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  {
   "cells": [
    {
     "cell_type": "heading",
     "level": 1,
     "metadata": {},
     "source": [
      "Chapter 3 :  Volumetric Properties Of Pure Fluids"
     ]
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.1 page no : 46"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "# Variables\n",
      "P1 = 1.;\t\t\t#Pressure = 1Bar\n",
      "T1 = 20.;\t\t\t#Temp = 293.15K(20`C)\n",
      "Beta = 1.487*10**(-3);\t\t\t#vol expansivity(K**-1)\n",
      "k = 62.*10**(-6);\t\t\t#isothermal compressibility(bar**-1)\n",
      "V1 = 1.287*10**(-3);\t\t\t#Volume(m**3 kg**-1)\n",
      "\n",
      "# Calculations and Results\n",
      "#(a)\n",
      "#Find (dP/dT)v??\n",
      "#Using eq.(3.4),V consmath.tant hence dV = 0\n",
      "ans_a = (Beta/k);\n",
      "print '(a)The value of (dp/dT)v is ',ans_a,'K**-1'\n",
      "\n",
      "#(b)\n",
      "#Find Pressure when acetone heated at const. Vol from T1(1bar) to T2.\n",
      "T2_b = 30.;\t\t\t#Temp2 = 303.15K(30`C)\n",
      "del_P = ans_a*(T2_b-T1);\n",
      "ans_b = P1+del_P;\n",
      "print '(b)The pressure is ',ans_b,'bar'\n",
      "\n",
      "#(c)\n",
      "#Find vol. change when acetone changed from T1(P1) to T2(P2)\n",
      "T2_c = 0;\t\t\t#Temp2 = 273.15K(0`C)\n",
      "P2 = 10.;\t\t\t#pressure = 10bar\n",
      "#solve using Eq. (3.5)\n",
      "ln_value = (Beta*(T2_c-T1))-(k*(P2-P1));\t\t\t#ln(V2/V1)\n",
      "ratio = math.exp(ln_value);\t\t\t#taking antimath.log,V2/V1\n",
      "V2 = ratio*V1;\n",
      "del_V = round(V2-V1,6)\n",
      "print '(c)The change in Volume is ',del_V*1000,'(X 10**-3) m**3 kg**-1'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a)The value of (dp/dT)v is  23.9838709677 K**-1\n",
        "(b)The pressure is  240.838709677 bar\n",
        "(c)The change in Volume is  -0.038 (X 10**-3) m**3 kg**-1\n"
       ]
      }
     ],
     "prompt_number": 1
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.2 page no : 47"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "%matplotlib inline\n",
      "\n",
      "import math \n",
      "from numpy import linspace\n",
      "from matplotlib.pyplot import plot,suptitle,xlabel,ylabel\n",
      "\n",
      "# Variables\n",
      "#Figure\n",
      "P = [1, 5];\n",
      "V = [25 ,25];\n",
      "\n",
      "# Calculations and Results\n",
      "plot(V,P)\n",
      "V = linspace(5,25,41)\n",
      "P = 25*V**-1;\n",
      "plot(V,P)\n",
      "P = P**1.4;\n",
      "plot(V,P)\n",
      "P = [5 ,9.52];\n",
      "V = [5 ,5];\n",
      "plot(V,P) #,rect = [0,0,30,10])\n",
      "suptitle(\"Diagram for Ex.3.2\")\n",
      "xlabel(\"V x 10**3(m**3)\")\n",
      "ylabel(\"P(bar)\")\n",
      "P = [5, 5];\n",
      "V = [5 ,25];\n",
      "plot(V,P)\n",
      "\n",
      "#Initial Stage\n",
      "P1 = 1.;\t\t\t#Pressure = 1bar\n",
      "T1 = 298.15;\t\t\t#Temp1 = 298.15K(25`C)\n",
      "\n",
      "#Final Stage\n",
      "P2 = 5.;\t\t\t#Pressure = 1bar\n",
      "#Temp same as Temp1(Isothermal)\n",
      "\n",
      "R = 8.314;\t\t\t#J/Mol/K\n",
      "Cv = (5./2)*R;\t\t\t#J/Mol/K\n",
      "Cp = (7./2)*R;\t\t\t#J/Mol/K\n",
      "\n",
      "#(a)\n",
      "#Const Vol follwd by const Pressure\n",
      "T2 = T1*(P2/P1);\n",
      "#By Eq 2.23\n",
      "del_T = T2-T1;\n",
      "Q1 = Cv*(T2-T1);\t\t\t#Heat at const Vol\n",
      "Q2 = Cp*(T1-T2);\t\t\t#Heat at const pressure\n",
      "\n",
      "Q_a = round(Q1+Q2);\n",
      "W_a = -Q_a;\t\t\t#W = del_U-Q,here del_U = 0\n",
      "print ('       (a) Heating at consmath.tant volume Followed by cooling at consmath.tant Pressure')\n",
      "print 'work done by heating at const vol followed by const Pressure ',W_a,'J'\n",
      "print 'Heat Transferred Q ',Q_a,'J'\n",
      "print ('change in Internal Energy and enthalpy  =  0')\n",
      "\n",
      "#(b)\n",
      "#Isothermal Compression\n",
      "#By Eq. (3.26)\n",
      "Q_b = round(R*T1*math.log(P1/P2));\n",
      "W_b = -Q_b;\n",
      "print ('       (b) Isothermal compression')\n",
      "print 'work done by Isothermal compression ',W_b,'J'\n",
      "print 'Heat Transferred Q',Q_b,'J'\n",
      "print ('change in Internal Energy and enthalpy  =  0')\n",
      "\n",
      "#(c)\n",
      "#Adiabatic compression\n",
      "gama = Cp/Cv;\n",
      "V1 = (R*T1)/(P1**(10**5));\n",
      "V2 = V1*(P1/P2);\n",
      "T2_c = T1*((V1/V2)**(gama-1));\t\t\t#Kelvin(K)\n",
      "P2_c = P1*((V1/V2)**gama);\t\t\t#bar\n",
      "#Umath.sing Eq. (3.31)\n",
      "W_c = round(Cv*(T2_c-T1));\t\t\t#W = Cv*del_T(Joules)\n",
      "Q_c = -W_c;\n",
      "\n",
      "print ('       (c) Adiabatic compression followed by cooling at consmath.tant Volume')\n",
      "print 'work done by Adiabatic compression Followed by Cooling at const Vol ',W_c,'J'\n",
      "print 'Heat Transferred Q',Q_c,'J'\n",
      "print 'change in Internal Energy and enthalpy  =  0'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "       (a) Heating at consmath.tant volume Followed by cooling at consmath.tant Pressure\n",
        "work done by heating at const vol followed by const Pressure  9915.0 J\n",
        "Heat Transferred Q  -9915.0 J\n",
        "change in Internal Energy and enthalpy  =  0\n",
        "       (b) Isothermal compression\n",
        "work done by Isothermal compression  3990.0 J\n",
        "Heat Transferred Q -3990.0 J\n",
        "change in Internal Energy and enthalpy  =  0\n",
        "       (c) Adiabatic compression followed by cooling at consmath.tant Volume\n",
        "work done by Adiabatic compression Followed by Cooling at const Vol  5600.0 J\n",
        "Heat Transferred Q -5600.0 J\n",
        "change in Internal Energy and enthalpy  =  0\n"
       ]
      },
      {
       "metadata": {},
       "output_type": "display_data",
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zEhcmX2iv9oIdO+DNN2H2bEhKMong+uuhSZNzPlWkNlMCkBrZdmgbczbOYc6m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\niIiIiIiI/f1/TPX8ZedkZoAAAAAASUVORK5CYII=\n",
       "text": [
        "<matplotlib.figure.Figure at 0x107a52c90>"
       ]
      }
     ],
     "prompt_number": 2
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.3 page no : 48"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "%matplotlib inline\n",
      "\n",
      "from matplotlib.pyplot import plot,suptitle,xlabel,ylabel\n",
      "import math \n",
      "from numpy import linspace\n",
      "\n",
      "# Variables\n",
      "#Figure\n",
      "V = linspace(2083,2853,1541);\n",
      "P = 2853*V**-1;\n",
      "P = P**1.67;\n",
      "plot(V,P)\n",
      "P = [1.698, 1.698];\n",
      "V = [1690 ,2083];\n",
      "plot(V,P)\n",
      "V = linspace(1690,2853,2327)\n",
      "P = 2853*V**-1;\n",
      "plot(V,P)\n",
      "suptitle(\"Diagram for Ex.3.3\")\n",
      "xlabel(\"V\")\n",
      "ylabel(\"P\")\n",
      "\n",
      "# Variables for the Ideal Gas\n",
      "R = 8.314;\t\t\t#J/Mol/K\n",
      "Cv = (3./2)*R;\t\t\t#J/Mol/K\n",
      "Cp = (5./2)*R;\t\t\t#J/Mol/K\n",
      "gama = Cp/Cv;\n",
      "\n",
      "# Calculations and Results\n",
      "\n",
      "#(a)\n",
      "#Adiabatic Compression\n",
      "P1 = 1;\t\t\t#Pressure = 1bar\n",
      "T1 = 343.15;\t\t\t#Temp1 = 343.15K(70`C)\n",
      "T2 = 423.15;\t\t\t#Temp2 = 423.15K(150`C)\n",
      "Q_a = 0;\t\t\t#Adiabatic Compression\n",
      "del_U_a = (Cv*(T2-T1));\n",
      "W_a = del_U_a;\n",
      "del_H_a = (Cp*(T2-T1));\n",
      "#Umath.sing Eq. (3.29b)\n",
      "P2 = P1*((T2/T1)**(gama/(gama-1)));\t\t\t#bar\n",
      "\n",
      "#(b)\n",
      "#cooled form 150`C to 70`C at Const pressure\n",
      "#Umath.sing Eq.(3.27)\n",
      "Q_b = round(Cp*(T1-T2));\n",
      "del_H_b = Q_b;\n",
      "#for Ideal Gas\n",
      "del_U_b = round(Cv*(T1-T2));\n",
      "#by First law\n",
      "W_b = del_U_b-Q_b;\t\t\t#Joules\n",
      "\n",
      "#(c)\n",
      "#Expanded Isothermally to original state\n",
      "del_U_c = 0;\t\t\t#isothermal\n",
      "del_H_c = 0;\t\t\t#isothermal\n",
      "Q_c = round(R*T1*math.log(P2/P1));\n",
      "W_c = -Q_c;\n",
      "\n",
      "#Entire process\n",
      "Qt  =  Q_a+Q_b+Q_c;\n",
      "Wt  =  W_a+W_b+W_c;\n",
      "del_Ut = del_U_a+del_U_b+del_U_c;\n",
      "del_Ht = del_H_a+del_H_b+del_H_c;\n",
      "\n",
      "\n",
      "#PartII(Irreversible)\n",
      "eta = .80;\t\t\t#Efficiency = 80%\n",
      "\n",
      "#(a)\n",
      "Wm_a = (W_a/eta);\n",
      "Qm_a = del_U_a-Wm_a;\t\t\t#del_U remains same (by First Law)\n",
      "\n",
      "#(b)\n",
      "Wm_b = round(W_b/eta);\n",
      "Qm_b = del_U_b-Wm_b;\t\t\t#del_U remains same (by First Law)\n",
      "\n",
      "#(c)\n",
      "Wm_c = round(W_c*eta);\n",
      "Qm_c = del_U_c-Wm_c;\t\t\t#del_U remains same (by First Law)\n",
      "\n",
      "#Entire Process\n",
      "Qmt  =  Qm_a+Qm_b+Qm_c;\n",
      "Wmt  =  Wm_a+Wm_b+Wm_c;\n",
      "\n",
      "\n",
      "del_U_rev = [del_U_a,del_U_b,del_U_c];\n",
      "del_H_rev = [del_H_a,del_H_b,del_H_c];\n",
      "Qrev = [Q_a,Q_b,Q_c];\n",
      "Wrev = [W_a,W_b,W_c];\n",
      "Sumr = [del_Ut,del_Ht,Qt,Wt];\n",
      "\n",
      "del_U_irev = del_U_rev;\n",
      "del_H_irev = del_H_rev;\n",
      "Qirev = [Qm_a,Qm_b,Qm_c];\n",
      "Wirev = [Wm_a,Wm_b,Wm_c];\n",
      "Sumi = [del_Ut,del_Ht,Qmt,Wmt];\n",
      "\n",
      "\n",
      "print ('     (a)Adiabatic Compression')\n",
      "print ('     (b)Cooled form 150`C to 70`C at Const pressure')\n",
      "print ('     (c)Expanded Isothermally to original state')\n",
      "\n",
      "print ('   Mechanically reversible');\n",
      "\n",
      "Ans_rev = [del_U_rev,del_H_rev,Qrev,Wrev];\n",
      "\n",
      "print '   del U   del H     Q        W',Ans_rev,'Sum',Sumr\n",
      "print ('        Irreversible');\n",
      "\n",
      "Ans_irev = [del_U_irev,del_H_irev,Qirev,Wirev];\n",
      "\n",
      "print '   del U   del H     Q        W',Ans_irev,'Sum',Sumi\n",
      "\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "     (a)Adiabatic Compression\n",
        "     (b)Cooled form 150`C to 70`C at Const pressure\n",
        "     (c)Expanded Isothermally to original state\n",
        "   Mechanically reversible\n",
        "   del U   del H     Q        W [[997.6800000000001, -998.0, 0], [1662.8, -1663.0, 0], [0, -1663.0, 1495.0], [997.6800000000001, 665.0, -1495.0]] Sum [-0.31999999999993634, -0.20000000000004547, -168.0, 167.68000000000006]\n",
        "        Irreversible\n",
        "   del U   del H     Q        W [[997.6800000000001, -998.0, 0], [1662.8, -1663.0, 0], [-249.41999999999985, -1829.0, 1196.0], [1247.1, 831.0, -1196.0]] Sum [-0.31999999999993634, -0.20000000000004547, -882.4200000000001, 882.0999999999999]\n"
       ]
      },
      {
       "metadata": {},
       "output_type": "display_data",
       "png": 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XpqQGD7a/zhHm4EFo2RIqVbKN5zr4KLKoKaBILPjhB1tG+8031jOqfvaV4+7t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\n",
       "text": [
        "<matplotlib.figure.Figure at 0x107c669d0>"
       ]
      }
     ],
     "prompt_number": 5
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.4  page no : 49"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "%matplotlib inline\n",
      "\n",
      "from matplotlib.pyplot import plot,suptitle,xlabel,ylabel\n",
      "from numpy import linspace\n",
      "import math \n",
      "\n",
      "\n",
      "#Figure\n",
      "P = [1.35 ,1.35];\n",
      "V = [0.24, 0.264];\n",
      "plot(V,P)\n",
      "V = linspace(0.12,0.24,121)\n",
      "P = 0.324*V**-1;\n",
      "plot(V,P)\n",
      "P = [2.7, 2.97];\n",
      "V = [0.12, 0.12];\n",
      "plot(V,P)\n",
      "suptitle(\"Diagram for Ex.3.4\")\n",
      "xlabel(\"V(m**3)\")\n",
      "ylabel(\"P(bar)\")\n",
      "\n",
      "P = [2.97, 2.97];\n",
      "V = [0 ,0.12];\n",
      "plot(V,P)\n",
      "P = [2.7, 2.7];\n",
      "V = [0 ,0.12];\n",
      "plot(V,P)\n",
      "P = [1.35, 1.35];\n",
      "V = [0 ,0.24];\n",
      "plot(V,P)\n",
      "P = [0, 2.7];\n",
      "V = [0.12, 0.12];\n",
      "plot(V,P)\n",
      "P = [0 ,1.35];\n",
      "V = [0.24, 0.24];\n",
      "plot(V,P)\n",
      "P = [0 ,1.35];\n",
      "V = [0.264, 0.264];\n",
      "plot(V,P)\n",
      "\n",
      "\n",
      "# Variables\n",
      "m = 0.4;\t\t\t#Kg\n",
      "M = 28.;\t\t\t#Molecular Mass Of Nitrogen\n",
      "T1 = 300.15;\t\t\t#Temp = 300.15K(27`C)\n",
      "Pn = 0.35;\t\t\t#Pressure of nitrogen  =  0.35bar\n",
      "Pa = 1.;\t\t\t#Atm Pressure  =  1bar\n",
      "R = 8.314;\t\t\t#J/Mol/K\n",
      "Cv = (5./2)*R;\t\t\t#J/Mol/K\n",
      "Cp = (7./2)*R;\t\t\t#J/Mol/K\n",
      "gama = Cp/Cv;\n",
      "\n",
      "n = (m/M)*1000;\t\t\t#moles\n",
      "\n",
      "# Calculations and Results\n",
      "\n",
      "#(a)\n",
      "#Immersed In ice/water bath\n",
      "T2 = 273.15;\t\t\t#Temp = 273.15K(0`C)\n",
      "W_a = -round(n*R*(T2-T1));\t\t\t#Joules\n",
      "del_H_a = round(Cp*(T2-T1),0);\n",
      "Q_a =  (n*del_H_a);\n",
      "del_U_a = round((Q_a+W_a)/n,0);\n",
      "print ('(a)Immersed In ice/water bath')\n",
      "print 'work done ',W_a,'J'\n",
      "print 'Heat Transferred Q  =  ',Q_a,'J'\n",
      "print 'change in Internal Energy ',del_U_a,'J'\n",
      "print 'change in enthalpy ',del_H_a,'J'\n",
      "\n",
      "\n",
      "#(b)\n",
      "#Isothermal Compression\n",
      "del_U_b = 0;\t\t\t#Isothermal\n",
      "del_H_b = 0;\t\t\t#Isothermal\n",
      "W_b = -round(n*R*T2*math.log(1./2));\t\t\t#W = nRTln(V3/V2),here V3/V2 = 0.5(Given)\n",
      "Q_b = -W_b;\n",
      "print ('(b)Isothermal Compression')\n",
      "print 'work done by Isothermal Compression ',W_b,'J'\n",
      "print 'Heat Transferred Q  =  ',Q_b,'J'\n",
      "print 'change in Internal Energy ',del_U_b,'J'\n",
      "print 'change in enthalpy ',del_H_b,'J'\n",
      "\n",
      "\n",
      "#(c)\n",
      "#constant Vol Process\n",
      "W_c = 0;\t\t\t#const Vol\n",
      "del_H_c = round((Cp*(T1-T2))/n,0);\n",
      "del_U_c = round(Cv*(T1-T2),0);\n",
      "Q_c = round(n*del_U_c);\n",
      "print ('(c)Consmath.tant Vol Process')\n",
      "print 'work done by Const Vol Process ',W_c,'J'\n",
      "print 'Heat Transferred Q  =  ',Q_c,'J'\n",
      "print 'change in Internal Energy ',del_U_c,'J'\n",
      "print 'change in enthalpy ',del_H_c,'J'\n",
      "\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a)Immersed In ice/water bath\n",
        "work done  3207.0 J\n",
        "Heat Transferred Q  =   -11228.5714286 J\n",
        "change in Internal Energy  -562.0 J\n",
        "change in enthalpy  -786.0 J\n",
        "(b)Isothermal Compression\n",
        "work done by Isothermal Compression  22487.0 J\n",
        "Heat Transferred Q  =   -22487.0 J\n",
        "change in Internal Energy  0 J\n",
        "change in enthalpy  0 J\n",
        "(c)Consmath.tant Vol Process\n",
        "work done by Const Vol Process  0 J\n",
        "Heat Transferred Q  =   8014.0 J\n",
        "change in Internal Energy  561.0 J\n",
        "change in enthalpy  55.0 J\n"
       ]
      },
      {
       "metadata": {},
       "output_type": "display_data",
       "png": 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TODnvuZOAO4ALgFuasK1NCZd12JxwfZzrI54D+BUhEHYjXE9nRPb52YSzY7/W\ntN2QJMVhA2Ax9Re37AG8np1+iXBZBoAzCB/mfyXcX+B84BLgecJlprtml+uWnT+R+ssgNPZcrmHA\n1TmPLwPOa/YeSZJa1EOEi7oBXE74lt8NeDFnmTMId+76CrAR4dIbZ2fnXQtcBGwC3AAMB04ndFk1\n9lyd/yVcuuNlwr1D6hwA3NUSOyZJKt6phO4lCNe26U24M+Bfc5YZTPiwr/M6IQAAzgR+nbfs2sYk\ncl0O3JzzeAfCjW+ksuOYhFqjicC3COHQiRAU0LBraEXOdG3O41pWvxfLrdR3Wa3puTp3sPoF11KU\n/z0a1EoZEmqNPgamEr7N17UoXidc1bXOmm521ZwbYW2XM3009cEEoYUSFShSopK8M52UpDuB+4CB\n2cf/Ifx/6AQsJ3yzz/12nz/d1G/+VwHfAL4gXM9/aM68fsATTdyeJKnERhIOhy21NB4CK0llb2Pq\n7xRYKrsQboAjSZIkSZIkSZIkSZIkSZIkSSre/wekZFbyO1hb0gAAAABJRU5ErkJggg==\n",
       "text": [
        "<matplotlib.figure.Figure at 0x107a522d0>"
       ]
      }
     ],
     "prompt_number": 7
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.6  page no : 49"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "# Variables\n",
      "n = 1.;\t\t\t#Molar Rate(mol/s)\n",
      "D = 5.;\t\t\t#inner Diameter(cm)\n",
      "R = 83.14;\n",
      "Cp = (7./2)*R;\n",
      "M = 29*10.**-3;\t\t\t#Molar mass(g/mol)\n",
      "T = 293.15;\t\t\t#temperature = 293.15K(20`C)\n",
      "P1 = 6.;\t\t\t#Upstream Pressure\n",
      "P2 = 3.;\t\t\t#Downstream Pressure\n",
      "\n",
      "# Calculations\n",
      "#from Eq.(2.24b)\n",
      "A = (math.pi/4)*((D*10**-2)**2);\t\t\t#Area(m**2)\n",
      "#upstream molar Volume\n",
      "V1 = (R*T/P1)*10**-6;\t\t\t#m**3/mol\n",
      "u1 = n*V1/A;\t\t\t#velocity(m/s)\n",
      "V2 = 2*V1;\n",
      "u2 = 2*u1;\n",
      "del_KE = round(n*M*((u2**2)-(u1**2))/2,3);\t\t\t#J/s(W)\n",
      "del_T = round(-del_KE/(Cp*0.1),4);\t\t\t#K\n",
      "\n",
      "# Results\n",
      "print 'Change in KE ',del_KE,'W or J/s'\n",
      "print 'Change in Temperature ',del_T,'K'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Change in KE  0.186 W or J/s\n",
        "Change in Temperature  -0.0064 K\n"
       ]
      }
     ],
     "prompt_number": 8
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.7  page no : 50"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "# Variables\n",
      "T = 473.15;\t\t\t#Temp = 473.15k(200`C)\n",
      "P = 10.;\t\t\t#Pressure = 10bar\n",
      "B = -0.388;\t\t\t#Viral Coefficient(m**3/Kmol)\n",
      "C = -26.*(10**(-3));\t\t\t#Viral Coefficient(m**6/(kmol)**2)\n",
      "\n",
      "# Calculate V and Z for isopropyl vapor\n",
      "R = 83.14*(10**(-3));\t\t\t#m**3bar/Kmol/K\n",
      "\n",
      "# Calculations and Results\n",
      "#(a)\n",
      "#Ideal Gas equation\n",
      "V_a = round((R*T)/P,3);\n",
      "Z_a = 1.;\t\t\t#Ideal Gas\n",
      "print ('(a) By Ideal gas Equation')\n",
      "print 'V  =  ',V_a,'m**3/kmol'\n",
      "print 'Z  =  ',Z_a\n",
      "\n",
      "#(b)\n",
      "#Using Eqution 3.37 -> Z = PV/RT = 1+BP/RT\n",
      "V_b = round((R*T/P)+B,3);\n",
      "Z_b = round(P*V_b/(R*T),4);\n",
      "print ('(b) Using Eqution 3.37 -> Z = PV/RT = 1+BP/RT')\n",
      "print 'V  =  ',V_b,'m**3/kmol'\n",
      "print 'Z  =  ',Z_b\n",
      "\n",
      "#(c)\n",
      "#Using Equation 3.39 -> Z = PV/RT = 1+(B/V)+(C/(V**2))\n",
      "#Iterations\n",
      "a = V_a;\t\t\t#Initial\n",
      "i = -1;\n",
      "while(i == -1):\n",
      "    b = ((R*T/P)*(1+(B/a)+(C/(a**2))));\n",
      "    c = abs(b-a)\n",
      "    if(c <= 0.0001):\n",
      "        i = 1;\n",
      "        break;\n",
      "    a = b;\n",
      "\n",
      "V_c = round(b,3);\n",
      "Z_c = round(P*V_c/(R*T),4);\n",
      "#Ans\n",
      "print ('(c) Using Equation 3.39 -> Z = PV/RT = 1+(B/V)+(C/(V**2))')\n",
      "print 'V  =  ',V_c,'m**3/kmol'\n",
      "print 'Z  =  ',Z_c\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a) By Ideal gas Equation\n",
        "V  =   3.934 m**3/kmol\n",
        "Z  =   1.0\n",
        "(b) Using Eqution 3.37 -> Z = PV/RT = 1+BP/RT\n",
        "V  =   3.546 m**3/kmol\n",
        "Z  =   0.9014\n",
        "(c) Using Equation 3.39 -> Z = PV/RT = 1+(B/V)+(C/(V**2))\n",
        "V  =   3.488 m**3/kmol\n",
        "Z  =   0.8867\n"
       ]
      }
     ],
     "prompt_number": 9
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.8  page no : 52"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "import math \n",
      "from numpy import array,zeros\n",
      "\n",
      "# Variables\n",
      "T = 350.;\t\t\t#Temp = 350K(76.85`C)\n",
      "P = 9.4573;\t\t\t#Pressure = 9.4573bar\n",
      "R = 83.14;\n",
      "\n",
      "Tc = 425.1;\t\t\t#App B\n",
      "Pc = 37.96;\t\t\t#App B\n",
      "Tr = T/Tc;\n",
      "Pr = P/Pc;\n",
      "#Parameters for RK\n",
      "si = 0.42748;\n",
      "omega = 0.08664;\n",
      "epsilon = 0;\n",
      "sigma = 1;\n",
      "a = Tr**-0.5;\n",
      "\n",
      "# Calculations and Results\n",
      "#Using Eq(3.51)\n",
      "q = si*a/(omega*Tr);\n",
      "Beta = omega*Pr/Tr;\n",
      "\n",
      "print ('The Following Results given By Redlich/Kwong Equation')\n",
      "#(a)\n",
      "Z = 1.;\t\t\t#initial\n",
      "a = Z;\n",
      "for i in range(0,11):\n",
      "    b = 1+Beta-((q*Beta)*(a-Beta)/(a*(a+Beta)));\n",
      "    if((b-a) == 0.0001):\n",
      "        break;\n",
      "    a = b;\n",
      "    \n",
      "Z = round(b,4)\n",
      "V = round(Z*R*T/P);\n",
      "print 'Molar Volume of saturated Vapor is ',V,'cm**3/mol'\n",
      "\n",
      "#(b)  \n",
      "Z = Beta;\t\t\t#initial\n",
      "a = Z;\n",
      "for i in range(0,21):\n",
      "    b = Beta+(a*(a+Beta)*(1+Beta-a)/(q*Beta));\n",
      "    if((b-a) == 0.0001):\n",
      "        break;\n",
      "    a = b;\n",
      "    i = i+1;\n",
      "\n",
      "Z = round(b,5)\n",
      "V = round(Z*R*T/P,1);\n",
      "print 'Molar Volume of Saturated Liquid is ',V,'cm**3/mol'\n",
      "\n",
      "# Variables\n",
      "T = 350.;\t\t\t#Temp = 350K(76.85`C)\n",
      "P = 9.4573;\t\t\t#Pressure = 9.4573bar\n",
      "R = 83.14;\n",
      "\n",
      "Tc = 425.1;\t\t\t#App B\n",
      "Pc = 37.96;\t\t\t#App B\n",
      "Tr = T/Tc;\n",
      "Pr = P/Pc;\n",
      "#Parameters for eqns[vdW,RK,SRK,PR]\n",
      "si = array([27./64,0.42748,0.42748,0.45724]);\n",
      "omega = array([1./8,0.08664,0.08664,0.07779]);\n",
      "epsilon = array([0,0,0,(1-math.sqrt(2))]);\n",
      "sigma = array([0,1,1,(1+math.sqrt(2))]);\n",
      "w = 0.2;\t\t\t#App B\n",
      "aSRK = (1+((0.480+(1.574*w)-(0.1768*w**2))*(1-Tr**0.5)))**2;\n",
      "aPR = (1+((0.37464+(1.54226*w)-(0.26992*w**2))*(1-Tr**0.5)))**2;\n",
      "a = [1,Tr**-0.5,aSRK,aPR];\n",
      "\n",
      "\n",
      "print ('      By All Equations')\n",
      "#Using Eq(3.51)\n",
      "q = si*a/(omega*Tr);\n",
      "Beta = omega*Pr/Tr;\n",
      "\n",
      "#print ('The Following Results given By Redlich/Kwong Equation')\n",
      "#(a)\n",
      "z = zeros(4)\n",
      "for j in range(4):\n",
      "    Z = 1;\t\t\t#initial\n",
      "    A = Z;\n",
      "    for i in range(11):\n",
      "        b = 1+Beta[j]-((q[j]*Beta[j])*(A-Beta[j])/((A+(epsilon[j]*Beta[j]))*(A+(sigma[j]*Beta[j]))));\n",
      "        if((b-A) == 0.0001):\n",
      "            break;\n",
      "        A = b;\n",
      "    z[j] = round(b,4);\n",
      "\n",
      "V = round(Z*R*T/P,1)\n",
      "print ('Molar Volume(Vv) of Saturated Vapor'); \n",
      "print V \n",
      "\n",
      "#(b)  \n",
      "for j in range(4):\n",
      "    Z = Beta[j];\t\t\t#initial\n",
      "    A = Z;\n",
      "    for i in range(21):\n",
      "        b = Beta[j]+((A+(epsilon[j]*Beta[j]))*(A+(sigma[j]*Beta[j]))*(1+Beta[j]-A)/(q[j]*Beta[j]));\n",
      "        if((b-A) == 0.0001):\n",
      "            break;\n",
      "        A = b;\n",
      "        i = i+1;\n",
      "    z[j] = round(b,5);\n",
      "\n",
      "V = round(Z*R*T/P,1);\n",
      "print ('Molar Volume(Vl) of Saturated Liquid'); \n",
      "print V\n",
      "\n",
      "print ('Note : Exp Value is Vv  =  2482 cm**3/mol and Vl  =  115 cm**3/mol')\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "The Following Results given By Redlich/Kwong Equation\n",
        "Molar Volume of saturated Vapor is  2555.0 cm**3/mol\n",
        "Molar Volume of Saturated Liquid is  133.3 cm**3/mol\n",
        "      By All Equations\n",
        "Molar Volume(Vv) of Saturated Vapor\n",
        "3076.9\n",
        "Molar Volume(Vl) of Saturated Liquid\n",
        "72.4\n",
        "Note : Exp Value is Vv  =  2482 cm**3/mol and Vl  =  115 cm**3/mol\n"
       ]
      }
     ],
     "prompt_number": 12
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.9  page no : 53"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "# Variables\n",
      "T = 510.\t\t\t#Temp = 510K\n",
      "P = 25.\t    \t\t#Pressure = 25bar\n",
      "R = 0.08314;\n",
      "\n",
      "\n",
      "# Calculations and Results\n",
      "#(a)\n",
      "#By the Ideal-gas Equation\n",
      "V = round(R*T/P,4);\t\t\t#m**3/kmol\n",
      "print ('(a)By the Ideal-gas Equation')\n",
      "print 'The Molar Volume is ',V,'m**3/kmol'\n",
      "\n",
      "#(b)\n",
      "#The Generalized compressibility-factor Correlation\n",
      "Tc = 425.1;\t\t\t#From App.B\n",
      "Pc = 37.96;\t\t\t#From App.B\n",
      "Tr = round(T/Tc,1);\n",
      "Pr = round(P/Pc,3)\n",
      "#Interpolation in Tables E.1 and E.2 then provides\n",
      "Z0 = 0.865;\n",
      "Z1 = 0.038;\n",
      "w = 0.200;\n",
      "Z = Z0+(w*Z1);\n",
      "V = round(Z*R*T/P,2);\t\t\t#m**3/kmol\n",
      "print ('(b)The Generalized compressibility-factor Correlation')\n",
      "print 'The Molar Volume is ',V,'m**3/kmol'\n",
      "\n",
      "#(c)\n",
      "#The Generalized Virial-coefficient Correlation\n",
      "B0 = 0.083-(0.422/(Tr**1.6));\t\t\t#Eqn (3.61)\n",
      "B1 = 0.139-(0.172/(Tr**4.2));\t\t\t#Eqn (3.62)\n",
      "K = round(B0+(w*B1),3)\t\t\t#K = BPc/RTc By Eqn (3.59)\n",
      "#By Eqn(3.58)\n",
      "Z = round(1+(K*Pr/Tr),3)\n",
      "V = round(Z*R*T/P,4);\t\t\t#m**3/kmol\n",
      "print ('(c)The Generalized Virial-coefficient Correlation')\n",
      "print 'The Molar Volume is ',V,'m**3/kmol'\n",
      "\n",
      "\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a)By the Ideal-gas Equation\n",
        "The Molar Volume is  1.6961 m**3/kmol\n",
        "(b)The Generalized compressibility-factor Correlation\n",
        "The Molar Volume is  1.48 m**3/kmol\n",
        "(c)The Generalized Virial-coefficient Correlation\n",
        "The Molar Volume is  1.4908 m**3/kmol\n"
       ]
      }
     ],
     "prompt_number": 13
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.10  page no : 54"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "# Variables\n",
      "T = 323.15;\t\t\t#Temp = 323.15K(50`C)\n",
      "V = 0.125;\t\t\t#Volume = 0.125m**3\n",
      "R = 0.08314;\n",
      "\n",
      "# Calculations and Results\n",
      "#(a)\n",
      "#By Ideal-gas equation,\n",
      "P = round(R*T/V,1);\t\t\t#in bar\n",
      "print ('(a)By Ideal-gas equation')\n",
      "print 'Pressure is ',P,'bar'\n",
      "\n",
      "#(b)\n",
      "#for Redlich/Kwong equation\n",
      "Tc = 190.6;\t\t\t#App B\n",
      "Tr = T/Tc;\n",
      "si = 0.42748;\n",
      "omega = 0.08664;\n",
      "Pc = 45.99;\t\t\t#App B\n",
      "a = round(si*((Tr**(-0.5))*(R**2)*(Tc**2))/Pc,3)\t\t\t#Eqn (3.42)Units of a(T) bar m**6\n",
      "b = round(omega*R*Tc/Pc,5)\t\t\t#Eqn (3.43)Units of b m**3\n",
      "#Umath.sing eqn (3.41)\n",
      "#P = RT/(V-b)-a(T)/(V+Eb)(V+~b),E->epsilon,~->sigma\n",
      "epsilon = 0;\n",
      "sigma = 1;\n",
      "P = round(((R*T/(V-b))-(a/((V+(epsilon*b))*(V+(sigma*b))))),2);\n",
      "print ('(b)for Redlich/Kwong equation')\n",
      "print 'Pressure is ',P,'bar'\n",
      "\n",
      "#(c)\n",
      "#A generalized Correlation\n",
      "Z0 = 0.887;\t\t\t#from Table E.3 and E.4\n",
      "Z1 = 0.258;\t\t\t#from Table E.3 and E.4\n",
      "w = 0.012;\n",
      "Z = Z0+(w*Z1);\n",
      "P = round(Z*R*T/V,1);\t\t\t#bar\n",
      "print ('(c)A generalized Correlation')\n",
      "print 'Pressure is ',P,'bar'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a)By Ideal-gas equation\n",
        "Pressure is  214.9 bar\n",
        "(b)for Redlich/Kwong equation\n",
        "Pressure is  189.73 bar\n",
        "(c)A generalized Correlation\n",
        "Pressure is  191.3 bar\n"
       ]
      }
     ],
     "prompt_number": 15
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.11  page no : 55"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "# Variables\n",
      "T = 338.15;\t\t\t#Temp = 338.15K(65`C)\n",
      "Vt = 0.03;\t\t\t#Volume = 0.03m**3\n",
      "R = 0.08314;\n",
      "m = 0.5;\t\t\t#mass in Kg\n",
      "M = 17.02;\t\t\t#Molecular Mass\n",
      "V = Vt/(m/M);\t\t\t# n = m/M(moles)\n",
      "\n",
      "# Calculations and Results\n",
      "#(a)\n",
      "#By Ideal-gas equation,\n",
      "P = round(R*T/V,2);\t\t\t#in bar\n",
      "print ('(a)By Ideal-gas equation')\n",
      "print 'Pressure is ',P,'bar'\n",
      "\n",
      "#(b)\n",
      "#A generalized correlation\n",
      "Tc = 405.7;\t\t\t#App B\n",
      "Tr = T/Tc;\n",
      "Pc = 112.8;\t\t\t#App B\n",
      "B0 = 0.083-(0.422/(Tr**1.6));\t\t\t#Eqn (3.61)\n",
      "B1 = 0.139-(0.172/(Tr**4.2));\t\t\t#Eqn (3.62)\n",
      "#Substituting in eq(3.59)\n",
      "w = 0.253;\n",
      "K = B0+(w*B1);\t\t\t#K = BPc/RTc\n",
      "B = K*R*Tc/Pc;\t\t\t#m**3 kmol**-1\n",
      "#solving eq.(3.37)\n",
      "P = round(R*T/(V-B),2);\n",
      "print ('(b)A generalized Correlation')\n",
      "print 'Pressure is ',P,'bar'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a)By Ideal-gas equation\n",
        "Pressure is  27.53 bar\n",
        "(b)A generalized Correlation\n",
        "Pressure is  23.77 bar\n"
       ]
      }
     ],
     "prompt_number": 16
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 3.12  page no : 56"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "\n",
      "import math \n",
      "\n",
      "\n",
      "# Variables\n",
      "T = 310;\t\t\t#Temp = 310K(36.85`C)\n",
      "M = 17.02;\n",
      "\n",
      "# Calculations and Results\n",
      "#(a)\n",
      "#saturated liquid\n",
      "Tc = 405.7;\t\t\t#App B\n",
      "Vc = 0.07247;\t\t\t#App B\n",
      "Zc = 0.242;\t\t\t#App B\n",
      "Vsat = round(Vc*(Zc**((1-Tr)**0.2857)),5);\t\t\t#m**3kmol**-1\n",
      "rho = round(M/Vsat,2);\n",
      "print ('(a)Saturated liquid')\n",
      "print 'Volume is ',Vsat,'m**3/kmol'\n",
      "print 'Density is ',rho,'kmol/m**3'\n",
      "\n",
      "#(b)\n",
      "#Liquid at 100bar\n",
      "P = 100.;\t\t\t#Pressure = 100bar\n",
      "Pc = 112.8;\t\t\t#App B\n",
      "Pr = P/Pc;\n",
      "rho_r = 2.38;\t\t\t#From Graph\n",
      "V = Vc/rho_r;\n",
      "#but this Gives large error\n",
      "rho_r1 = 2.34;\n",
      "V_new = round(V*rho_r1/rho_r,5);\n",
      "#In excepmath.tance with Experimental Value\n",
      "\n",
      "rho = round(M/V_new,2);\n",
      "print ('(b)For Liquid at 100bar')\n",
      "print 'Volume is ',V_new,'m**3/kmol'\n",
      "print 'Density is ',rho,'kmol/m**3'\n",
      "\n",
      "\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "(a)Saturated liquid\n",
        "Volume is  0.03097 m**3/kmol\n",
        "Density is  549.56 kmol/m**3\n",
        "(b)For Liquid at 100bar\n",
        "Volume is  0.02994 m**3/kmol\n",
        "Density is  568.47 kmol/m**3\n"
       ]
      }
     ],
     "prompt_number": 17
    }
   ],
   "metadata": {}
  }
 ]
}