn.(12.5)\n",
+      "    Lm[i]=Lf[i]*(1-ephsilonf[i])/(1-ephsilonm);#Length of bed when settled\n",
+      "    XA2[i]=1-math.exp(-Kf12[i]*tou2[i]);#Conversion from Eqn.(12.26)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Let Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively'\n",
+      "print '(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo)',\n",
+      "print '\\tReactor No.\\tKf12(s**-1)\\tuo(m/s)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i\n",
+      "     print '\\t\\t%f'%Kf12[i],\n",
+      "     print '\\t%f'%uo\n",
+      "     i=i+1;\n",
+      "\n",
+      "print '\\n(b)Relation between selectivity with conversion'\n",
+      "print '\\n\\tReactor No.\\tKf12(s**-1)\\tSR(mol R formed/mol A reacted)'\n",
+      "i=0\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i,\n",
+      "     print '\\t\\t%f'%Kf12[i],\n",
+      "     print '\\t%f'%SR[i]\n",
+      "     i=i+1;\n",
+      "\n",
+      "print '(c)Relation between exit compostion and space time',\n",
+      "print '\\tReactor No.\\tXA\\t\\tCR/CAi'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i,\n",
+      "     print '\\t\\t%f'%XA1[i],\n",
+      "     print '\\t%f'%y1[i]\n",
+      "     i=i+1;\n",
+      "\n",
+      "print '(d)Height of bed needed to maximize the production of acrylonitrile',\n",
+      "print '\\tReactor No.\\tLm(m)\\t\\tXA'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "     print '\\t%1.0f'%i,\n",
+      "     print '\\t\\t%f'%Lm[i],\n",
+      "     print '\\t%f'%XA2[i]\n",
+      "     i=i+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Let Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively\n",
+        "(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo) \tReactor No.\tKf12(s**-1)\tuo(m/s)\n",
+        "\t0\n",
+        "\t\t0.410042 \t0.200000\n",
+        "\t1\n",
+        "\t\t0.270620 \t0.200000\n",
+        "\t2\n",
+        "\t\t0.128980 \t0.200000\n",
+        "\n",
+        "(b)Relation between selectivity with conversion\n",
+        "\n",
+        "\tReactor No.\tKf12(s**-1)\tSR(mol R formed/mol A reacted)\n",
+        "\t0 \t\t0.410042 \t0.641507\n",
+        "\t1 \t\t0.270620 \t0.618358\n",
+        "\t2 \t\t0.128980 \t0.558283\n",
+        "(c)Relation between exit compostion and space time \tReactor No.\tXA\t\tCR/CAi\n",
+        "\t0 \t\t0.871292 \t0.564802\n",
+        "\t1 \t\t0.741562 \t0.484243\n",
+        "\t2 \t\t0.475286 \t0.313823\n",
+        "(d)Height of bed needed to maximize the production of acrylonitrile \tReactor No.\tLm(m)\t\tXA\n",
+        "\t0 \t\t3.056064 \t0.956404\n",
+        "\t1 \t\t4.137401 \t0.939139\n",
+        "\t2 \t\t7.049378 \t0.897005\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 438\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "deltaHr=5.15E8; #Heat of reaction in J/k mol\n",
+      "W=5E4;          #Weight of acrylonitirle produced per 334-day year in tonnes\n",
+      "db=0.07;        #Estimated bubble size in m\n",
+      "dte=0.7;        #Equivalent diameter in m\n",
+      "Kf12=0.35;      #Effective rate constant in s**-1 from Example 1\n",
+      "dp=60;          #Particle size in micrometer\n",
+      "ephsilonm=0.50; #Void fraction of fixed bed\n",
+      "ephsilonmf=0.55;#Void fraction at minimum fluidized condition\n",
+      "T=460;          #Temperature in reactor in degree C\n",
+      "Pr=2.5;         #Pressure inside reactor in bar\n",
+      "#Feed gas composition\n",
+      "x1=1;           #Propylene\n",
+      "x2=1.1;         #Ammonia\n",
+      "x3=11;          #Air\n",
+      "do1=0.08;       #OD of heat exchanger tubes in m\\\n",
+      "L=7;            #Length of tubes in m\n",
+      "ho=300;         #Outside heat transfer coefficient in W/m**2 K\n",
+      "hi=1800;        #Inside heat transfer coefficient in W/m**2 K\n",
+      "Tc=253.4;       #Temperature of coolant in degree C\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Preliminary calculation\n",
+      "uo=0.46;#Superficial gas velocity from Fig.E1(a) for the value of Kf12 & db\n",
+      "tou=8;#Space time from Fig.E2(b) for highest concentraion of product R\n",
+      "Lm=uo*tou/(1-ephsilonm);\n",
+      "y=0.58;#CR/CAi from Fig.E1(c) for the value of tou & Kf12\n",
+      "XA=0.95#From Fig.E1(c) for the value of tou & Kf12\n",
+      "SR=y/XA;#Selectivity of R\n",
+      "\n",
+      "#Cross-sectional area of the reactor\n",
+      "P=W*10**3/(334*24*3600);#Production rate of acrylonitrile\n",
+      "F=(P/0.053)/(SR*XA/0.042);#Feed rate of propylene\n",
+      "V=((F*22.4*(T+273)*(x1+x2+x3))/(42*273*Pr));\n",
+      "At=V/uo;#Cross-sectional area of reactor needed for the fluidized bed\n",
+      "\n",
+      "#Heat exchanger calculation\n",
+      "q=F*XA*deltaHr/42;#Rate of heat liberation in the reactor\n",
+      "U=(ho**-1+hi**-1)**-1;#Overall heat transfer coefficient\n",
+      "deltaT=T-Tc;#Driving force for heat transfer\n",
+      "Aw=q/(U*deltaT);#Heat exchanger area required to remove q\n",
+      "Nt=Aw/(pi*do1*L);\n",
+      "li1=(At/Nt)**0.5;#Pitch for square pitch arrangement\n",
+      "dte1=4*(li1**2-(pi/4)*do1**2)/(pi*do1);\n",
+      "if dte1>dte:\n",
+      "    li=(pi/4*dte*do1+pi/4*do1**2)**0.5;#Pitch if we add dummy tubes\n",
+      "import math\n",
+      "f=li**2-pi/4*do1**2;#Fraction of bed cross section taken up by tubes\n",
+      "dt1=math.sqrt(4/pi*At/(1-f));#Reactor diameter including all its tubes\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Superficial gas velocity=%fm/s'%uo\n",
+      "print 'No. of %1.0fm tubes required=%1.0f'%(L,Nt);\n",
+      "print 'Reactor diameter=%fm'%dt1\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Superficial gas velocity=0.460000m/s\n",
+        "No. of 7m tubes required=295\n",
+        "Reactor diameter=7.173176m\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 444\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "db=0.08;       #Estimated bubble size in m\n",
+      "dte=2;         #Equivalent diameter in m\n",
+      "F1=55.6;       #Feed rate of oil in kg/s\n",
+      "XA=0.63;       #Conversion\n",
+      "uo=0.6;        #Superficial gas velocity in m/s\n",
+      "T1=500.0;      #Temperature of reactor in degree C\n",
+      "T2=580.0;      #Temperature of regenerator in degree C\n",
+      "Fs=F1*23.3;    #Solid circulation rate from Ex.(15.2)\n",
+      "rhos=1200.0;   #Density of catalyst in kg/m**3\n",
+      "dpbar=60.0;    #Average particle size in micrometer\n",
+      "ephsilonm=0.50;#Void fraction of fixed bed\n",
+      "ephsilonmf=0.55;#Void fraction at minimum fluidized condition\n",
+      "umf=0.006;      #Velocity at minimum fluidization condition in m/s\n",
+      "dt=8.0;         #Diameter of reactor in m\n",
+      "D=2E-5;         #Diffusion coefficient of gas in m**2/s\n",
+      "Kr=8.6;         #Rate constant for reaction at 500 degree C in s**-1\n",
+      "Ka1=0.06;       #Rate constant for deactivatiion at 500 degree C in s**-1\n",
+      "Ka2=0.012;      #Rate constant for regeneration at 580 degree C in s**-1\n",
+      "gammab=0.005;   #Ratio of volume of dispersed solids to that of bubble phase\n",
+      "g=9.81;         #Acceleration due to gravity in square m/s**2\n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Parameters for the fluidized reactor\n",
+      "ubr=0.711*(g*db)**0.5;#Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub=1.55*((uo-umf)+14.1*(db+0.005))*dte**0.32+ubr;#Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)\n",
+      "delta=uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "ephsilonf=1-(1-delta)*(1-ephsilonmf);#Void fraction of fixed bed from Eqn.(6.20)\n",
+      "fw=0.6;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "gammac=(1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);#Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;#Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "Kbc=4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5.0/4));#Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "Kce=6.77*((D*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;#Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "import math\n",
+      "#Bed height versus catalyst activity in reactor\n",
+      "a1bar=0.07;#Guess value for average activity in reactor\n",
+      "x=Kr*a1bar;#Value of Kra1 to be used in the following equation\n",
+      "Kf=(gammab*x+1/((1/Kbc)+(1/(gammac*x+1/((1/Kce)+(1/(gammae*x)))))))*(delta/(1-ephsilonf));#Effective rate constant from Eqn.(12.14)\n",
+      "tou=-math.log(1-XA)/Kf;#Space time from Eqn.(12.16)\n",
+      "Lm=tou*uo/(1-ephsilonm);#Length of fixed bed for guess value of a1bar\n",
+      "a1bar1=[0.0233,0.0465,0.0698,0.0930,0.116,0.140];#Various activity values to find Lm\n",
+      "x1 = [0,0,0,0,0,0]\n",
+      "Kf1 = [0,0,0,0,0,0]\n",
+      "tou1 = [0,0,0,0,0,0]\n",
+      "Lm1 = [0,0,0,0,0,0]\n",
+      "\n",
+      "n=len(a1bar1);\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    x1[i]=Kr*a1bar1[i];\n",
+      "    Kf1[i]=(gammab*x1[i]+1/((1/Kbc)+(1/(gammac*x1[i]+1/((1/Kce)+ \\\n",
+      "    (1/(gammae*x1[i])))))))*(delta/(1-ephsilonf));\n",
+      "    #Effective rate constant from Eqn.(12.14)\n",
+      "    \n",
+      "    tou1[i]=-math.log(1-XA)/Kf1[i];#Space time from Eqn.(12.16)\n",
+      "    Lm1[i]=tou1[i]*uo/(1-ephsilonm);\n",
+      "    #Length of fixed bed for guess value of a1bar...Condition [i]\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Find the optimum size ratio for various a1bar\n",
+      "Lm=[5,6,7,8,10,12];\n",
+      "W1 = [0,0,0,0,0,0]\n",
+      "t1bar = [0,0,0,0,0,0]\n",
+      "t2bar = [0,0,0,0,0,0]\n",
+      "a1bar2 = [0,0,0,0,0,0]\n",
+      "m=len(Lm);\n",
+      "i=0;\n",
+      "while i<m:\n",
+      "    W1[i]=(pi/4)*dt**2*rhos*(1-ephsilonm)*Lm[i];#Bed weight\n",
+      "    t1bar[i]=W1[i]/Fs;#Mean residence time of solids in reactor\n",
+      "    t2bar[i]=t1bar[i]*(Ka1/Ka2)**0.5;#Mean residence time of soilds at optimum from Eqn.(16)\n",
+      "    a1bar2[i]=(Ka2*t2bar[i])/(Ka1*t1bar[i]+Ka1*t1bar[i]*Ka2*t2bar[i]+Ka2*t2bar[i]);#From Eqn.(15)...Condition (ii)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Final design values\n",
+      "Lm4=7.3;#For satisfying condition [i] & (ii)\n",
+      "a1bar3=0.0744;#By interpolation\n",
+      "x2=a1bar3*Kr;\n",
+      "W11=(pi/4)*dt**2*rhos*(1-ephsilonm)*Lm4;#Bed weight for reactor\n",
+      "t1bar1=W11/Fs;#Mean residence time of solids in reactor\n",
+      "a2bar=(1+Ka1*t1bar1)*a1bar3;#Average activity in regenrator from Eqn.(10)\n",
+      "t2bar1=t1bar1*(Ka1/Ka2)**0.5;#Mean residence time of solids in regenerator from Eqn.(16)\n",
+      "W2=W11*(t2bar1/t1bar1);#Bed weight for regenerator\n",
+      "dt2=dt*(W2/W11)**0.5;#Diameter of regenerator assuming same static bed height for reactor and regerator\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Bed height versus catalyst activity in reactor'\n",
+      "print '\\tAverage activity',\n",
+      "print '\\tLength of fixed bed(m)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '\\t%f'%a1bar1[i],\n",
+      "    print '\\t\\t%f'%Lm1[i];\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Optimum size ratio for various activity in reactor'\n",
+      "print '\\tLength of fixed bed(m)',\n",
+      "print '\\tAverage activity'\n",
+      "i=0\n",
+      "while i<m:\n",
+      "    print '\\t%f'%Lm[i],\n",
+      "    print '\\t\\t%f'%a1bar2[i]\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Final design values'\n",
+      "print '\\tDiameter of reactor(m):%.0f'%dt\n",
+      "print '\\tBed weight for reactor(tons):%.0f'%(W11/10**3)\n",
+      "print '\\tBed weight for regenerator(tons):%.0f'%(W2/10**3)\n",
+      "print '\\tDiameter of regenerator(m):%.0f'%(dt2);\n",
+      "print '\\tSolid circulation rate(tons/hr):%f'%(Fs*3.6);\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Bed height versus catalyst activity in reactor\n",
+        "\tAverage activity \tLength of fixed bed(m)\n",
+        "\t0.023300 \t\t11.059747\n",
+        "\t0.046500 \t\t7.911053\n",
+        "\t0.069800 \t\t6.756202\n",
+        "\t0.093000 \t\t6.118750\n",
+        "\t0.116000 \t\t5.696470\n",
+        "\t0.140000 \t\t5.372072\n",
+        "Optimum size ratio for various activity in reactor\n",
+        "\tLength of fixed bed(m) \tAverage activity\n",
+        "\t5.000000 \t\t0.097879\n",
+        "\t6.000000 \t\t0.086112\n",
+        "\t7.000000 \t\t0.076871\n",
+        "\t8.000000 \t\t0.069420\n",
+        "\t10.000000 \t\t0.058149\n",
+        "\t12.000000 \t\t0.050026\n",
+        "Final design values\n",
+        "\tDiameter of reactor(m):8\n",
+        "\tBed weight for reactor(tons):220\n",
+        "\tBed weight for regenerator(tons):492\n",
+        "\tDiameter of regenerator(m):12\n",
+        "\tSolid circulation rate(tons/hr):4663.728000\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch18.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch18.ipynb
new file mode 100755
index 00000000..281bc4a5
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch18.ipynb
@@ -0,0 +1,570 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:3eba5bf9f8e98dcb46f4a3b03f9f7fa4b342f8fb2d0d8b697e9a50303c32aa8f"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 18 : The Design of Noncatalytic Gas Solid Reactors"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 456\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "xA=0.08;      #Fraction of oxygen in stream\n",
+      "dp=[2,0.1];   #Particle diameter in mm\n",
+      "rhos=4130;    #Density of catalyst in kg/m**3\n",
+      "Ds=8E-6;      #Diffusion coefficient of solid in m**2/s\n",
+      "kc=0.02;      #Reaction rate constant in m/s\n",
+      "P=10**5;      #Pressure in bar\\\n",
+      "R=8.314;      #Universal gas constant\n",
+      "T=900;        #Temperature in degree C\n",
+      "mB=0.09745;   #Molecular weight of ZnS in kg/mol\n",
+      "\n",
+      "#CALCULATION\n",
+      "b=2.0/3;#Stoichiometric coefficient of ZnS in the reaction equation\n",
+      "CA=xA*P/(R*(T+273));#Concentration of Oxygen\n",
+      "rhob=rhos/mB;       #Molar density of pure solid\n",
+      "n=len(dp);\n",
+      "i=0;\n",
+      "kbar = [0,0]\n",
+      "tou = [0,0]\n",
+      "while i<n:\n",
+      "    kbar[i]=(kc**-1+(dp[i]*10**-3/(12.0*Ds)))**-1;#Average reaction rate constant from Eqn.(11)\n",
+      "    tou[i]=rhob*dp[i]*10**-3/(2*b*kbar[i]*CA);#Time for complete reaction in seconds from Eqn.(9)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Particle Size(mm)\\tAverage rate constant(m/s)\\tTime for complete reaction(min)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f\\t\\t%f\\t\\t\\t%.2f'%(dp[i],kbar[i],tou[i]/60.0);\n",
+      "    i=i+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Particle Size(mm)\tAverage rate constant(m/s)\tTime for complete reaction(min)\n",
+        "2.000000\t\t0.014118\t\t\t91.49\n",
+        "0.100000\t\t0.019592\t\t\t3.30\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 457\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "xA=0.08;   #Fraction of oxygen in stream\n",
+      "dp=1;      #Particle diameter in mm\n",
+      "rhos=2200; #Density of catalyst in kg/m**3\n",
+      "kc=0.2;    #Reaction rate constant in m/s\n",
+      "mC=0.012;  #Molecular weight of carbon in kg/mol\n",
+      "P=10**5;   #Pressure in bar\\\n",
+      "R=8.314;   #Universal gas constant\n",
+      "T=900;     #Temperature in degree C\n",
+      "\n",
+      "#CALCULATION\n",
+      "b=1;#Stoichiometric coefficient of C in the reaction equation\n",
+      "CA=xA*P/(R*(T+273));#Concentration of Oxygen\n",
+      "rhob=rhos/mC;#Molar density of pure solid reactant\n",
+      "tou=rhob*10**-3/(2*b*kc*CA);#Time required for complete reaction in seconds\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The time required for complete combustion:%.1fmins'%(tou/60);"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The time required for complete combustion:9.3mins\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 462\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "from numpy import zeros\n",
+      "\n",
+      "\n",
+      "#INPUT\n",
+      "dp = 110.;#Particle size in micrometer\n",
+      "T = 900.;#Temperature of roaster in degree C\n",
+      "tbar1 = [3.,10.,30.,50.];#Reported average time in min\n",
+      "XBbarr = [0.840,0.940,0.985,0.990];#Reported value of average conversion\n",
+      "tbar = 3.;\n",
+      "XBbar = 0.840;#Average conversion for tbar  =  3 mins\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Uniform-Reaction Model\n",
+      "x = (1./tbar)*(1./(1-XBbar)-1);#Term KrCA of Eqn.(20)\n",
+      "n = len(tbar1);\n",
+      "i = 0;\n",
+      "XBbar1 = zeros(n)\n",
+      "while i<  n:\n",
+      "    XBbar1[i] = 1-1./(1+x*tbar1[i]);#Average conversion umath.sing calculated value of KrCA from Eqn.(20)\n",
+      "    i = i+1;\n",
+      "\n",
+      "#Shrinking-Core, Rection Control\n",
+      "touguess = 2;#Guess value of tou\n",
+      "def solver_func(tou):#Function defined for solving the system\n",
+      "    return (1-XBbar)-(0.25*tou/tbar)+(0.05*(tou/tbar)**2)-((1./120)*(tou/tbar)**3);\n",
+      "\n",
+      "tou = fsolve(solver_func,touguess)\n",
+      "i = 0;\n",
+      "XBbar2 = zeros(n)\n",
+      "while i<n:\n",
+      "    XBbar2[i] = 1-(0.25*tou/tbar1[i])+(0.05*(tou/tbar1[i])**2)-((1./120)*(tou/tbar1[i])**3);#Average conversion umath.sing calculated value of tou from Eqn.(23)\n",
+      "    i = i+1;\n",
+      "\n",
+      "#Shrinking-Core, Diffusion Control\n",
+      "touguess1 = 2;#Guess value of tou\n",
+      "def solver_func1(tou):      #Function defined for solving the system\n",
+      "    fn = (1-XBbar)-(1./5*tou/tbar)+(19./420*(tou/tbar)**2)-(41./4620*(tou/tbar)**3)+(0.00149*(tou/tbar)**4);\n",
+      "\n",
+      "tou1 = fsolve(solver_func1,touguess1)\n",
+      "i = 0;\n",
+      "XBbar3 = zeros(n)\n",
+      "while i< n:\n",
+      "    #Average conversion umath.sing calculated value of tou from Eqn.(23)\n",
+      "    XBbar3[i] = 1-(1./5*tou1/tbar1[i])+(19./420*(tou1/tbar1[i])**2)-(41./4620*(tou1/tbar1[i])**3)+(0.00149*(tou1/tbar)**4);\n",
+      "    i = i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\t\\t\\t\\tXBbar calculated for Models';\n",
+      "print 'Reported Data';\n",
+      "print 'tbarmin)\\tXBbar\\tUniform Reaction\\tShrinking-Core%( Rection Control\\t\\tShrinking-Core, Diffusion Control'\n",
+      "i = 0\n",
+      "while i< n:\n",
+      "    print '%f\\t%f\\t%f\\t\\t%f\\t\\t\\t\\t%f'%(tbar1[i],XBbarr[i],XBbar1[i],XBbar2[i],XBbar3[i]);\n",
+      "    i = i+1;\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\t\t\t\tXBbar calculated for Models\n",
+        "Reported Data\n",
+        "tbarmin)\tXBbar\tUniform Reaction\tShrinking-Core%( Rection Control\t\tShrinking-Core, Diffusion Control\n",
+        "3.000000\t0.840000\t0.840000\t\t0.840000\t\t\t\t0.884437\n",
+        "10.000000\t0.940000\t0.945946\t\t0.947234\t\t\t\t0.962033\n",
+        "30.000000\t0.985000\t0.981308\t\t0.981898\t\t\t\t0.987159\n",
+        "50.000000\t0.990000\t0.988701\t\t0.989075\t\t\t\t0.992366\n"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stderr",
+       "text": [
+        "/usr/lib/python2.7/dist-packages/scipy/optimize/minpack.py:227: RuntimeWarning: The iteration is not making good progress, as measured by the \n",
+        "  improvement from the last ten iterations.\n",
+        "  warnings.warn(msg, RuntimeWarning)\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 462\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "from numpy import zeros\n",
+      "\n",
+      "\n",
+      "#INPUT\n",
+      "W = 1;          #Bed weight in kg\n",
+      "F1 = 0.01;      #Solid feed rate in kg/min\n",
+      "dp = [200.,600.];           #Particle size in micrometer\n",
+      "XBbar = [0.85,0.64];        #Average conversion for corresponding particle sizes\n",
+      "rhos = 2500.;               #Density of solid in kg/m**3\n",
+      "ephsilonm = 0.4;            #Void fracton of fixed bed\n",
+      "F11 = 4.;                   #Feed rate of solids in tons/hr\n",
+      "XBbar1 = 0.98;\n",
+      "dp1 = 600.;\n",
+      "pi = 3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Shrinking-Core, Rection Control\n",
+      "n = len(dp);\n",
+      "i = 0;\n",
+      "touguess = 2;#Guess value of tou\n",
+      "tou = zeros(n)\n",
+      "while i< n:\n",
+      "    def solver_func2(t):  #Function defined for solving the system\n",
+      "        return  (1-XBbar[i])-(0.25*t/107)+(0.05*(t/107.)**2)-((1./120)*(t/107.)**3)\n",
+      "    tou[i] = fsolve(solver_func2,touguess)\n",
+      "    i = i+1;\n",
+      "\n",
+      "tou1 = tou[1];\n",
+      "#For a math.single stage fluidized roaster\n",
+      "tbar1 = 0.25*(tou1/(1-XBbar1))/60.;          #Mean residence time of solids in reactor in hr from Eqn.(24)\n",
+      "W1 = F11*tbar1;\n",
+      "dtguess = 2.;                    #Guess value of tou\n",
+      "def solver_func3(dt):           #Function defined for solving the system\n",
+      "    return  W1*10**3-(pi/4.)*dt**2*0.5*dt*rhos*(1-ephsilonm);#Since Lm = 0.5dt\n",
+      "\n",
+      "dt = fsolve(solver_func3,dtguess)\n",
+      "Lm = dt/2.;#Length of bed required\n",
+      "\n",
+      "#For a two-stage fluidized roaster\n",
+      "tbar2 = tou1*math.sqrt(1./(20*(1-XBbar1)))/60;      #Mean residence time of solids in reactor in hr from Eqn.(30)\n",
+      "W2 = F11*tbar2;\n",
+      "dtguess1 = 2;                   #Guess value of tou\n",
+      "def solver_func4(dt):           #Function defined for solving the system\n",
+      "    return W2*10**3-(pi/4.)*dt**2*0.5*dt*rhos*(1-ephsilonm);       #Since Lm = 0.5dt\n",
+      "\n",
+      "dt1 = fsolve(solver_func4,dtguess)\n",
+      "Lm1 = dt1/2.;           #Length of bed required\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Single stage fluidized roaster';\n",
+      "print '\\tWeight of bed needed:%ftons'%(W1);\n",
+      "print '\\tDiameter of reactor:%fm'%(dt);\n",
+      "print '\\tLength of bed:%fm'%(Lm);\n",
+      "print 'Two-stage fluidized roaster';\n",
+      "print '\\tWeight of bed needed:%ftons'%(W2);\n",
+      "print '\\tDiameter of reactor:%fm'%(dt1);\n",
+      "print '\\tLength of bed:%fm'%(Lm1);\n",
+      "print 'These results show that this operation can be accomplished in a math.single bed of %ftons or in two beds of %f tons each.'%(W1,W2);\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Single stage fluidized roaster\n",
+        "\tWeight of bed needed:174.370805tons\n",
+        "\tDiameter of reactor:6.665728m\n",
+        "\tLength of bed:3.332864m\n",
+        "Two-stage fluidized roaster\n",
+        "\tWeight of bed needed:22.056356tons\n",
+        "\tDiameter of reactor:3.346064m\n",
+        "\tLength of bed:1.673032m\n",
+        "These results show that this operation can be accomplished in a math.single bed of 174.370805tons or in two beds of 22.056356 tons each.\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 5, Page 468\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "from numpy import zeros\n",
+      "\n",
+      "#INPUT\n",
+      "T = 900;                #Temperature in roaster in degree C\n",
+      "P = 101325;             #Pressure in Pa\n",
+      "R = 8.314;              #Universal gas consmath.tant\n",
+      "dpbar = 150;            #Average particle size in micrometer\n",
+      "rhosbar = 4130;         #Average particle density in kg/m**3\n",
+      "kc = 0.015              #Rate consmath.tant in m/s for reaction which follows shrinking core model\n",
+      "Ds = 8E-6;              #Diffusion coefficient of solid in m**2/s\n",
+      "uo = 0.6;               #Superficial gas velocity in m/s\n",
+      "D = 2.3E-4;             #Diffusion coefficient of gas in m**2/s\n",
+      "Lm = 1;                 #Length of fixed bed in m\n",
+      "dte = 0.4;              #Equivalent diameter of bed\n",
+      "umf = 0.025;            #Velocity at minimum fluidization condition in m/s\n",
+      "ephsilonm = 0.45;       #Void fraction of fixed bed\n",
+      "ephsilonmf = 0.50;      #Void fraction at minimum fluidized condition\n",
+      "db = 0.2;               #Estimated bubble size in m\n",
+      "gammab = 0.005;         #Ratio of volume of print ersed solids to that of bubble phase\n",
+      "Fo = 2;                 #Feed rate of solids in kg/s\n",
+      "XA = 0.6677;            #Conversion of Oxygen\n",
+      "xA = 0.21;              #Mole fraction of oxygen in feed\n",
+      "mB = 0.09744;           #Molecular weight of ZnS\n",
+      "F = 0.85;               #Fraction of open area\n",
+      "g = 9.81;               #Acceleration due to gravity in square m/s**2\n",
+      "pi = 3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#(a)Extreme Calculation\n",
+      "a = 3./2;#Stoichiometric coefficient of Oxygen in the reaction equation\n",
+      "At = (Fo/mB)*(a)/(uo*(273./(T+273))*(XA*xA)/0.0224);\n",
+      "dt = math.sqrt(At/F*4/pi);\n",
+      "\n",
+      "#(b)The Three-Step Procedure\n",
+      "#Step 1. Conversion of gas\n",
+      "ubr = 0.711*(g*db)**0.5;                                #Rise velocity of bubble from Eqn.(6.7)\n",
+      "ub = 1.6*((uo-umf)+1.13*db**0.5)*dte**1.35+ubr;         #Bubble rise velocity for Geldart B particle\n",
+      "\n",
+      "delta = uo/ub;#Fraction of bed in bubbles from Eqn.(6.29)\n",
+      "ephsilonf = 1-(1-delta)*(1-ephsilonmf);                 #Void fraction of fixed bed from Eqn.(6.20)\n",
+      "\n",
+      "fw = 0.15;#Wake volume to bubble volume from Fig.(5.8)\n",
+      "gammac = (1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);        #Volume of solids in cloud to that of the bubble from Eqn.(6.36)\n",
+      "gammae = ((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;      #Volume of solids in emulsion to that of the bubble from Eqn.(6.35)\n",
+      "Kbc = 4.5*(umf/db)+5.85*((D**0.5*g**0.25)/db**(5./4));           #Gas interchange coefficient between bubble and cloud from Eqn.(10.27)\n",
+      "Kce = 6.77*((D*ephsilonmf*0.711*(g*db)**0.5)/db**3)**0.5;       #Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)\n",
+      "x = delta*Lm*(1-ephsilonm)/((1-ephsilonf)*uo);                  #Term Lf/ub of Eqn.(12.16) from Eqn.(6.19)\n",
+      "CAi = xA*P/(R*(T+273));                                         #Initial concentration of oxygen\n",
+      "\n",
+      "#Step 2.Conversion of solids\n",
+      "rhob = rhosbar/mB;                                              #Density of ZnS\n",
+      "kbar = (kc**-1+(dpbar*10**-6/(12*Ds))**-1)**-1;                 #Modified rate consmath.tant from Eqn.(11)\n",
+      "tbar = At*Lm*(1-ephsilonm)*rhosbar/Fo;                          #Mean residence time of solids\n",
+      "Krguess = 2;                                                    #Guess value of Kr\n",
+      "def solver_func(Kr):                #Function defined for solving the system\n",
+      "    Kf = gammab*Kr+1/((1./Kbc)+(1./(gammac*Kr+1/((1./Kce)+(1./(gammae*Kr))))));            #Reaction rate for fluidized bed from Eqn.(14)\n",
+      "    XA = 1-math.exp(-x*Kf);                                                         #Conversion of oxygen from Eqn.(42)\n",
+      "    CAbar = (CAi*XA*uo)/(Kr*Lm*(1-ephsilonm));                                      #Average concentration of oxygen from Eqn.(43)\n",
+      "    tou = rhob*dpbar*10**-6*a/(2*kbar*CAbar);                                       #Time for complete reaction from Eqn.(9)\n",
+      "    y = tbar/tou;#Term tbar/tou\n",
+      "    XBbar = 3*y-6*y**2+6*y**3*(1-math.exp(-1/y));                                   #Average conversion of ZnS from Eqn.(22)\n",
+      "    #Step 3. Material balance of both streams\n",
+      "    return (Fo/mB)*XBbar-(At*uo*CAi*XA/a);                                          #From Eqn.(44b)\n",
+      "\n",
+      "Kr = fsolve(solver_func,Krguess)\n",
+      "Kf = gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));             #Reaction rate for fluidized bed from Eqn.(14)\n",
+      "XA = 1-math.exp(-x*Kf);                                                             #Conversion of oxygen from Eqn.(42)\n",
+      "CAbar = (CAi*XA*uo)/(Kr*Lm*(1-ephsilonmf));                                         #Average concentration of oxygen from Eqn.(43)\n",
+      "tou = rhob*dpbar*10**-6*a/(2*kbar*CAbar);                                           #Time for complete reaction from Eqn.(9)\n",
+      "y = tbar/tou;                                                                       #Term tbar/tou\n",
+      "XBbar = 3*y-6*y**2+6*y**3*(1-math.exp(-1/y));                                       #Average conversion of ZnS from Eqn.(22)\n",
+      "\n",
+      "\n",
+      "#(c) For other feed rates of solids\n",
+      "F1 = [2,2.5,3,3.5];#Various feed rates of solids in kg/s\n",
+      "n = len(F1)\n",
+      "i = 0;\n",
+      "tbar1 = zeros(n)\n",
+      "Kr1 = zeros(n)\n",
+      "XA1 = zeros(n)\n",
+      "y1 = zeros(n)\n",
+      "tou1 = zeros(n)\n",
+      "XBbar1 = zeros(n)\n",
+      "Kf1 = zeros(n)\n",
+      "CAbar1 = zeros(n)\n",
+      "Krguess1 = 2;           #Guess value of Kr\n",
+      "while i<  n:\n",
+      "    tbar1[i] = At*Lm*(1-ephsilonm)*rhosbar/F1[i];#Mean residence time of solids\n",
+      "    def solver_func1(Kr):               #Function defined for solving the system\n",
+      "        Kf1 = gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));#Reaction rate for fluidized bed from Eqn.(14)\n",
+      "        XA1 = 1-math.exp(-x*Kf1);#Conversion of oxygen from Eqn.(42)\n",
+      "        CAbar1 = (CAi*XA1*uo)/(Kr*Lm*(1-ephsilonm));#Average concentration of oxygen from Eqn.(43)\n",
+      "        tou1 = rhob*dpbar*10**-6*a/(2*kbar*CAbar1);#Time for complete reaction from Eqn.(9)\n",
+      "        y1[i] = tbar1[i]/tou1;#Term tbar/tou\n",
+      "        XBbar1[i] = 3*y1[i]-6*y1[i]**2+6*y1[i]**3*(1-math.exp(-1/y1[i]));#Average conversion of ZnS from Eqn.(22)\n",
+      "        #Step 3. Material balance of both streams\n",
+      "        return (F1[i]/mB)*XBbar1[i]-(At*uo*CAi*XA1/a);#From Eqn.(44b)\n",
+      "\n",
+      "    Kr1[i] = fsolve(solver_func1,Krguess1)\n",
+      "    Kf1[i] = gammab*Kr1[i]+1/((1/Kbc)+(1/(gammac*Kr1[i]+1/((1/Kce)+(1/(gammae*Kr1[i]))))));#Reaction rate for fluidized bed from Eqn.(14)\n",
+      "    XA1[i] = 1-math.exp(-x*Kf1[i]);#Conversion of oxygen from Eqn.(42)\n",
+      "    CAbar1[i] = (CAi*XA1[i]*uo)/(Kr1[i]*Lm*(1-ephsilonmf));#Average concentration of oxygen from Eqn.(43)\n",
+      "    tou1[i] = rhob*dpbar*10**-6*a/(2*kbar*CAbar1[i]);#Time for complete reaction from Eqn.(9)\n",
+      "    y1[i] = tbar1[i]/tou1[i];#Term tbar/tou\n",
+      "    XBbar1[i] = 3*y1[i]-6*y1[i]**2+6*y1[i]**3*(1-math.exp(-1/y1[i]));#Average conversion of ZnS from Eqn.(22)\n",
+      "    i = i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Extreme Calculation';\n",
+      "print '\\tDiameter of tube with all its internals:%fm'%(dt);\n",
+      "print 'Three step procedure';\n",
+      "print '\\tConversion of ZnS:%f'%(XBbar);\n",
+      "print 'For other feed rates of solids';\n",
+      "print '\\tFeedkg/s\\ttbars\\t\\tXBbar/XA\\tKrbars**-1\\tCAbar/CAi\\ttous\\t\\tXA\\t\\tXB';\n",
+      "i = 0;\n",
+      "while i<  n:\n",
+      "    print '\\t%f\\t%f\\t%f\\t%f\\t%f\\t%f\\t%f\\t%f'%(F1[i],tbar1[i],XBbar1[i]/XA1[i],Kr1[i],CAbar1[i]/CAi,tou1[i],XA1[i],XBbar1[i]);\n",
+      "    i = i+1;\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Extreme Calculation\n",
+        "\tDiameter of tube with all its internals:7.265465m\n",
+        "Three step procedure\n",
+        "\tConversion of ZnS:0.992491\n",
+        "For other feed rates of solids\n",
+        "\tFeedkg/s\ttbars\t\tXBbar/XA\tKrbars**-1\tCAbar/CAi\ttous\t\tXA\t\tXB\n",
+        "\t2.000000\t40003.518104\t1.498777\t6.529973\t0.121691\t1208.748626\t0.662201\t0.992491\n",
+        "\t2.500000\t32002.814483\t1.201348\t23.149964\t0.041993\t3502.838402\t0.810111\t0.973225\n",
+        "\t3.000000\t26669.012069\t1.007581\t76.183481\t0.014228\t10338.227251\t0.903294\t0.910141\n",
+        "\t3.500000\t22859.153202\t0.871565\t146.263086\t0.007742\t18998.458994\t0.943693\t0.822490\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 6, Page 471\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "from scipy.optimize import fsolve \n",
+      "import math \n",
+      "\n",
+      "\n",
+      "#INPUT\n",
+      "T = 900;                #Temperature in roaster in degree C\n",
+      "P = 101325;             #Pressure in Pa\n",
+      "R = 8.314;              #Universal gas consmath.tant\n",
+      "dp = 750;               #Particle size in micrometer5\n",
+      "Fo = 2.5;               #Feed rate of solids in kg/s\n",
+      "uo = 0.6;               #Superficial gas velocity in m/s\n",
+      "W = 80140;              #Weight of bed in kg\n",
+      "ephsilonmf = 0.50;      #Void fraction at minimum fluidized condition\n",
+      "umf = 0.5;              #Velocity at minimum fluidization condition in m/s\n",
+      "db = 0.2;               #Estimated bubble size in m\n",
+      "g = 9.81;               #Acceleration due to gravity in square m/s**2\n",
+      "Lm = 1;                 #Length of fixed bed in m\n",
+      "ephsilonm = 0.45;       #Void fraction of fixed bed\n",
+      "xA = 0.21;              #Mole fraction of oxygen in feed\n",
+      "kc = 0.015              #Rate consmath.tant in m/s for reaction which follows shrinking core model\n",
+      "Ds = 8E-6;              #Diffusion coefficient of solid in m**2/s\n",
+      "rhosbar = 4130;         #Average particle density in kg/m**3\n",
+      "mB = 0.09744;           #Molecular weight of ZnS\n",
+      "a = 3./2;               #Stoichiometric coefficient of Oxygen in the reaction equation\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Selection of models to represent reactor\n",
+      "ubr = 0.711*(g*db)**0.5;        #Rise velocity of bubble from Eqn.(6.7)\n",
+      "f = ubr/(umf/ephsilonmf);\n",
+      "\n",
+      "#Step 1.\n",
+      "ub = uo-umf+ubr;            #Rise velocity of bubbles from Eqn.(6.8)\n",
+      "delta = (uo-umf)/(ub+2*umf);        #Fraction of the bed in bubbles from Eqn.(6.26)\n",
+      "Krguess = 2;                        #Guess value of Kr\n",
+      "x = Lm*(1-ephsilonm)*umf*(1-delta)/uo**2;\n",
+      "CAi = xA*P/(R*(T+273));             #Initial concentration of oxygen\n",
+      "\n",
+      "#Step 2.\n",
+      "kbar = (kc**-1+(dp*10**-6/(12*Ds))**-1)**-1;            #Modified rate consmath.tant from Eqn.(11)\n",
+      "tbar = W/Fo;                    #Mean residence time of solids from Eqn.(14.2)\n",
+      "rhob = rhosbar/mB;              #Density of ZnS\n",
+      "def solver_func1(Kr):           #Function defined for solving the system\n",
+      "    XA = 1-math.exp(-x*Kr);     #Conversion from Eqn.(42)\n",
+      "    CAbar = (CAi*XA*uo**2)/(Kr*Lm*(1-ephsilonm)*umf*(1-delta));         #Average concentration of oxygen from Eqn.(43)\n",
+      "    tou = rhob*dp*10**-6*a/(2*kbar*CAbar);          #Time for complete reaction from Eqn.(9)\n",
+      "    y = tbar/tou;               #Term tbar/tou\n",
+      "    XBbar = 3*y-6*y**2+6*y**3*(1-math.exp(-1./y));          #Average conversion of ZnS from Eqn.(22)\n",
+      "    return XBbar-1.2*XA;        #From Table E5, for Fo = 2.5kg/s\n",
+      "\n",
+      "Kr = fsolve(solver_func1,Krguess)\n",
+      "XA = 1-math.exp(-x*Kr);         #Conversion from Eqn.(42)\n",
+      "CAbar = (CAi*XA*uo**2)/(Kr*Lm*(1-ephsilonm)*umf*(1-delta))      #Average concentration of oxygen from Eqn.(43)\n",
+      "tou = rhob*dp*10**-6*a/(2*kbar*CAbar);          #Time for complete reaction from Eqn.(9)\n",
+      "y = tbar/tou;                   #Term tbar/tou\n",
+      "XBbar = 3*y-6*y**2+6*y**3*(1-math.exp(-1./y));  #Average conversion of ZnS from Eqn.(22)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Selection of models to represent reactor';\n",
+      "print '\\tSince ratio ubr/umf/ephsilonmf) =  %f <1 the reactor is operating in slow bubble regime'%(f);\n",
+      "print '\\tSince particle size  = %f micrometer they react according to shrinking-core model'%(dp);\n",
+      "print '\\tConversion obtained for %f micrometer particle:%f'%(dp,XBbar);\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Selection of models to represent reactor\n",
+        "\tSince ratio ubr/umf/ephsilonmf) =  0.995908 <1 the reactor is operating in slow bubble regime\n",
+        "\tSince particle size  = 750.000000 micrometer they react according to shrinking-core model\n",
+        "\tConversion obtained for 750.000000 micrometer particle:0.988127\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch3.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch3.ipynb
new file mode 100755
index 00000000..72abab33
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch3.ipynb
@@ -0,0 +1,267 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:c2d23a740208e3823c43d8afcfc0ef305894f28fcd5f9e9793f1f1c6fe8b25f1"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 3 : Fluidization and Mapping of Regimes"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 68\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "weight = [0,60,150,270,330,360.0];        # Weight in grams for the oversized particles\n",
+      "psize = [50,75,100,125,150,175];          #PSD in micrometers\n",
+      "\n",
+      "#CALCULATION\n",
+      "l = len(psize); # To obtain the size of input array\n",
+      "# Computation of sauter mean diameter for the given PSD\n",
+      "i = 0;\n",
+      "dpi = [0,0,0,0,0,0]\n",
+      "weightf = [0,0,0,0,0,0]\n",
+      "dp = [0,0,0,0,0,0]\n",
+      "while i<l-1:\n",
+      "        dpi[i]=(psize[i]+ psize[i+1])/2.0;\n",
+      "        weightf[i]=(weight[i+1]-weight[i])/weight[5];    \n",
+      "        dp[i]=weightf[i]/float(dpi[i]);    \n",
+      "        i=i+1;\n",
+      "\n",
+      "dpbar=1/sum(dp);                        #Calculation of average particle daimeter Eq.(15)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\n The Sauter mean diameter of the material with the given particle size distribution = %.0f micrometer'%dpbar\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        " The Sauter mean diameter of the material with the given particle size distribution = 98 micrometer\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 76\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "#Estimation of Minimum fluidizing velocity\n",
+      "\n",
+      "#INPUT\n",
+      "ephsilon=0.55;     #Void fraction of bed\n",
+      "rhog=0.0012;       #Density of gas in g/cc\n",
+      "myu=.00018;        #Viscosity of gas in g/cm s\n",
+      "dpbar=0.016;       #Mean diameter of solids in centimeter\n",
+      "phis=0.67;         #Sphericity of solids\n",
+      "rhos=2.6;          #Density of solids in g/cc\n",
+      "g=980;             #Acceleration due to gravity in square cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Computation of umf using the simplified equation for small particles\n",
+      "umf=((dpbar**2)*(rhos-rhog)*g*(ephsilon**3)*(phis**2))/(150*myu*(1-ephsilon));#Simplified equation to calculate minimum fluidizing velocity \n",
+      "                                                                              #for small particles Eq.(21)\n",
+      "Re=(dpbar*umf*rhog)/myu;#To calculate Reynolds number for particle\n",
+      "\n",
+      "#Computation of umf if neither void fraction of bed nor sphericity is known\n",
+      "c1=28.7\n",
+      "c2=0.0494;                      #Value of constants from Table 4, page 70\n",
+      "umf1=(myu/(dpbar*rhog))*(((c1**2)+((c2*(dpbar**3)*rhog*(rhos-rhog)*g)/(myu**2)))**0.5-c1); #Equation to calculate minimum fluidizing velocity \n",
+      "                                                                                           #for coarse particles Eq.(25)\n",
+      "err=((umf-umf1)/umf)*100;       #Calculation of error from experimental value\n",
+      "\n",
+      "#OUTPUT\n",
+      "if Re<20:\n",
+      "\tprint 'The particle Reynolds no = %f'%Re\n",
+      "\tprint 'The simplified equation used for calculating minimum fluidizing velocity is valid.'\n",
+      "\n",
+      "print 'The minimum fluidizing velocity by simplified equation for small particles = %.2fcm/s'%umf\n",
+      "print 'The minimum fluidizing velocity by equation for coarse partilces = %.2fcm/s'%umf1\n",
+      "print 'This value is %d percent below the experimentally reported value.'%err\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The particle Reynolds no = 0.427493\n",
+        "The simplified equation used for calculating minimum fluidizing velocity is valid.\n",
+        "The minimum fluidizing velocity by simplified equation for small particles = 4.01cm/s\n",
+        "The minimum fluidizing velocity by equation for coarse partilces = 3.10cm/s\n",
+        "This value is 22 percent below the experimentally reported value.\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 82\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "rhog=1.2e-3;    #Density of air in g/cc\n",
+      "myu=1.8e-4      #Viscosity of air in g/cm s\n",
+      "dpbar=0.016     #Mean diameter of solids in centimeter\n",
+      "phis=0.67;      #Sphericity of solids\n",
+      "rhos=2.6;       #Density of solids in g/cc\n",
+      "g=980           #Acceleration due to gravity in square cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "dpstar=dpbar*((rhog*(rhos-rhog)*g)/myu**2)**(1/3.0);              #Calculation of dimensionless particle size Eq.(31)\n",
+      "utstar=((18/(dpstar**2))+(2.335-(1.744*phis))/(dpstar**0.5))**-1; #Calculation of dimensionless gas velocity Eq.(33)\n",
+      "ut=utstar*((myu*(rhos-rhog)*g)/rhog**2)**(1/3.0);                 #Calculation of terminal velocity of falling particles Eq.(32)\n",
+      "\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The dimensionless particle size = %.2f'%dpstar\n",
+      "print 'The dimensionless gas velocity = %.3f'%utstar\n",
+      "print 'The terminal velocity of falling particles = %d cm/s'%ut\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The dimensionless particle size = 7.28\n",
+        "The dimensionless gas velocity = 1.296\n",
+        "The terminal velocity of falling particles = 88 cm/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 91\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "rhos=1.5;                 #Density of Solid in g/cc\n",
+      "uo1=40; uo2=80;           #Superficial gas velocity in cm/s\n",
+      "dp1=0.006; dp2=0.045;     #Particle size in centimeter\n",
+      "rhog1=1.5E-3; rhog2=1E-3; #Density of gas in g/cc\n",
+      "myu1=2E-4; myu2=2.5E-4;   #Viscosity of air in g/cm s\n",
+      "g=980;                    #Acceleration due to gravity in square cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "#for smaller particles\n",
+      "dpstar1=dp1*((rhog1*(rhos-rhog1)*g)/myu1**2)**(1/3.0);     #Calculation of dimensionless particle diamter Eq.(31)\n",
+      "uostar1=uo1*((rhog1**2)/((myu1)*(rhos-rhog1)*g))**(1/3.0);\n",
+      "uostar2=uo2*((rhog1**2)/((myu1)*(rhos-rhog1)*g))**(1/3.0); #Calculation of dimensionless superficial gas velocity Eq.(32)\n",
+      "\n",
+      "#for larger particles \n",
+      "dpstar2=dp2*((rhog2*(rhos-rhog2)*g)/myu2**2)**(1/3.0);     #Calculation of dimensionless particle diamter Eq.(31)\n",
+      "uostar3=uo1*((rhog2**2)/((myu2)*(rhos-rhog2)*g))**(1/3.0);\n",
+      "uostar4=uo2*((rhog2**2)/((myu2)*(rhos-rhog2)*g))**(1/3.0); #Calculation of dimensionless superficial gas velocity Eq.(32)\n",
+      "\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'For particle of size %.3f centimeter'%dp1\n",
+      "print 'The dimensionless particle diameter = %.2f'%dpstar1\n",
+      "print 'The dimensionless superficial gas velocity = %.4fcm/s(for superficial gas velocity of %dcm/s)'%(uostar1,uo1)\n",
+      "print 'The dimensionless superficial gas velocity = %.3fcm/s(for superficial gas velocity of %dcm/s)'%(uostar2,uo2)\n",
+      "print 'From Fig.16(page 89)comparing u*=%.4f vs dp*=%.2f'%(uostar1,dpstar1)\n",
+      "print 'For Superficial gas velocity =%d Mode of Fluidization:Onset of turbulent fluidization in an ordinary bubbling bed'%(uo1)\n",
+      "print 'From Fig.16(page 89)comparing u* =%.3f vs dp* =%f'%(uostar2,dpstar1)\n",
+      "print 'For Superficial gas velocity =%f Mode of Fluidization:Fast fluidization(requires a circulating solid system)'%(uo2)\n",
+      "print 'For particle of size %f centimeter'%(dp2)\n",
+      "print 'The dimensionless particle diameter = %f'%(dpstar2)\n",
+      "print 'The dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)'%(uostar3,uo1)\n",
+      "print 'The dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)'%(uostar4,uo2)\n",
+      "print 'From Fig.16(page 89)comparing u*=%f vs dp*=%f'%(uostar3,dpstar2)\n",
+      "print 'For Superficial gas velocity =%f Mode of Fluidization:Bublling Fluidization'%(uo1)\n",
+      "print 'From Fig.16(page 89)comparing u* =%f vs dp* =%f'%(uostar4,dpstar2)\n",
+      "print 'For Superficial gas velocity =%f Mode of Fluidization:Bubbling Fluidization'%(uo2)\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "For particle of size 0.006 centimeter\n",
+        "The dimensionless particle diameter = 2.28\n",
+        "The dimensionless superficial gas velocity = 0.7885cm/s(for superficial gas velocity of 40cm/s)\n",
+        "The dimensionless superficial gas velocity = 1.577cm/s(for superficial gas velocity of 80cm/s)\n",
+        "From Fig.16(page 89)comparing u*=0.7885 vs dp*=2.28\n",
+        "For Superficial gas velocity =40 Mode of Fluidization:Onset of turbulent fluidization in an ordinary bubbling bed\n",
+        "From Fig.16(page 89)comparing u* =1.577 vs dp* =2.282737\n",
+        "For Superficial gas velocity =80.000000 Mode of Fluidization:Fast fluidization(requires a circulating solid system)\n",
+        "For particle of size 0.045000 centimeter\n",
+        "The dimensionless particle diameter = 12.890262\n",
+        "The dimensionless superficial gas velocity = 0.558561cm/s(for superficial gas velocity of 40.000000cm/s)\n",
+        "The dimensionless superficial gas velocity = 1.117122cm/s(for superficial gas velocity of 80.000000cm/s)\n",
+        "From Fig.16(page 89)comparing u*=0.558561 vs dp*=12.890262\n",
+        "For Superficial gas velocity =40.000000 Mode of Fluidization:Bublling Fluidization\n",
+        "From Fig.16(page 89)comparing u* =1.117122 vs dp* =12.890262\n",
+        "For Superficial gas velocity =80.000000 Mode of Fluidization:Bubbling Fluidization\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch4.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch4.ipynb
new file mode 100755
index 00000000..cbd2e1e4
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch4.ipynb
@@ -0,0 +1,306 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:66650a76faf5eec3efd8e3c62ecb57addf32e1a6b2cb5d90995ca785777b9427"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 4 :  The Dense Bed"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 106\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "#Variable declaration\n",
+      "dt=4;               #Vessel diameter in m\n",
+      "Lmf=2;              #Length of the bed in m\n",
+      "ephsilonmf=0.48;    #Void fraction of bed\n",
+      "rhos=1500;          #Density of solid in kg/m**3\n",
+      "rhog=3.6;           #Density of gas in kg/m**3\n",
+      "myu=2E-5;           #Viscosity of gas in kg/m s\n",
+      "po=3;               #Pressure of inlet gas in bar\n",
+      "uo=0.4;             #Superficial velocity of gas in m/s\n",
+      "uorm=40;            #Maximum allowable jet velocity from holes in m/s\n",
+      "g=9.80;             #Acceleration due to gravity in m/s**2\n",
+      "gc=1;\n",
+      "pi=3.1428;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Computation of minimum allowable pressure drop through the distributor\n",
+      "deltapb=((1-ephsilonmf)*(rhos-rhog)*g*Lmf)/gc;  #Calculation of pressure drop in bed using Eqn.(3.17)\n",
+      "deltapd=0.3*deltapb;                            #Calculation of pressure drop in distributor using Eqn.(3)\n",
+      "\n",
+      "#Computation of orifice coefficient\n",
+      "Ret=(dt*uo*rhog)/myu;\n",
+      "if Ret>=3000:\n",
+      "    Cd=0.60;\n",
+      "elif Ret>=2000:\n",
+      "    Cd=0.61;\n",
+      "elif Ret>=1000:\n",
+      "    Cd=0.64;\n",
+      "elif Ret>=500:\n",
+      "    Cd=0.68;\n",
+      "elif Ret>=300:\n",
+      "    Cd=0.70;\n",
+      "elif Ret>=100:\n",
+      "    Cd=0.68;\n",
+      "\n",
+      "#Computation of gas velocity through orifice\n",
+      "uor=Cd*((2*deltapd)/rhog)**0.5;   #Calculation of gas velocity through orifice by using Eqn.(12)\n",
+      "f=(uo/uor)*100;                   #Calculation of fraction of open area in the perforated plate \n",
+      "\n",
+      "\n",
+      "#Computation of number of orifices per unit area of distributor\n",
+      "dor=[0.001,0.002,0.004];          #Different orifice diameters in m\n",
+      "n=len(dor);\n",
+      "i=0;\n",
+      "Nor = [0.,0.,0.]\n",
+      "while i<n:\n",
+      "    Nor[i]=(uo*4)/(pi*uor*(dor[i])**2);#Calculation of number of orifices by using Eqn.(13)\n",
+      "    i=i+1;\n",
+      "    \n",
+      "#OUTPUT\n",
+      "print 'The pressure drop in bed:%fPa'%deltapb\n",
+      "print 'The minimum allowable pressure drop in distributor:%fPa'%deltapd\n",
+      "if uor<uorm:\n",
+      "    print 'The gas veleocity of %fm/s is satisfactory'%uor\n",
+      "else:\n",
+      "    print 'The gas veleocity of %fm/s is not satisfactory'%uor\n",
+      "\n",
+      "if f<10:\n",
+      "    print 'The fraction of open area of %f percent is allowable'%f\n",
+      "else:\n",
+      "    print 'The fraction of open area of %f percent is not allowable'%f\n",
+      "\n",
+      "print 'Diameter of orifice(m)',\n",
+      "print '\\tNumber of orifices per unit area(per sq.m)'\n",
+      "\n",
+      "j=0;\n",
+      "while j<n:\n",
+      "    print '%f'%dor[j],\n",
+      "    print '\\t\\t%f'%Nor[j]\n",
+      "    j=j+1;\n",
+      "\n",
+      "print 'This number can be rounded off.'\n",
+      "print 'Since orifices that are too small are liable to clog and those that are too large cause uneven distribution of gas, we choose orifice of diameter %fm'%dor[2]\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The pressure drop in bed:15251.308800Pa\n",
+        "The minimum allowable pressure drop in distributor:4575.392640Pa\n",
+        "The gas veleocity of 30.250265m/s is satisfactory\n",
+        "The fraction of open area of 1.322302 percent is allowable\n",
+        "Diameter of orifice(m) \tNumber of orifices per unit area(per sq.m)\n",
+        "0.001000 \t\t16829.610145\n",
+        "0.002000 \t\t4207.402536\n",
+        "0.004000 \t\t1051.850634\n",
+        "This number can be rounded off.\n",
+        "Since orifices that are too small are liable to clog and those that are too large cause uneven distribution of gas, we choose orifice of diameter 0.004000m\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 108\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "lor=0.1;      #Minimum allowable tuyere spacing in m\n",
+      "uorm=30;      #Maximum allowable jet velocity from the tuyere in m/s\n",
+      "uo=0.4;       #Superficial velocity of gas in m/s\n",
+      "uor=30.2;     #Gas velocity through orifice,from Exa 1, in m/s\n",
+      "Cd=0.6;       #Dicharge coefficient from Exa 1\n",
+      "rhog=3.6      #Density of gas in kg/m**3\n",
+      "pi=3.1428;\n",
+      "\n",
+      "#CALCULATION\n",
+      "Nor=1/(lor**2);                     #Calculation of number of orifices per unit area by assuming minimum spacing for tuyeres\n",
+      "dor=((4/pi)*(uo/uor)*(1/Nor))**0.5; #Calculation of diameter of inlet orifiec by using Eqn.(13)\n",
+      "\n",
+      "#Computation of diameter of hole for different number of holes per tuyere\n",
+      "q=(lor**2)*uo;                      #Volumetric flow rate in m**3/s\n",
+      "Nh=[8.,6.,4.];                         #Different number of holes per tuyere\n",
+      "n=len(Nh);\n",
+      "i=0;\n",
+      "dh = [0.,0.,0.]\n",
+      "while i<n:\n",
+      "    dh[i]=((((q/Nh[i])*(4./pi))/uorm)**0.5);#Calculation of diameter of holes\n",
+      "    i=i+1;\n",
+      "\n",
+      "deltaph=(rhog/2.)*((uor/Cd)**2)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Number of holes(number of holes/tuyeres)',\n",
+      "print '\\tDiameter of hole(m)'\n",
+      "j=0;\n",
+      "while j<n:\n",
+      "    print '%f'%Nh[j],\n",
+      "    print '\\t\\t\\t\\t\\t%f'%dh[j]\n",
+      "    j=j+1;\n",
+      "\n",
+      "print 'The design chosen is as follows'\n",
+      "print '\\tTuyeres are as shown in Fig.2(b),page 97'\n",
+      "print '\\tNumber of holes = %f(Since rectangular pitch is chosen for tuyeres)'%Nh[1]\n",
+      "print '\\tDiameter of hole = %fm'%dh[1]\n",
+      "print '\\tDiameter of incoming high-pressure-drop orifice = %fm ID'%dor\n",
+      "print 'Checking the pressure drop in tuyeres'\n",
+      "print 'Since pressure drop of %.1f Pa gives sufficiently high \\\n",
+      "distributor pressure drop as seen in Exa.1, use of inlet orifice can be dispensed.'%deltaph\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Number of holes(number of holes/tuyeres) \tDiameter of hole(m)\n",
+        "8.000000 \t\t\t\t\t0.004606\n",
+        "6.000000 \t\t\t\t\t0.005318\n",
+        "4.000000 \t\t\t\t\t0.006513\n",
+        "The design chosen is as follows\n",
+        "\tTuyeres are as shown in Fig.2(b),page 97\n",
+        "\tNumber of holes = 6.000000(Since rectangular pitch is chosen for tuyeres)\n",
+        "\tDiameter of hole = 0.005318m\n",
+        "\tDiameter of incoming high-pressure-drop orifice = 0.012984m ID\n",
+        "Checking the pressure drop in tuyeres\n",
+        "Since pressure drop of 4560.2 Pa gives sufficiently high distributor pressure drop as seen in Exa.1, use of inlet orifice can be dispensed.\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "heading",
+     "level": 2,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 110\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "deltapd=[3,10]    #Distributor pressure drop in kPa\n",
+      "deltapd2=10.0;    #Distributor pressure drop in kPa\n",
+      "po=101.0;         #Entering air pressure in kPa\n",
+      "To=20.0;          #Entering air temperature in degree C\n",
+      "y=1.4;            #Fugacity of air\n",
+      "deltapb=10;       #Pressure drop in bed in kPa\n",
+      "p3=103;           #Pressure at the bed exit in kPa\n",
+      "F=8;              #Feed rate of coal in tons/hr\n",
+      "H=25;             #Gross heatig value of coal in MJ/kg\n",
+      "Fa=10;            #Air required at standard condition in nm**3/kg\n",
+      "etac=0.75;        #Efficiency of compressor\n",
+      "etap=36;          #Efficiency of plant in %\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Calculation of volumetric flow rate of air\n",
+      "vo=((F*1000)*Fa*((To+273)/273.0))/3600.0;\n",
+      "\n",
+      "#Case(a) Distributor Pressure drop = 3kPa and Case(b) Distributor Pressure drop = 10kPa\n",
+      "n=len(deltapd);\n",
+      "i=0;\n",
+      "p1= [0,0]\n",
+      "p2 = [0,0]\n",
+      "ws = [0.,0.]\n",
+      "while i<n:\n",
+      "    p2[i]=p3+deltapb;      #Calculation of pressure at the entrance of the bed\n",
+      "    p1[i]=p2[i]+deltapd[i];#Calculation of pressure before entering the bed\n",
+      "    ws[i]=(y/(y-1))*po*vo*((p1[i]/po)**((y-1)/y)-1)*(1.0/etac);#Calculation of power required for the compressor by Eqn.(18) & Eqn.(20)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Case(c) 50% of the required bypassed to burn the volatile gases. Distributor Pressure drop = 3kPa\n",
+      "#No change in pressure drop from case(a)\n",
+      "v1=vo/2.0;   #New volumetric flow rate of air\n",
+      "ws1=455/2.0; #Power required for blower for primary air\n",
+      "ws2=(y/(y-1))*po*v1*((p3/po)**((y-1)/y)-1)*(1/etac);#Power required for blower for bypassed air\n",
+      "wst=ws1+ws2;                #Total power required for the two blowers\n",
+      "p=((ws[1]-wst)/ws[1])*100;  #Saving in power when compared to case(a)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Case(a)'\n",
+      "print '\\tVolumetric flow rate of air = %.2f m**3/hr'%vo\n",
+      "print '\\tPower required for compressor = %.0f kW'%ws[0]\n",
+      "print 'Case(b)'\n",
+      "print '\\tVolumetric flow rate of air = %.2f m**3/hr'%vo\n",
+      "print '\\tPower required for compressor = %.0f kW'%ws[1]\n",
+      "print 'Case(c)'\n",
+      "print '\\tVolumetric flow rate of air = %.3f m**3/hr'%v1\n",
+      "print '\\tPower required for compressor for primary air = %.1f kW'%ws1\n",
+      "print '\\tPower required for blower for bypassed air = %.1f kW'%ws2\n",
+      "print '\\tTotal power required for the two blowers = %.0f kW'%wst\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Case(a)\n",
+        "\tVolumetric flow rate of air = 23.85 m**3/hr\n",
+        "\tPower required for compressor = 454 kW\n",
+        "Case(b)\n",
+        "\tVolumetric flow rate of air = 23.85 m**3/hr\n",
+        "\tPower required for compressor = 651 kW\n",
+        "Case(c)\n",
+        "\tVolumetric flow rate of air = 11.925 m**3/hr\n",
+        "\tPower required for compressor for primary air = 227.5 kW\n",
+        "\tPower required for blower for bypassed air = 31.6 kW\n",
+        "\tTotal power required for the two blowers = 259 kW\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch5.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch5.ipynb
new file mode 100755
index 00000000..791c6af2
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch5.ipynb
@@ -0,0 +1,137 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:502044f71f0f4f73ada9ff3f4a68fa509018810bcbdaf16eaa17d381758e9755"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 5 : Bubbles in Dense Beds"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 126\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dt=60.0;        #ID of tube in cm \n",
+      "dp=300;         #Size of particles of bed in micrometers\n",
+      "umf=3;          #Velocity at minimum fluidization condition in cm/s\n",
+      "ephsilonmf=0.5; #Void fraction of bed at minimum fluidization condition\n",
+      "db=5;           #Diameter of bubble in cm\n",
+      "g=980;          #Acceleration due to gravity in cm/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Computation of rise velocity of bubble\n",
+      "if (db/dt)<0.125:\n",
+      "    ubr=(0.711*((g*db)**0.5));#Rise velocity by Eqn.(3)\n",
+      "elif (db/dt)<0.6:\n",
+      "    ubr=(0.711*((g*db)**0.5))*1.2*exp(-1.49*(db/dt));#Rise velocity by Eqn.(4)   \n",
+      "\n",
+      "#Computation of cloud thickness\n",
+      "Rb=db/2.0;          #Radius of bubble\n",
+      "uf=umf/ephsilonmf;  #Velocity of emulsion gas\n",
+      "Rc=Rb*((ubr+(2*uf))/(ubr-uf))**(1/3.0);#Radius of cloud by Eqn.(6)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'The rise velocity of the bubble=%.1f cm/s'%ubr\n",
+      "print 'The cloud thickness=%.2f cm'%(Rc-Rb)\n",
+      "print 'From Fig.8(page 124)comparing fw vs dp, for dp = %.0f micrometer, wake fraction = 0.24'%dp\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "The rise velocity of the bubble=49.8 cm/s\n",
+        "The cloud thickness=0.30 cm\n",
+        "From Fig.8(page 124)comparing fw vs dp, for dp = 300 micrometer, wake fraction = 0.24\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 132\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "uo=15;     #Superificial gas velocity in cm/s\n",
+      "umf=1;     #Velocity at minimum fluidization condition in cm/s\n",
+      "lor=2.0;   #Pitch of perforated plate in cm\n",
+      "g=980;     #Acceleration due to gravity in cm/s**2\n",
+      "#CALCULATION\n",
+      "#Case(a) For porous plate\n",
+      "dbo1=(2.78/g)*(uo-umf)**2;#Initial bubble size using Eqn.(19)\n",
+      "\n",
+      "#Case(b) For Perforated plate\n",
+      "Nor=(2/math.sqrt(3))*(1/lor)**2;#Number of orifices in cm**-2\n",
+      "dbo2=(1.30/(g**0.2))*((uo-umf)/Nor)**0.4;#Initial bubble size using Eqn.(15) assuming inital bubble size is smaller than hole spacing\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Case(a) For porous plate'\n",
+      "print '\\tInitial bubble size=%.2fcm'%dbo1\n",
+      "print 'Case(b) For Perforated plate'\n",
+      "print '\\tInitial bubble size=%.2fcm'%dbo2\n",
+      "print '\\tSince %f<%f, the equation used is correct.'%(dbo2,lor)"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Case(a) For porous plate\n",
+        "\tInitial bubble size=0.56cm\n",
+        "Case(b) For Perforated plate\n",
+        "\tInitial bubble size=1.55cm\n",
+        "\tSince 1.548765<2.000000, the equation used is correct.\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch6.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch6.ipynb
new file mode 100755
index 00000000..9c4f2311
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch6.ipynb
@@ -0,0 +1,499 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:432c74872bfc5b3cdf6cd2ab6c97c0ab1581b40f382e3a1bf8502ef1c3f981bb"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 6 : Bubbling Fluidized Beds"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 150"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "z=0.5;     #Height of bed in m\n",
+      "dt=0.5;    #ID of tube in m\n",
+      "rhos=1.6;  #Density of catalyst in g/cm**3\n",
+      "dpbar=60.;  #Averge catalyst diameter in micrometer\n",
+      "umf=0.002; #Velocity at minimum fluidization condition in m/s\n",
+      "uo=0.2;    #Superficial velocity in m/s\n",
+      "dor=2.;     #Diameter of orifice in mm\n",
+      "lor=20.;    #Pitch of perforated plate in mm\n",
+      "g=9.80;    #g=980;#Acceleration due to gravity in m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Method 1. Procedure using Eqn.(10) & Eqn.(11)\n",
+      "db=(0.035+0.040)/2.;#Bubble size at z=0.5m from Fig.7(a) & Fig.7(b)\n",
+      "ub1=1+1.55*((uo-umf)+14.1*(db+0.005))*(dt**0.32)*0.711*(g*db)**0.5;#Bubble velocity using Eqn.(10) & Eqn.(11)\n",
+      "\n",
+      "#Method 2. Werther's procedure\n",
+      "si=0.8;#From Fig.6 for Geldart A solids \n",
+      "ub2=si*(uo-umf)+(3.2*(dt**(1./3)))*(0.711*(g*db)**0.5);#Bubble velocity using Eqn.(9)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Method 1. Procedure using Eqn.(10) & Eqn.(11)'\n",
+      "print '\\tDiameter of the bubble=%.4fm'%db\n",
+      "print '\\tRise velocity of the bubble=%.4fm/s'%ub1\n",
+      "print 'Method 2. Werthers procedure'\n",
+      "print '\\tDiameter of the bubble=%fm'%db\n",
+      "print '\\tRise velocity of the bubble=%fm/s'%ub2\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Method 1. Procedure using Eqn.(10) & Eqn.(11)\n",
+        "\tDiameter of the bubble=0.0375m\n",
+        "\tRise velocity of the bubble=1.4267m/s\n",
+        "Method 2. Werthers procedure\n",
+        "\tDiameter of the bubble=0.037500m\n",
+        "\tRise velocity of the bubble=1.253125m/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 151\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "z=0.5;      #Height of bed in m\n",
+      "dt=0.5;     #ID of tube in m\n",
+      "rhos=2.6;   #Density of catalyst in g/cm**3\n",
+      "dpbar=100.; #Averge catalyst diameter in micrometer\n",
+      "umf=0.01;   #Velocity at minimum fluidization condition in m/s\n",
+      "uo=0.45;    #Superficial velocity in m/s\n",
+      "dor=2.;     #Diameter of orifice in mm\n",
+      "lor=30.;    #Pitch of perforated plate in mm\n",
+      "g=9.80;     #Acceleration due to gravity in m/s**2\n",
+      "pi=3.142857;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Part(a).Bubble Size\n",
+      "Nor=(2/math.sqrt(3))*(1/lor**2);\n",
+      "dbo=5.5;\n",
+      "\n",
+      "#Method 1.Werther's procedure for finding bubble size\n",
+      "z1=[0,5,10,20,30,50,70]\n",
+      "db = [0.,0.,0.,0.,0.,0.,0.]\n",
+      "n=len(z1);\n",
+      "i=0; \n",
+      "while i<n:\n",
+      "    db[i]=0.853*((1+0.272*(uo-umf)*100)**(1/3.0))*(1+0.0684*z1[i])**1.21;\n",
+      "    i=i+1;    \n",
+      "\n",
+      "db1=0.163;#Since bubble size starts at dbo=5.5cm at z=0, we shift the curve accordingly to z=0.5m\n",
+      "\n",
+      "#Method 2.Mori and Wen's procedure for finding bubble size\n",
+      "dbm=0.65*((math.pi/4.0)*((dt*100)**2)*(uo-umf)*100)**0.4;\n",
+      "db2=dbm-(dbm-dbo)*math.exp(-0.3**(z/dt));\n",
+      "\n",
+      "#Part(b).Bubble Velocity\n",
+      "#Method 1.Procedure using Eqn.(12)\n",
+      "ub1=1.6*((uo-umf)+1.13*db1**0.5)*(dt**1.35)+(0.711*(g*db1)**0.5);\n",
+      "\n",
+      "#Method 2.Werther's Procedure\n",
+      "si=0.65;\n",
+      "ub2=si*(uo-umf)+2*(dt**0.5)*(0.711*(g*db1)**0.5);\n",
+      "\n",
+      "#Using Eqn.(7) & Eqn.(8)\n",
+      "ubr1=0.711*(g*db1)**0.5;\n",
+      "ubr2=0.711*(g*db2/100.0)**0.5\n",
+      "ub3=uo-umf+ubr1;\n",
+      "ub4=uo-umf+ubr2;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Bubble Size'\n",
+      "print 'Initial bubble size from Fig.5.14 for %.2fm/s = %.2fcm'%(uo-umf,dbo)\n",
+      "print '\\tMethod 1.Werthers procedure for finding bubble size'\n",
+      "print '\\t\\tHeight of bed(cm)'\n",
+      "print '\\t\\t\\tBubble size(cm)'\n",
+      "m=len(z1);\n",
+      "j=0;\n",
+      "while j<m:\n",
+      "    print '\\t\\t%d'%z1[j],\n",
+      "    print '\\t\\t\\t\\t%.2f'%db[j]\n",
+      "    j=j+1;\n",
+      "\n",
+      "print '\\tMethod 2.Mori and Wens procedure for finding bubble size'\n",
+      "print '\\t\\tMaximum expected bubble size=%.2fcm'%dbm\n",
+      "print '\\t\\tBubble size=%.0fcm'%db2\n",
+      "print 'Bubble Velocity'\n",
+      "print '\\tMethod 1.Procedure using Eqn.(12)'\n",
+      "print '\\t\\tBubble velocity=%.2fm/s'%ub1\n",
+      "print '\\tMethod 2.Werthers procedure'\n",
+      "print '\\t\\tBubble velocity=%.2fm/s'%ub2\n",
+      "print 'Comparing the above results with the expressions of the simple two-phase theory'\n",
+      "print '\\tWerthers bubble size'\n",
+      "print '\\tBubble rise velocity=%.2fm/s\\tBubble velocity=%.2fm/s'%(ubr1,ub3)\n",
+      "print '\\tMori & Wens bubble size'\n",
+      "print '\\tBubble rise velocity=%.1fm/s\\tBubble velocity=%.2fm/s'%(ubr2,ub4)\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Bubble Size\n",
+        "Initial bubble size from Fig.5.14 for 0.44m/s = 5.50cm\n",
+        "\tMethod 1.Werthers procedure for finding bubble size\n",
+        "\t\tHeight of bed(cm)\n",
+        "\t\t\tBubble size(cm)\n",
+        "\t\t0 \t\t\t\t2.00\n",
+        "\t\t5 \t\t\t\t2.86\n",
+        "\t\t10 \t\t\t\t3.77\n",
+        "\t\t20 \t\t\t\t5.69\n",
+        "\t\t30 \t\t\t\t7.73\n",
+        "\t\t50 \t\t\t\t12.10\n",
+        "\t\t70 \t\t\t\t16.77\n",
+        "\tMethod 2.Mori and Wens procedure for finding bubble size\n",
+        "\t\tMaximum expected bubble size=61.31cm\n",
+        "\t\tBubble size=20cm\n",
+        "Bubble Velocity\n",
+        "\tMethod 1.Procedure using Eqn.(12)\n",
+        "\t\tBubble velocity=1.46m/s\n",
+        "\tMethod 2.Werthers procedure\n",
+        "\t\tBubble velocity=1.56m/s\n",
+        "Comparing the above results with the expressions of the simple two-phase theory\n",
+        "\tWerthers bubble size\n",
+        "\tBubble rise velocity=0.90m/s\tBubble velocity=1.34m/s\n",
+        "\tMori & Wens bubble size\n",
+        "\tBubble rise velocity=1.0m/s\tBubble velocity=1.43m/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 153\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dpbar=53.;      #Average particle size in micrometer\n",
+      "s=[1,2];        #Size of Bermuda rock in cm \n",
+      "rhosbar=3200.;  #Average solid density of the coke-zircon mixture in kg/m**3\n",
+      "ephsilonm=0.5;  #Void fraction for fixed bed\n",
+      "ephsilonf=0.75; #Void fraction for bubbling bed\n",
+      "rhogbar=0.64;   #Average density of gas in kg/m**3\n",
+      "uo=14.;         #Superficial gas velocity in cm/s\n",
+      "myu=5E-5;       #Viscosity of gas in kg/m s\n",
+      "T=1000.;        #Temperature in degree C\n",
+      "P=1.;           #Pressure in atm\n",
+      "dt=91.5;        #ID of bed in cm\n",
+      "sh=150.;        #Slumped height in cm\n",
+      "\n",
+      "#CALCULATION\n",
+      "rhog2=1.2;      #Density of ambient air\n",
+      "myu2=1.8E-5;    #Viscosity of ambient air\n",
+      "rhos2=rhog2*(rhosbar/rhogbar);#For the requirement of constant density ratio\n",
+      "m=((rhogbar*myu2)/(rhog2*myu))**(2./3);#Scale factor by usin Eqn.(16)\n",
+      "u2=(m**0.5)*uo;  #Superficial gas velocity by using Eqn.(17)\n",
+      "#OUTPUT\n",
+      "print 'For the model use'\n",
+      "print '\\tBed of ID %.2fcm\\tSlumped bed height of %.2fcm\\tPacked bed distributor consisting of %.2f-%.2fmm rock'%(m*dt,m*sh,m*s[0],m*s[1])\n",
+      "print 'Fluidizing gas: ambient air at %.2fatm'%P\n",
+      "print 'Solids: \\tzirconia, Average particle size=%.2fmicrometers'%(m*dpbar)\n",
+      "print 'Entering gas:\\tSuperficial velocity=%.2fcm/s'%u2\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "For the model use\n",
+        "\tBed of ID 30.45cm\tSlumped bed height of 49.92cm\tPacked bed distributor consisting of 0.33-0.67mm rock\n",
+        "Fluidizing gas: ambient air at 1.00atm\n",
+        "Solids: \tzirconia, Average particle size=17.64micrometers\n",
+        "Entering gas:\tSuperficial velocity=8.08cm/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 6
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 159\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "dtb=20;          #ID of bench-scale reactor\n",
+      "dtp=1;           #ID of pilot reactor\n",
+      "dpbar=52;        #Average particle size in micrometer\n",
+      "ephsilonm=0.45;  #Void fraction for fixed bed\n",
+      "ephsilonmf=0.50; #Void fraction at minimum fluidization condition\n",
+      "ephsilonmb=0.60; #Void fraction \n",
+      "uo=30;           #Superficial gas velocity in cm/s\n",
+      "Lmb=2;           #Length of fixed bed in m\n",
+      "umf=0.33;        #Velocity at minimum fluidization condition in cm/s\n",
+      "umb=1;           #Velocity at in cm/s\n",
+      "db=3;            #Equilibrium bubble size in cm\n",
+      "g=9.80;          #Acceleration due to gravity in m/s**2\n",
+      "pi=3.142857;\n",
+      "\n",
+      "#CALCULATION\n",
+      "ubr=0.711*(g*db/100)**0.5;#Rise velocity of bubble using Eqn.(7)\n",
+      "\n",
+      "#Bubble velocity for the bench unit\n",
+      "ubb1=1.55*(((uo-umf)/100.0)+14.1*((db/100.0)+0.005))*((dtb/100.0)**0.32)+ubr;#Bubble velocity using Eqn.(11)\n",
+      "si=1;\n",
+      "ubb2=si*((uo-umf)/100.0)+(3.2*((dtb/100.0)**(1/3.0)))*ubr;#Bubble velocity using Eqn.(9)\n",
+      "ubb=(ubb1+ubb2)/2;#Average bubble velocity\n",
+      "\n",
+      "#Bubble velocity for the pilot unit\n",
+      "ubp1=1.55*(((uo-umf)/100.0)+14.1*((db/100.0)+0.005))*(dtp**0.32)+ubr;#Bubble velocity using Eqn.(11)\n",
+      "si=1;\n",
+      "ubp2=si*((uo-umf)/100)+(3.2*(dtp**(1/3)))*ubr;#Bubble velocity using Eqn.(9)\n",
+      "ubp=(ubp1+ubp2)/2;#Average bubble velocity\n",
+      "\n",
+      "#Rise velocity of upflowing emulsion\n",
+      "ueb=ubb-ubr;#For the bench unit\n",
+      "uep=ubp-ubr;#For the pilot unit\n",
+      "\n",
+      "#Scale-Up Alternative 1.\n",
+      "dteb=20;#Effective bubble diameter\n",
+      "dib=[5,10,15,20];#Different outside diameters\n",
+      "n=len(dib);\n",
+      "li = [0.,0.,0.,0.]\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    li[i]=math.sqrt(((pi*dib[i]*dteb)/4)+((pi/4)*(dib[i])**2));#Pitch using Eqn.(13)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Scale-Up Alternative 2.\n",
+      "Lmp=Lmb*(ubp/ubb);#Static bed height of commercial unit\n",
+      "dtep=100.0;#Effective bubble diameter\n",
+      "dip=[10,15,20,25];#Different outside diameters\n",
+      "m=len(dip);\n",
+      "i=0;\n",
+      "lip = [0.,0.,0.,0.]\n",
+      "while i<m:\n",
+      "    lip[i]=math.sqrt(((math.pi*dip[i]*dtep)/4.0)+(math.pi/4.0)*dip[i]);#Pitch using Eqn.(13)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Height of Bubbling beds\n",
+      "#For bench unit\n",
+      "deltab=((uo/100.0)-(umb/100.0))/(ubb-(umb/100.0));#Fraction of bed in bubbles using Eqn.(28)\n",
+      "ephsilonfb=deltab+(1-deltab)*ephsilonmb;#Void fraction of bubbling bed using Eqn.(20)\n",
+      "Lfb=Lmb*(1-ephsilonm)/(1-ephsilonfb);#Hieght of bubbling bed usnig Eqn.(19)\n",
+      "#For pilot unit\n",
+      "deltap=((uo/100.0)-(umb/100.0))/(ubp-(umb/100.0));#Fraction of bed in bubbles using Eqn.(28)\n",
+      "ephsilonfp=deltap+(1-deltap)*ephsilonmb;#Void fraction of bubbling bed using Eqn.(20)\n",
+      "Lfp=Lmp*(1-ephsilonm)/(1-ephsilonfp);#Hieght of bubbling bed usnig Eqn.(19)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Rise velocity of bubble=%.3fm/s'%ubr\n",
+      "print 'For the bench unit'\n",
+      "print '\\tWith Eqn.(11), Rise velocity=%.3fm/s'%ubb1\n",
+      "print '\\tWith Werthers procedure, Rise velocity=%.2fm/s'%ubb2\n",
+      "print '\\tAverage rise velocity=%.2fm/s'%ubb\n",
+      "print '\\tRise velocity of upflowing emulsion=%.2fm/s'%ueb\n",
+      "print 'For the pilot unit'\n",
+      "print '\\tWith Eqn.(11), Rise velocity=%.2fm/s'%ubp1\n",
+      "print '\\tWith Werthers procedure, Rise velocity=%.2fm/s'%ubp2\n",
+      "print '\\tAverage rise velocity=%.2fm/s'%ubp\n",
+      "print '\\tRise velocity of upflowing emulsion=%.2fm/s'%uep\n",
+      "print 'Scale-Up Alternative 1.'\n",
+      "print '\\tOuter diameter of tube(cm)'\n",
+      "print '\\tPitch(cm)'\n",
+      "n=len(dib);\n",
+      "j=0;\n",
+      "while j<n:\n",
+      "    print '\\t\\t%d'%dib[j],\n",
+      "    print '\\t\\t\\t%.2f'%li[j]\n",
+      "    j=j+1;\n",
+      "\n",
+      "print '\\tSuitable arrangement'\n",
+      "print '\\t\\tOuter Diameter=%dcm\\tPitch:Diameter ratio=%.2f'%(dib[1],(li[1]/dib[1]))\n",
+      "print 'Scale-Up Alternative 2.'\n",
+      "print '\\tStatic bed height for commercial unit=%fm'%Lmp\n",
+      "print '\\tOuter diameter of tube(cm)'\n",
+      "print '\\tPitch(cm)'\n",
+      "n=len(dip);\n",
+      "j=0;\n",
+      "\n",
+      "while j<n:\n",
+      "    print '\\t\\t%d'%dip[j],\n",
+      "    print '\\t\\t\\t%.2f'%lip[j]\n",
+      "    j=j+1;\n",
+      "\n",
+      "print '\\tSuitable arrangement'\n",
+      "print '\\t\\tOuter Diameter=%dcm\\tPitch:Diameter ratio=%.2f'%(dip[2],(lip[2]/dip[2]))\n",
+      "print '\\t\\t\\t\\tFraction of bed in bubbles\\tVoid fraction of bed\\tStatic bed height(m)\\tHeight of bubbling bed(m)'\n",
+      "print '\\t\\t\\t\\t---------------------------------------------------------------------------------------------------------'\n",
+      "print 'Bench unit\\tID=%fm\\t%f\\t\\t\\t%f\\t\\t%f\\t\\t%f'%(dtb/100.,deltab,ephsilonfb,Lmb,Lfb)\n",
+      "print 'Commercial unit\\tID=%fm\\t%f\\t\\t\\t%f\\t\\t%f\\t\\t%f'%(dtp,deltap,ephsilonfp,Lmp,Lfp)\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Rise velocity of bubble=0.386m/s\n",
+        "For the bench unit\n",
+        "\tWith Eqn.(11), Rise velocity=1.117m/s\n",
+        "\tWith Werthers procedure, Rise velocity=1.02m/s\n",
+        "\tAverage rise velocity=1.07m/s\n",
+        "\tRise velocity of upflowing emulsion=0.68m/s\n",
+        "For the pilot unit\n",
+        "\tWith Eqn.(11), Rise velocity=1.61m/s\n",
+        "\tWith Werthers procedure, Rise velocity=1.53m/s\n",
+        "\tAverage rise velocity=1.57m/s\n",
+        "\tRise velocity of upflowing emulsion=1.18m/s\n",
+        "Scale-Up Alternative 1.\n",
+        "\tOuter diameter of tube(cm)\n",
+        "\tPitch(cm)\n",
+        "\t\t5 \t\t\t9.91\n",
+        "\t\t10 \t\t\t15.35\n",
+        "\t\t15 \t\t\t20.31\n",
+        "\t\t20 \t\t\t25.07\n",
+        "\tSuitable arrangement\n",
+        "\t\tOuter Diameter=10cm\tPitch:Diameter ratio=1.54\n",
+        "Scale-Up Alternative 2.\n",
+        "\tStatic bed height for commercial unit=2.941439m\n",
+        "\tOuter diameter of tube(cm)\n",
+        "\tPitch(cm)\n",
+        "\t\t10 \t\t\t28.16\n",
+        "\t\t15 \t\t\t34.49\n",
+        "\t\t20 \t\t\t39.83\n",
+        "\t\t25 \t\t\t44.53\n",
+        "\tSuitable arrangement\n",
+        "\t\tOuter Diameter=20cm\tPitch:Diameter ratio=1.99\n",
+        "\t\t\t\tFraction of bed in bubbles\tVoid fraction of bed\tStatic bed height(m)\tHeight of bubbling bed(m)\n",
+        "\t\t\t\t---------------------------------------------------------------------------------------------------------\n",
+        "Bench unit\tID=0.200000m\t0.274171\t\t\t0.709668\t\t2.000000\t\t3.788769\n",
+        "Commercial unit\tID=1.000000m\t0.185857\t\t\t0.674343\t\t2.941439\t\t4.967774\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 5, Page 161\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dtb=20;          #ID of bench-scale reactor\n",
+      "dtp=1;           #ID of pilot reactor\n",
+      "dpbar=200;       #Average particle size in micrometer\n",
+      "ephsilonmf=0.50; #Void fraction at minimum fluidization condition\n",
+      "ephsilonmb=0.50; #Void fraction \n",
+      "uo=30;           #Superficial gas velocity in cm/s\n",
+      "Lmb=2;           #Length of fixed bed in m\n",
+      "umf=3;           #Velocity at minimum fluidization condition in cm/s\n",
+      "umb=3;           #Velocity at in cm/s\n",
+      "g=9.80;          #Acceleration due to gravity in m/s**2\n",
+      "pi=3.142857;\n",
+      "\n",
+      "#CALCULATION\n",
+      "#In the small bench unit\n",
+      "c=1;\n",
+      "ubb=c*((uo-umf)/100.0)+0.35*(g*(dtb/100.0))**0.5;#Velocity using Eqn.(5.22)\n",
+      "zsb=60*(dtb)**0.175;#Height using Eqn.(5.24)\n",
+      "\n",
+      "#In the large pilot unit\n",
+      "ubp=c*((uo-umf)/100.0)+0.35*(g*dtp)**0.5;#Velocity using Eqn.(5.22)\n",
+      "zsp=60*(dtp*100)**0.175;#Height using Eqn.(5.24)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Condition at which bubbles transform into slugs'\n",
+      "print 'For tha small bench unit\\t\\tVelocity=%fm/s\\t\\tHeight above distributor plate=%fm'%(ubb,zsb/100.)\n",
+      "print 'For tha large pilot unit\\t\\tVelocity=%fm/s\\t\\tHeight above distributor plate=%fm'%(ubp,zsp/100.);\n",
+      "\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Condition at which bubbles transform into slugs\n",
+        "For tha small bench unit\t\tVelocity=0.760000m/s\t\tHeight above distributor plate=1.013518m\n",
+        "For tha large pilot unit\t\tVelocity=1.365673m/s\t\tHeight above distributor plate=1.343233m\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch7.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch7.ipynb
new file mode 100755
index 00000000..aafc2f66
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch7.ipynb
@@ -0,0 +1,399 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:8eb00dc3983a05f0d88bd9a81e8b022860563cdbf1df8dacf4157210feb1c3ce"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 7  : Entrainment and Elutriation  from Fluidized Beds"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 179"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "rhog=5.51;  #Density of gas in kg/m**3\n",
+      "rhos=1200;  #Density of solid in kg/m**3\n",
+      "dpbar=130;  #Average size of particles in micrometer\n",
+      "uo=0.61;    #Superficial gas velocity in m/s\n",
+      "g=9.80;     #Acceleration due to gravity in m/s**2\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Assuming that freeboard in higher than TDH, computation of entrainment rate by Zenz & Weil's method\n",
+      "x=(uo**2)/(g*(dpbar*10**-6)*rhos**2);#Calculation of value of x-axis for Fig.(6), page 175\n",
+      "y=1.2;                               # Value of y-axis from Fig.(6)\n",
+      "Gsstar=y*rhog*uo;                    #Computation of rate of entrainment\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nRate of entrainment=%.2fkg/m**2s'%Gsstar\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Rate of entrainment=4.03kg/m**2s\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 180\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "x=0.2;          #Fraction of fines in the bed\n",
+      "Gsstar=4.033320 #Rate of entrainment in kg/m**2s(from Exa.1)\n",
+      "\n",
+      "#CALCULATION\n",
+      "Gsstar1=x*Gsstar;#Rate of entrainment by Eqn.(3)\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nRate of entrainment=%.3fkg/m**2s'%Gsstar1\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Rate of entrainment=0.807kg/m**2s\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 181\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "rhog=5.51;                    #Density of gas in kg/m**3\n",
+      "rhos=1200;                    #Density of solid in kg/m**3\n",
+      "uo=0.61;                      #Superficial gas velocity in m/s\n",
+      "g=9.80;                       #Acceleration due to gravity in m/s**2\n",
+      "dp=[10,30,50,70,90,110,130];  #Diameter of particle in micrometer\n",
+      "p=[0.,0.0110,0.0179,0.0130,0.0058,0.0020,0.];\n",
+      "pi=3.142857;\n",
+      "dt=6;\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(dp);\n",
+      "i=0;\n",
+      "x = [0,0,0,0,0,0,0]\n",
+      "while i<n:\n",
+      "    x[i]=(uo**2)/(g*(dp[i]*10**-6)*rhos**2);#Computation of value of x-axis for Fig.(6), page 175)\n",
+      "    i=i+1;\n",
+      "\n",
+      "y=[40,12,6,3.2,2.,1.3,1];#Value of y-axis corresponding to each value of x-axis\n",
+      "y1 = []\n",
+      "for i in range(n):\n",
+      "    y1.append(y[i]*p[i]);\n",
+      "i=0;\n",
+      "k=0;\n",
+      "\n",
+      "while i<n-2:\n",
+      "    y1[i]=(y[i]*p[i]);\n",
+      "    k=k+((0.5)*(dp[i+1]-dp[i])*(y1[i+1]+y1[i]));#Integration using Trapezoidal rule\n",
+      "    i=i+1;\n",
+      "rhosbar=k*rhog;#Computation of solid loading\n",
+      "te=(pi/4)*(dt**2)*rhosbar*uo;#Computation of total entrainment\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nSolid loading =%.1fkg/m**3'%rhosbar\n",
+      "print '\\nTotal Entrainment =%.0fkg/s'%te\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Solid loading =32.4kg/m**3\n",
+        "\n",
+        "Total Entrainment =559kg/s\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 4, Page 181\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "dp=[40,60,80,100,120]; #Diameter of particle in micrometer\n",
+      "uo=0.381;              #Superficial gas velocity in m/s\n",
+      "\n",
+      "#CALCULATION\n",
+      "Gs=0.9;#Rate of entrainment in kg/m**2 s from Fig.3(a)\n",
+      "pb = [0.45,1.00,1.25,1.00,0.60];#Size distribution for bed particles from Fig.3(b)\n",
+      "pe=[1.20,2.00,1.25,0.45,0.10];  #Size distribution for entrained particles from Fig.3(b)\n",
+      "n=len(dp);\n",
+      "for i in range(n):\n",
+      "    pb[i] = pb[i]/100.\n",
+      "    pe[i] = pe[i]/100.\n",
+      "i=0;\n",
+      "ki = []\n",
+      "while i<n:\n",
+      "    ki.append((Gs*pe[i])/pb[i]);#Calculation of ki* using Eqn.(13)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\ndpi(micrometer)',\n",
+      "print '\\t100pb(dpi)(micrometer**-1)',\n",
+      "print '\\t100pe(dpi)(micrometer**-1)',\n",
+      "print '\\tki*(kg/m**2 s)'\n",
+      "\n",
+      "j=0;\n",
+      "while j<n:\n",
+      "    print '%f'%dp[j],\n",
+      "    print '\\t%f'%(100*pb[j]),\n",
+      "    print '\\t\\t\\t%f'%(100*pe[j]),\n",
+      "    print '\\t\\t\\t%f'%ki[j]\n",
+      "    j=j+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "dpi(micrometer) \t100pb(dpi)(micrometer**-1) \t100pe(dpi)(micrometer**-1) \tki*(kg/m**2 s)\n",
+        "40.000000 \t0.450000 \t\t\t1.200000 \t\t\t2.400000\n",
+        "60.000000 \t1.000000 \t\t\t2.000000 \t\t\t1.800000\n",
+        "80.000000 \t1.250000 \t\t\t1.250000 \t\t\t0.900000\n",
+        "100.000000 \t1.000000 \t\t\t0.450000 \t\t\t0.405000\n",
+        "120.000000 \t0.600000 \t\t\t0.100000 \t\t\t0.150000\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 5, Page 181\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "rhog=1.217;                                   #Density of gas in kg/m**3\n",
+      "myu=1.8E-5;                                   #Viscosity of gas in kg/m s\n",
+      "umf=0.11;                                     #Velocity at minimum fluidization condition in m/s\n",
+      "rhos=2000.0;                                  #Density of solid in kg/m**3\n",
+      "uo=1.0;                                       #Superficial gas velocity in m/s\n",
+      "g=9.80;                                       #Acceleration due to gravity in m/s**2\n",
+      "dp=[30,40,50,60,80,100,120];                  #Diameter of particle in micrometer\n",
+      "uti=[0.066,0.115,0.175,0.240,0.385,0.555,1.0];#Terminal velocity of particles in m/s\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(dp);\n",
+      "i=0;\n",
+      "Ret = []\n",
+      "kistar1 = []\n",
+      "kistar2 = []\n",
+      "kistar3 = []\n",
+      "kistar4 = []\n",
+      "kistar5 = []\n",
+      "kistar6 = []\n",
+      "x1 = []\n",
+      "x2 = []\n",
+      "\n",
+      "while i<n:\n",
+      "    #Using Yagi & Aochi's correlation\n",
+      "    Ret.append((rhog*(uti[i])*dp[i]*10**-6)/myu)\n",
+      "    a =((myu*((uo-uti[i])**2))/(g*(dp[i]*10**-6)**2))*(0.0015*(Ret[i]**0.5)+(0.01*(Ret[i]**1.2)));\n",
+      "    kistar1.append(a)\n",
+      "    #Using Wen & Hasinger's correlation\n",
+      "    a=(((1.52E-5)*((uo-uti[i])**2)*rhog)/(g*dp[i]*10**-6)**0.5)*(Ret[i]**0.725)*((rhos-rhog)/rhog)**1.15;\n",
+      "    kistar2.append(a)\n",
+      "    #Using Merrick & Highley's correlation\n",
+      "    a=uo*rhog*(0.0001+130*math.exp(-10.4*((uti[i]/uo)**0.5)*((umf/(uo-umf))**0.25)));\n",
+      "    kistar3.append(a)\n",
+      "    #Using Geldart's correlation\n",
+      "    a=23.7*uo*rhog*math.exp(-5.4*(uti[i]/uo));\n",
+      "    kistar4.append(a)\n",
+      "    #Using Zenz & Weil's procedure\n",
+      "    a=(uo**2)/(g*(dp[i]*10.0**-6)*rhos**2);#Computation of value of x-axis for Fig.(6), page 175)\n",
+      "    x1.append(a)\n",
+      "    y1=[12.2,8.6,6.4,4.9,2.75,1.8,1.2];#Value of y-axis corresponding to each value of x-axis\n",
+      "    kistar5.append(y1[i]*rhog*uo)\n",
+      "    #Using Gugnoni & Zenz's procedure\n",
+      "    a=(uo-uti[i])/((g*dp[i]*10**-6)**0.5);#Computation of value of x-axis for Fig.(6), page 175)\n",
+      "    x2.append(a)\n",
+      "    y=[5.8,5.4,3.2,2.8,1.3,0.6,0];#Value of y-axis corresponding to each value of x-axis\n",
+      "    kistar6.append(y[i]*rhog*uo)\n",
+      "    i=i+1;\n",
+      "\n",
+      "i=0;\n",
+      "print 'dp(micrometer)',\n",
+      "print '\\tYagi & Aochi',\n",
+      "print '\\tWen & Hashinger',\n",
+      "print '\\t\\tMerrick & Highley',\n",
+      "print '\\tGeldart et al.',\n",
+      "print '\\t\\tZenz & Well',\n",
+      "print '\\t\\tGugnoni & Zenz'\n",
+      "while i<n:\n",
+      "    print '\\n%f'%dp[i],\n",
+      "    print '\\t%f'%kistar1[i],\n",
+      "    print '\\t%f'%kistar2[i],\n",
+      "    print '\\t\\t%f'%kistar3[i],\n",
+      "    print '\\t\\t%f'%kistar4[i],\n",
+      "    print '\\t\\t%f'%kistar5[i],\n",
+      "    print '\\t\\t%f'%kistar6[i],\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Note: There is huge deviation of the calculated answer and the answer given in the textbook for the correlation of Merrick & Highley.  There is a contradiction in the correlation used in the problem and the one given in page 179. \n",
+      "#We tried to retrieve the original paper i.e. D.Merrick and J.Highley, AICHE J., 6, 220(1960). But the effort was not fruitful.\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "dp(micrometer) \tYagi & Aochi \tWen & Hashinger \t\tMerrick & Highley \tGeldart et al. \t\tZenz & Well \t\tGugnoni & Zenz\n",
+        "\n",
+        "30.000000 \t2.571188 \t1.092184 \t\t32.451340 \t\t20.195582 \t\t14.847400 \t\t7.058600 \n",
+        "40.000000 \t2.965958 \t1.564720 \t\t19.546385 \t\t15.500369 \t\t10.466200 \t\t6.571800 \n",
+        "50.000000 \t3.240381 \t1.938471 \t\t11.993076 \t\t11.210646 \t\t7.788800 \t\t3.894400 \n",
+        "60.000000 \t3.289995 \t2.154988 \t\t7.713841 \t\t7.892113 \t\t5.963300 \t\t3.407600 \n",
+        "80.000000 \t2.852535 \t2.120728 \t\t3.447977 \t\t3.606955 \t\t3.346750 \t\t1.582100 \n",
+        "100.000000 \t1.883718 \t1.521994 \t\t1.600171 \t\t1.440318 \t\t2.190600 \t\t0.730200 \n",
+        "120.000000 \t0.000000 \t0.000000 \t\t0.332158 \t\t0.130271 \t\t1.460400 \t\t0.000000\n"
+       ]
+      }
+     ],
+     "prompt_number": 5
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 6, Page 190\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "dpbar=60.0;   #Average size of particles in micrometer\n",
+      "rhog=1.3;     #Density of gas in kg/m**3\n",
+      "rhos=1500.0;  #Density of solid in kg/m**3\n",
+      "umf=0.003;    #Velocity at minimum fluidization condition in m/s\n",
+      "uo=0.503;     #Superficial gas velocity in m/s\n",
+      "g=9.80;       #Acceleration due to gravity in m/s**2\n",
+      "Hf=2.0;       #Height at which the cyclone inlet is to be located in m\n",
+      "\n",
+      "#CALCULATION\n",
+      "y=(uo**2)/(g*(dpbar*10**-3)*rhos**2);#Calculation of value of y-axis for Fig.(6), page 175\n",
+      "x=1;#Value of x-axis from Fig.(6), page 175\n",
+      "Gsstar=x*rhog*uo;#Computation of rate of entrainment\n",
+      "Gsuo=5.0;#Ejection rate pf particles in kg/m**2 s from Fig.(11), page 188\n",
+      "a=0.72/uo;#From Fig.(12), page 189\n",
+      "Gs=Gsstar+(Gsuo-Gsstar)*math.exp(-a*Hf);\n",
+      "p=((Gs-Gsstar)/Gsstar)*100.0;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\nRate of entrainment from short bed=%.3fkg/m**2s'%Gs\n",
+      "print '\\nThis entrainment is %f percent higher than it would be if the gas exit were at the TDH'%p\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "\n",
+        "Rate of entrainment from short bed=0.902kg/m**2s\n",
+        "\n",
+        "This entrainment is 37.955972 percent higher than it would be if the gas exit were at the TDH\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch8.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch8.ipynb
new file mode 100755
index 00000000..9fed0363
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch8.ipynb
@@ -0,0 +1,218 @@
+{
+ "metadata": {
+  "name": ""
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 8 : High Velocity Fludization"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 206\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "import math \n",
+      "from numpy import zeros\n",
+      "from scipy.optimize import fsolve \n",
+      "\n",
+      "\n",
+      "#INPUT\n",
+      "Lmf=2.4;            #Length of bed at minimum fluidized condition in m\n",
+      "uo=[2.,4.,6.];         #Superficial gas velocity in m/s\n",
+      "GsII=100.;          #Solid circulation rate in kg/m**2 s for Mode II\n",
+      "uoIII=4.;            #Superficial gas velocity in m/s for Mode III\n",
+      "GsIII=[42.,50.,100.,200.,400.];          #Solid circulation rate in kg/m**2 s for Mode III\n",
+      "GsIV=[70.,100.,120.];                  #Solid circulation rate in kg/m**2 s for Mode IV\n",
+      "dt=0.4;                             #Column diamter in m\n",
+      "Ht=10.;                              #Height of column in m\n",
+      "rhos=1000.;                         #Density of solid in kg/m**3\n",
+      "dpbar=55.;                          #Particle diameter in micrometer\n",
+      "ephsilonmf=0.5;                     #Void fraction at minimum fluidization condition\n",
+      "\n",
+      "#CALCULATION\n",
+      "#Mode I\n",
+      "ephsilonstar=0.01;                  #Saturation carrying capacity of gas\n",
+      "ephsilonsd=[0.2,0.16,0.14];         #Solid holdup in lower dense region from Fig.8(b) for various uo\n",
+      "n=len(uo);\n",
+      "i=0;\n",
+      "Hfguess=2.;          #Guess value of height\n",
+      "a = zeros(n)\n",
+      "Hf = zeros(n)\n",
+      "Hd = zeros(n)\n",
+      "ephsilonse = zeros(n)\n",
+      "GsI = zeros(n)\n",
+      "#    endfunction\n",
+      " \n",
+      "while i<n:\n",
+      "    a[i]= 3./uo[i];         #Decay consmath.tant\n",
+      "    def solver_func(Hf):            #Function defined for solving the system\n",
+      "        return Lmf*(1-ephsilonmf)-((ephsilonsd[i]-(ephsilonstar+(ephsilonsd[i]-ephsilonstar)*math.exp(-a[i]*Hf)))/a[i])-Ht*ephsilonsd[i]+Hf*(ephsilonsd[i]-ephsilonstar);\n",
+      "        \n",
+      "    Hf[i] = fsolve(solver_func,1E-6)\n",
+      "    Hd[i]=Ht-Hf[i];#Height of lower densce region\n",
+      "    ephsilonse[i]=ephsilonstar+(ephsilonsd[i]-ephsilonstar)*math.exp(-a[i]*Hf[i]);#Solid holdup at exit\n",
+      "    GsI[i]=rhos*uo[i]*ephsilonse[i];#Solid circulation rate from Eqn.(4)\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Mode II\n",
+      "i=0;\n",
+      "Hfguess2=2;#Guess value of height\n",
+      "ephsilonseII = zeros(n)\n",
+      "HdII = zeros(n)\n",
+      "LmfII = zeros(n)\n",
+      "HfII = zeros(n)\n",
+      "while i<n:\n",
+      "    ephsilonseII[i]=GsII/(rhos*uo[i]);#Solid holdup at exit\n",
+      "    def solver_func1(Hf):           #Function defined for solving the system\n",
+      "        return ephsilonseII[i]-ephsilonstar-(ephsilonsd[i]-ephsilonstar)*math.exp(-a[i]*Hf);#From Eqn.(7)\n",
+      "    HfII[i] = fsolve(solver_func1,1E-6)\n",
+      "    HdII[i]=Ht-HfII[i];#Height of lower dense region\n",
+      "    #Length of bed minimum fluidization condtion\n",
+      "    LmfII[i]=(1-ephsilonmf)**-1*((ephsilonsd[i]-ephsilonseII[i])/a[i])+Ht*ephsilonsd[i]-HfII[i]*(ephsilonsd[i]-ephsilonstar);\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Mode III\n",
+      "aIII = 3./uoIII;            #Decay consmath.tant\n",
+      "ephsilonsdIII=0.16;         #Solid holdup at lower dense region\n",
+      "i=0;\n",
+      "m=len(GsIII);\n",
+      "Hfguess3=2;#Guess value of height \n",
+      "ephsilonseIII = zeros(m)\n",
+      "HdIII = zeros(m)\n",
+      "ephsilonseIII = zeros(m)\n",
+      "LmfIII = zeros(m)\n",
+      "HfIII = zeros(m)\n",
+      "while i<m:\n",
+      "    ephsilonseIII[i]=GsIII[i]/(rhos*uoIII);#Solid holdup at exit\n",
+      "    def solver_func2(Hf):       #Function defined for solving the system\n",
+      "        return ephsilonseIII[i]-ephsilonstar-(ephsilonsdIII-ephsilonstar)*math.exp(-aIII*Hf);#From Eqn.(7)\n",
+      "\n",
+      "    HfIII[i] = fsolve(solver_func2,1E-6)\n",
+      "    HdIII[i]=Ht-HfIII[i];       #Height of lower dense region\n",
+      "    #Length of bed at minimum fluidization condition\n",
+      "    LmfIII[i]=(1-ephsilonmf)**-1*(((ephsilonsdIII-ephsilonseIII[i])/aIII)+Ht*ephsilonsdIII-HfIII[i]*(ephsilonsdIII-ephsilonstar));\n",
+      "    i=i+1;\n",
+      "\n",
+      "#Mode IV\n",
+      "i=0;\n",
+      "Hfguess4=2;#Guess value of height\n",
+      "aIV = zeros(n)\n",
+      "ephsilonseIV = zeros(n)\n",
+      "HdIV = zeros(n)\n",
+      "HfIV = zeros(n)\n",
+      "LmfIV = zeros(n)\n",
+      "while i<n:\n",
+      "    aIV[i]=3./uo[i];            #Decay consmath.tant\n",
+      "    ephsilonseIV[i]=GsIV[i]/(rhos*uo[i]);       #Solid holdup at exit\n",
+      "    def solver_func3(Hf):       #Function defined for solving the system\n",
+      "        return ephsilonseIV[i]-ephsilonstar-(ephsilonsd[i]-ephsilonstar)*math.exp(-aIV[i]*Hf);      #From Eqn.(7)\n",
+      "\n",
+      "    HfIV[i] = fsolve(solver_func3,1E-6)\n",
+      "    HdIV[i]=Ht-HfIV[i];#Height of lower dense region\n",
+      "    #Length of bed at minimum fluidization condition\n",
+      "    LmfIV[i]=(1-ephsilonmf)**-1*(((ephsilonsd[i]-ephsilonseIV[i])/aIV[i])+Ht*ephsilonsd[i]-HfIV[i]*(ephsilonsd[i]-ephsilonstar));\n",
+      "    i=i+1;\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'Mode I';\n",
+      "print '\\tuom/s\\t\\tephsilonse-\\tHfm\\t\\tHdm\\t\\tGskg/m**2 s';\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '\\t%f\\t%f\\t%f\\t%f\\t%f'%(uo[i],ephsilonse[i],Hf[i],Hd[i],GsI[i]);\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Mode II';\n",
+      "print '\\tuom/s\\t\\tephsilonse-\\tHfm\\t\\tHdm\\t\\tLmfm';\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '\\t%f\\t%f\\t%f\\t%f\\t%f'%(uo[i],ephsilonseII[i],HfII[i],HdII[i],LmfII[i]);\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Mode III';\n",
+      "print '\\tGskg/m** s\\tephsilonse-\\tHfm\\t\\tHdm\\t\\tLmfm';\n",
+      "i=0;\n",
+      "while i<m:\n",
+      "    print '\\t%f\\t%f\\t%f\\t%f\\t%f'%(GsIII[i],ephsilonseIII[i],HfIII[i],HdIII[i],LmfIII[i]);\n",
+      "    i=i+1;\n",
+      "\n",
+      "print 'Mode IV';\n",
+      "print '\\tuom/s\\t\\tGskg/m**2 s\\tephsilonse-\\tHfm\\t\\tLmfm';\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '\\t%f\\t%f\\t%f\\t%f\\t%f'%(uo[i],GsIV[i],ephsilonseIV[i],HfIV[i],LmfIV[i]);\n",
+      "    i=i+1;\n",
+      "\n",
+      "#====================================END OF PROGRAM ======================================================"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Mode I\n",
+        "\tuom/s\t\tephsilonse-\tHfm\t\tHdm\t\tGskg/m**2 s\n",
+        "\t2.000000\t0.192856\t0.025551\t9.974449\t385.711493\n",
+        "\t4.000000\t0.017870\t3.930041\t6.069959\t71.481458\n",
+        "\t6.000000\t0.037349\t3.117707\t6.882293\t224.094133\n",
+        "Mode II\n",
+        "\tuom/s\t\tephsilonse-\tHfm\t\tHdm\t\tLmfm\n",
+        "\t2.000000\t0.050000\t1.038763\t8.961237\t2.002635\n",
+        "\t4.000000\t0.025000\t3.070113\t6.929887\t1.499483\n",
+        "\t6.000000\t0.016667\t5.940829\t4.059171\t1.121026\n",
+        "Mode III\n",
+        "\tGskg/m** s\tephsilonse-\tHfm\t\tHdm\t\tLmfm\n",
+        "\t42.000000\t0.010500\t7.605043\t2.394957\t1.317154\n",
+        "\t50.000000\t0.012500\t5.459126\t4.540874\t1.955596\n",
+        "\t100.000000\t0.025000\t3.070113\t6.929887\t2.638966\n",
+        "\t200.000000\t0.050000\t1.762341\t8.237659\t2.964631\n",
+        "\t400.000000\t0.100000\t0.681101\t9.318899\t3.155670\n",
+        "Mode IV\n",
+        "\tuom/s\t\tGskg/m**2 s\tephsilonse-\tHfm\t\tLmfm\n",
+        "\t2.000000\t70.000000\t0.035000\t1.352099\t3.706202\n",
+        "\t4.000000\t100.000000\t0.025000\t3.070113\t2.638966\n",
+        "\t6.000000\t120.000000\t0.020000\t5.129899\t1.946226\n"
+       ]
+      },
+      {
+       "output_type": "stream",
+       "stream": "stderr",
+       "text": [
+        "/usr/lib/python2.7/dist-packages/scipy/optimize/minpack.py:227: RuntimeWarning: The iteration is not making good progress, as measured by the \n",
+        "  improvement from the last ten iterations.\n",
+        "  warnings.warn(msg, RuntimeWarning)\n"
+       ]
+      }
+     ],
+     "prompt_number": 1
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch9.ipynb b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch9.ipynb
new file mode 100755
index 00000000..5087d780
--- /dev/null
+++ b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/ch9.ipynb
@@ -0,0 +1,265 @@
+{
+ "metadata": {
+  "name": "",
+  "signature": "sha256:52ff353152f32e41c2e832a90f993fbd3f11b7f2a5fbb5e4f20eb7599a61f880"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+  {
+   "cells": [
+    {
+     "cell_type": "heading",
+     "level": 1,
+     "metadata": {},
+     "source": [
+      "Chapter 9 :  Solid Movement Mixing  Segregation and Staging"
+     ]
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 1, Page 218\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "umf=0.015;                 #Velocity at minimum fluidization condition in m/s\n",
+      "ephsilonmf=0.5;            #Void fraction at minimum fluidization condition\n",
+      "uo=0.1;                    #Superficial gas velocity in m/s\n",
+      "delta=0.2;                 #Bed fraction in bubbles\n",
+      "db=0.06;                   #Equilibrium bubble size in m\n",
+      "dt=[0.1,0.3,0.6,1.5];      #Various vessel sizes in m\n",
+      "ub=[0.4,0.75,0.85,1.1];    #Bubble velocity in m/s\n",
+      "Dsv=[0.03,0.11,0.14,0.23]; #Reported values of vertical dispersion coefficient\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(ub);\n",
+      "i=0;\n",
+      "fw1=2;#Wake fraction from Hamilton et al.\n",
+      "fw2=0.32;#Wake fraction from Fig.(5.8)\n",
+      "fw=(fw1+fw2)*0.5;#Average value of wake fraction\n",
+      "Dsv1 = []\n",
+      "Dsv2 = []\n",
+      "while i<n:\n",
+      "    Dsv1.append(12*((uo*100)**0.5)*((dt[i]*100)**0.9));#Vertical distribution coefficient from Eqn.(3)\n",
+      "    Dsv2.append((fw**2*ephsilonmf*delta*db*ub[i]**2)/(3*umf));#Vertical distribution coefficient from Eqn.(12)\n",
+      "    i=i+1;\n",
+      "\n",
+      "print Dsv1\n",
+      "\n",
+      "#OUTPUT\n",
+      "print '\\t\\tVertical dispersion coefficient(m**2/s)'\n",
+      "print 'Vessel Size(m)',\n",
+      "print '\\tFrom Experiment',\n",
+      "print '\\tFrom Eqn.(3)',\n",
+      "print '\\tFrom Eqn.(12)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%.2f'%dt[i],\n",
+      "    print '\\t%.3f'%Dsv[i],\n",
+      "    print '\\t%.2f'%(Dsv1[i]/10**4),\n",
+      "    print '\\t%.2f'%Dsv2[i]\n",
+      "    i=i+1;   \n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "[301.42637178114967, 810.1965234492834, 1511.8801720132121, 3448.7632274996104]\n",
+        "\t\tVertical dispersion coefficient(m**2/s)\n",
+        "Vessel Size(m) \tFrom Experiment \tFrom Eqn.(3) \tFrom Eqn.(12)\n",
+        "0.10 \t0.030 \t0.03 \t0.03\n",
+        "0.30 \t0.110 \t0.08 \t0.10\n",
+        "0.60 \t0.140 \t0.15 \t0.13\n",
+        "1.50 \t0.230 \t0.34 \t0.22\n"
+       ]
+      }
+     ],
+     "prompt_number": 2
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 2, Page 222\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "Lmf=0.83;                          #Length of bed at minimum fluidization condition in m\n",
+      "dp=450.0;                          #Average particle size in micrometer\n",
+      "ephsilonmf=0.42;                   #Void fraction at minimum fluidization condition\n",
+      "umf=0.17;                          #Velocity at minimum fluidization condition in m/s\n",
+      "uo=[0.37,0.47,0.57,0.67];          #Superficial gas velocity in m/s\n",
+      "Dsh=[0.0012,0.0018,0.0021,0.0025]; #Horizontal Drift Coefficient from Experiment in m**2/s\n",
+      "db=[0.10,0.14];                    #Equilibrium bubble size in m\n",
+      "g=9.81;                            #Acceleration due to gravity in m/s**2\n",
+      "\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(uo);\n",
+      "m=len(db);\n",
+      "k=0;\n",
+      "alpha=0.77;#Since we are not dealing with Geldart A or AB solids\n",
+      "uf=umf/ephsilonmf;\n",
+      "ubr = []\n",
+      "ub = []\n",
+      "delta = []\n",
+      "Dshc = []\n",
+      "for j in range(m):\n",
+      "    for i in range(n):\n",
+      "        ubr.append(0.711*(db[j]*g)**0.5);#Rise velocity of a single bubble in m/s\n",
+      "        ub.append(uo[i]-umf+ubr[k]);#Rise velocity of bubbles in a bubbling bed\n",
+      "        delta.append((uo[i]-umf)/(ub[k]+umf));#Bed fraction in bubbles\n",
+      "        if ubr[i]>uf:\n",
+      "            Dshc.append((3/16.0)*(delta[k]/(1-delta[k]))*((alpha**2*db[j]*ubr[k]*((((ubr[k]+2*uf)/(ubr[k]-uf))**(1.0/3))-1))));\n",
+      "                #Horizontal Distribution coeff. from Eqn.(14)\n",
+      "        else:\n",
+      "            Dsh.append((3.0/16)*(delta/(1-delta))*(alpha**2*umf*db/ephsilonmf))\n",
+      "                #Horizontal Distribution coeff. from Eqn.(15)\n",
+      "        Dshc.append((3/16.0)*(delta[k]/(1-delta[k]))*((alpha**2*db[j]*ubr[k]*((((ubr[k]+2*uf)/(ubr[k]-uf))**(1/3.0))-1))));#Horizontal Distribution coeff. from Eqn.(14)\n",
+      "        k=k+1;\n",
+      "i=0;\n",
+      "j=0;\n",
+      "k=0;\n",
+      "while k<m*n:\n",
+      "    print 'Snce we do not have ub=%fm/s>>uf=%fm/s we use Eqn.(14).'%(ub[k],uf)\n",
+      "    print 'Gas Velocity(m/s)'\n",
+      "    print '\\tHorizontal Drift Coefficient Calculated(m**2/s)'\n",
+      "    print '\\tHorizontal Drift Coefficient from Experiment(m**2/s)'\n",
+      "    while j<m:\n",
+      "        print 'db=%fm'%db[j]\n",
+      "        while i<n:\n",
+      "            print '%f'%uo[i],\n",
+      "            print '\\t\\t%f'%Dshc[k],\n",
+      "            print '\\t\\t\\t\\t\\t%f'%Dsh[i]\n",
+      "            i=i+1;   \n",
+      "            k=k+1;\n",
+      "        i=0;\n",
+      "        j=j+1;\n",
+      "\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "Snce we do not have ub=0.904213m/s>>uf=0.404762m/s we use Eqn.(14).\n",
+        "Gas Velocity(m/s)\n",
+        "\tHorizontal Drift Coefficient Calculated(m**2/s)\n",
+        "\tHorizontal Drift Coefficient from Experiment(m**2/s)\n",
+        "db=0.100000m\n",
+        "0.370000 \t\t0.001283 \t\t\t\t\t0.001200\n",
+        "0.470000 \t\t0.001283 \t\t\t\t\t0.001800\n",
+        "0.570000 \t\t0.001924 \t\t\t\t\t0.002100\n",
+        "0.670000 \t\t0.001924 \t\t\t\t\t0.002500\n",
+        "db=0.140000m\n",
+        "0.370000 \t\t0.002566 \t\t\t\t\t0.001200\n",
+        "0.470000 \t\t0.002566 \t\t\t\t\t0.001800\n",
+        "0.570000 \t\t0.003207 \t\t\t\t\t0.002100\n",
+        "0.670000 \t\t0.003207 \t\t\t\t\t0.002500\n"
+       ]
+      }
+     ],
+     "prompt_number": 3
+    },
+    {
+     "cell_type": "heading",
+     "level": 3,
+     "metadata": {},
+     "source": [
+      "Example 3, Page 232\n"
+     ]
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [
+      "\n",
+      "\n",
+      "import math\n",
+      "\n",
+      "#Variable declaration\n",
+      "Gsup=1.5;               #Solid interchange rate in kg/m**2plate s\n",
+      "dor=19.1;               #Orifice diameter in mm\n",
+      "dp=210;                 #Particle size in micrometer\n",
+      "uo=0.4;                 #Superficial gas velocity in m/s\n",
+      "fopen=[0.12,0.17,0.26]; #Open area fraction \n",
+      "pi=3.14;\n",
+      "\n",
+      "#CALCULATION\n",
+      "n=len(fopen);\n",
+      "uor = []\n",
+      "ls1 = []\n",
+      "i=0\n",
+      "while i<n:\n",
+      "    uor.append(uo/fopen[i]);  #Gas velocity through the orifice\n",
+      "    ls1.append(Gsup/fopen[i]);#Flux of solids through the holes\n",
+      "    i=i+1;\n",
+      "\n",
+      "ls2=[12,20,25];                #Flux of solids through holes from Fig.13(c) for different uor values\n",
+      "fopen1=0.12;                   #Open area fraction which gives reasonable fit\n",
+      "lor=math.sqrt(((math.pi/4)*dor**2)/fopen1);#Orifice spacing\n",
+      "\n",
+      "#OUTPUT\n",
+      "print 'fopen',\n",
+      "print '\\t\\tuor(m/s)',\n",
+      "print '\\tls from Eqn.(18)',\n",
+      "print '\\tls from Fig.13(c)'\n",
+      "i=0;\n",
+      "while i<n:\n",
+      "    print '%f'%fopen[i],\n",
+      "    print '\\t%f'%uor[i],\n",
+      "    print '\\t%f'%ls1[i],\n",
+      "    print '\\t\\t%f'%ls2[i]\n",
+      "    i=i+1;   \n",
+      "\n",
+      "print '\\nFor square pitch, the orifice spacing should be %fmm'%lor\n"
+     ],
+     "language": "python",
+     "metadata": {},
+     "outputs": [
+      {
+       "output_type": "stream",
+       "stream": "stdout",
+       "text": [
+        "fopen \t\tuor(m/s) \tls from Eqn.(18) \tls from Fig.13(c)\n",
+        "0.120000 \t3.333333 \t12.500000 \t\t12.000000\n",
+        "0.170000 \t2.352941 \t8.823529 \t\t20.000000\n",
+        "0.260000 \t1.538462 \t5.769231 \t\t25.000000\n",
+        "\n",
+        "For square pitch, the orifice spacing should be 48.863850mm\n"
+       ]
+      }
+     ],
+     "prompt_number": 4
+    },
+    {
+     "cell_type": "code",
+     "collapsed": false,
+     "input": [],
+     "language": "python",
+     "metadata": {},
+     "outputs": []
+    }
+   ],
+   "metadata": {}
+  }
+ ]
+}
+\ No newline at end of file
diff --git a/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/screenshots/plotkbckbedb.png b/Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel/screenshots/plotkbckbedb.png
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author	Thomas Stephen Lee	2015-09-04 22:04:10 +0530
committer	Thomas Stephen Lee	2015-09-04 22:04:10 +0530
commit	41f1f72e9502f5c3de6ca16b303803dfcf1df594 (patch)
tree	f4bf726a3e3ce5d7d9ee3781cbacfe3116115a2c /Fluidization_Engineering_by_K_Daizo_And_O_Levenspiel
parent	9c9779ba21b9bedde88e1e8216f9e3b4f8650b0e (diff)
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