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  {
   "cells": [
    {
     "cell_type": "heading",
     "level": 1,
     "metadata": {},
     "source": [
      "Chapter 6 : Thermodynamics Properties of Fluids"
     ]
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.1  page no : 88"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "import math \n",
      "\n",
      "# Variables\n",
      "\n",
      "#At Temp T1 = 298.15K\n",
      "T1 = 298.15;\t\t\t#[K]\n",
      "P1 = 1.;\t    \t\t#[bar]\n",
      "P2 = 1000.;\t\t    \t#[bar]\n",
      "Cp_T1 = 75.305;\t\t\t#[KJ Kmol/K]\n",
      "V1_T1 = 18.071*10**-3;\t\t\t#[m**3/Kmol]\n",
      "V2_T1 = 18.012*10**-3;\t\t\t#[m**3/Kmol]\n",
      "beta1_T1 = 256.*10**-6;\t\t\t#[1/K]\n",
      "beta2_T1 = 366.*10**-6;\t\t\t#[1/K]\n",
      "\n",
      "#At Temp T2 = 323.15K\n",
      "T2 = 323.15;\t\t\t#[K]\n",
      "P1 = 1.;\t\t\t#[bar]\n",
      "P2 = 1000.;\t\t\t#[bar]\n",
      "Cp_T2 = 75.314;\t\t\t#[KJ Kmol/K]\n",
      "V1_T2 = 18.234*10**-3;\t\t\t#[m**3/Kmol]\n",
      "V2_T2 = 18.174*10**-3;\t\t\t#[m**3/Kmol]\n",
      "beta1_T2 = 458.*10**-6;\t\t\t#[1/K]\n",
      "beta2_T2 = 568.*10**-6;\t\t\t#[1/K]\n",
      "\n",
      "#Solution\n",
      "\n",
      "#Formula to be used\n",
      "#Eqn (6.28) del_H = ((Cp)(T2-T1))-((V)(1-(beta)(T2)(P2-P1))\n",
      "#Eqn (6.29) del_S = ((Cp)ln(T2/T1)-((beta)(V)(P2-P1))\n",
      "\n",
      "#For P = 1\n",
      "Cp = (Cp_T1+Cp_T2)/2;\n",
      "#For T = 323.15K\n",
      "V = (V1_T2+V2_T2)/2;\n",
      "beta_T = (beta1_T2+beta2_T2)/2;\n",
      "\n",
      "del_H = round((Cp*(T2-T1))+(V*(1-(beta_T*T2))*(P2-P1)*10**5*10**-3),0);\n",
      "del_S = round((Cp*(math.log(T2/T1)))-(beta_T*V*(P2-P1)*10**5*10**-3),2);\n",
      "\n",
      "print 'Change In Enthalpy',del_H,'KJ/Kmol'\n",
      "print 'Change In Entropy',del_S,'KJ/Kmol/K'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Change In Enthalpy 3400.0 KJ/Kmol\n",
        "Change In Entropy 5.13 KJ/Kmol/K\n"
       ]
      }
     ],
     "prompt_number": 1
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.3  page no : 89"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "%matplotlib inline\n",
      "import math \n",
      "from matplotlib.pyplot import plot,suptitle,xlabel,ylabel\n",
      "from numpy import array\n",
      "\n",
      "def ICPS(T0,T,A,B,C,D):\n",
      "    t = T/T0;\n",
      "    return  ((A)*math.log(t))+(((B*T0)+(((C*T0*T0)+(D/(t*t*T0*T0)))*(t+1)/2))*(t-1))\n",
      "\n",
      "def ICPH(T0,T,A,B,C,D):\n",
      "    t = T/T0;\n",
      "    return (A+((B/2)*T0*(t+1))+((C/3)*T0*T0*((t**2)+t+1))+(D/(t*T0*T0)))*(T-T0)\n",
      "\n",
      "# Variables\n",
      "T0 = 300.;\t\t\t#[K]\n",
      "T = 360.;\t\t\t#[K]\n",
      "R = 8.314;\n",
      "P = 15.14;\t\t\t#[bar]\n",
      "A = 1.7765;\n",
      "B = 33.037*10**-3;\n",
      "C = 0;\n",
      "D = 0;\n",
      "H0 = 18115.;  \t\t\t#J/mol\n",
      "S0 = 295.976;\t\t\t#J/mol/K\n",
      "\n",
      "#Graph\n",
      "X = array([0,0.10,0.50,2,4,6,8,10,12,14,15.41]);\n",
      "Y1 = array([1.780,1.700,1.514,1.293,1.290,1.395,1.560,1.777,2.073,2.432,2.720]);\t\t\t#[(dZ/dT)p/P]\n",
      "Y2 = array([2.590,2.470,2.186,1.759,1.591,1.544,1.552,1.592,1.658,1.750,1.835]);\t\t\t#[-(Z-1)/P]\n",
      "plot(Y1,X);\n",
      "suptitle(\"(a)\")\n",
      "xlabel(\"P(bar)\")\n",
      "ylabel(\"[(dZ/dT)p/P]X10**4(K**-1 bar**-1)\");\n",
      "plot(Y2,X);\n",
      "suptitle(\"(b)\")\n",
      "xlabel(\"P(bar)\")\n",
      "ylabel(\"[-(Z-1)/P]X10**2(bar**-1)\");\n",
      "\n",
      "\n",
      "#Area Under the Curve (a)\n",
      "Y1 = Y1*10**-4;\n",
      "A1 = 0;\n",
      "for i in range(1,11):\n",
      "    A1 = A1+((X[i-1]-X[i])*Y1[i]);\n",
      "\n",
      "print 'Area under the graph(a)',A1*10000,'(X 10**-4) K**-1'\n",
      "#Area Under the Curve (b)\n",
      "Y2 = Y2*10**-2;\n",
      "A2 = 0;\n",
      "for i in range(1,11):\n",
      "    A2 = A2+((X[i-1]-X[i])*Y2[i]);\n",
      "\n",
      "print 'Area under the graph(b)',round(A2,4)\n",
      "\n",
      "\n",
      "K = A1*T;\t\t\t#Hr/RT\n",
      "#From Eqn(6.47)\n",
      "Hr = R*T*(K);\t\t\t#[J/mol]\n",
      "#From Eqn(6.48)\n",
      "Sr = R*(K-(A2));\t\t\t#[J/mol/K]\n",
      "\n",
      "#From Eqn(6.49) and Eqn(6.50)\n",
      "H1 = R*ICPH(T0,T,A,B,C,D);\n",
      "S1 = R*ICPS(T0,T,A,B,C,D);\n",
      "\n",
      "H = H0+H1+Hr;\n",
      "S = round(S0+S1+Sr-(R*math.log(P)),3);\n",
      "\n",
      "print 'Enthalpy',H,'J/mol'\n",
      "print 'Entropy',S,'J/mol/K'\n",
      "print ('Note: The Answer is different with that of the Book because the Method Used\\\n",
      " to find the Area under the Graph is done by finding the area of small Rectangles')\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        " Area under the graph(a) -27.6043 (X 10**-4) K**-1\n",
        "Area under the graph(b) -0.2572\n",
        "Enthalpy 21465.2998298 J/mol\n",
        "Entropy 286.433 J/mol/K\n",
        "Note: The Answer is different with that of the Book because the Method Used to find the Area under the Graph is done by finding the area of small Rectangles\n"
       ]
      },
      {
       "metadata": {},
       "output_type": "display_data",
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VszoyEf/LbrC4LfAY8B+UCPKNc5fP8dGmj9g4aqPVofjduXNmAtjkyaYLaNw46NlTE8Ck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\nRERERERERETEav8fNQToewWcF3kAAAAASUVORK5CYII=\n",
       "text": [
        "<matplotlib.figure.Figure at 0x110044150>"
       ]
      }
     ],
     "prompt_number": 4
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.4  page no : 92"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "import math \n",
      "\n",
      "# Variables\n",
      "T = 500.;\t\t\t#[K]\n",
      "R = 8.314;\n",
      "Tc = 425.1;\t\t\t#[K]\n",
      "P = 50.;\t\t\t#[bar]\n",
      "Pc = 37.96;\t\t\t#[bar]\n",
      "omega = 0.08664;\n",
      "si = 0.4636;\n",
      "Tr = T/Tc;\n",
      "Pr = P/Pc;\n",
      "alpha_Tr = Tr**(-0.5);\t\t\t#a(Tr)\n",
      "#Using Eqn(3.50)\n",
      "Beta = omega*(Pr/Tr);\n",
      "#Using Eqn(3.51)\n",
      "q = si*alpha_Tr/(omega*(Tr**1.5));\n",
      "\n",
      "#using eqn(3.49)\n",
      "#Z = 1+beta-q*beta*((Z-beta)/((Z+(epsilon*beta))*(Z+(sigma*beta)))\n",
      "\n",
      "#calculation of Z\n",
      "Z = 1;\t\t\t#Initial\n",
      "a = Z;\n",
      "for i in range(11):\n",
      "    b = 1+Beta-(q*Beta*((a-Beta)/(a*(a+Beta))));\n",
      "    if((b-a) == 0.0001):\n",
      "        break;\n",
      "    a = b;\n",
      "    i = i+1;\n",
      "\n",
      "Z = round(b,3)\n",
      "\n",
      "#Umath.sing Eqn(6.64) and eqn(6.65)\n",
      "#(Hr/RT) = Z-1+[(d ln(alpha_Tr)/d ln Tr)-1]qI   I = ln((Z+beta)/Z)  d ln(alpha_Tr)/d ln Tr = -0.5\n",
      "#Sr/R) = ln(Z-beta)+[d ln(alpha_Tr)/d ln Tr]qI  I = ln((Z+beta)/Z)  d ln(alpha_Tr)/d ln Tr = -0.5\n",
      "I = math.log((Z+Beta)/Z);\n",
      "Hr = round(R*T*(Z-1+((-0.5-1)*q*I)),0);\n",
      "Sr = round(R*(math.log(Z-Beta)+(-0.5*q*I)),3);\n",
      "\n",
      "print ('Using Redlich/Kwong Equation')\n",
      "print 'Residual Enthalpy',Hr,'J/mol'\n",
      "print 'Residual Entropy',Sr,'J/mol/K'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Using Redlich/Kwong Equation\n",
        "Residual Enthalpy -4504.0 J/mol\n",
        "Residual Entropy -6.545 J/mol/K\n"
       ]
      }
     ],
     "prompt_number": 6
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.6  page no : 93"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "# Variables\n",
      "P1 = 1000.;\t\t\t#[KPa]\n",
      "T = 533.15;\t\t\t#[K]\n",
      "P2 = 200.;\t\t\t#[KPa]\n",
      "H1 = 2965.2;\t\t\t#[KJ/kg]  from Steam tables\n",
      "S1 = 6.9680;\t\t\t#[KJ/Kg/K] From steam tables\n",
      "S2 = S1;\n",
      "S_l = 1.5301;\t\t\t#[KJ/Kg/K]  Entropy Of Saturated Liquid @ 200KPa\n",
      "S_v = 7.1268;\t\t\t#[KJ/Kg/K]  Entropy Of Saturated vapor  @ 200KPa\n",
      "H_l = 504.7;\t\t\t#[KJ/Kg]     Enthalpy Of saturated liquid @ 200KPa\n",
      "H_v = 2706.7;\t\t\t#[KJ/Kg]    Enthalpy Of saturated vapor @ 200KPa\n",
      "\n",
      "# Calculations\n",
      "#find x_v from the eqn S = (1-x_v)S_l+x_c*S_v\n",
      "x_v = round((S1-S_l)/(S_v-S_l),4);\n",
      "\n",
      "#From Eqn(6.73a)\n",
      "H2 = ((1-x_v)*H_l)+(x_v*H_v);\n",
      "del_H = round(H2-H1,0);\t\t\t#[KJ/Kg]\n",
      "\n",
      "# Results\n",
      "print 'Percent vapor',x_v*100,'%'\n",
      "print 'Percent Liquid',(1-x_v)*100,'%'\n",
      "print 'Change In Enthalpy',del_H,'KJ/Kg'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Percent vapor 97.16 %\n",
        "Percent Liquid 2.84 %\n",
        "Change In Enthalpy -321.0 KJ/Kg\n"
       ]
      }
     ],
     "prompt_number": 7
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.7 page no : 96"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "import math \n",
      "from numpy import array,linalg\n",
      "\n",
      "# Variables(from steam tables)\n",
      "H = 293.;\t\t\t#[KJ/Kg]  at 343.15K\n",
      "H_liquid = 419.1;\t\t\t#[KJ/Kg]  at 373.15K\n",
      "H_vapor = 2676;\t\t\t#[KJ/Kg]    at 373.15K\n",
      "V_vapor = 1.5;\t\t\t#[m**3]\n",
      "m1_liquid = 500.;\t\t\t#[Kg]\n",
      "rho_liquid = 0.001044;\t\t\t#[m**3/Kg]\n",
      "rho_vapor = 1.673;\t\t\t#[m**3/Kg]\n",
      "del_m = 750.;\t\t\t#[Kg]\n",
      "\n",
      "# Calculations\n",
      "#using the eqn Q = (m2H2)math.tank-(m1H1)math.tank-(H*del_m)math.tank\n",
      "m1_vapor = (V_vapor-(m1_liquid*rho_liquid))/rho_vapor;\n",
      "#Term2 = ((m1H1)math.tank\n",
      "Term2 = (m1_liquid*H_liquid)+(m1_vapor*H_vapor);\n",
      "mT = m1_liquid+del_m+m1_vapor;\n",
      "#Solving Eqn By matrix Method\n",
      "#m_vapor+m_liquid = mT  and   (rho_vapor*m_vapor)+(rho_liquid*rho_vapor) = V_vapor\n",
      "A = array([[1,1],[rho_vapor,rho_liquid]]);\n",
      "B = array([mT,V_vapor]);\n",
      "X = linalg.solve(A,B);\n",
      "m2_vapor = X[0]\n",
      "m2_liquid = X[1]\n",
      "\n",
      "Term1 = (m2_liquid*H_liquid)+(m2_vapor*H_vapor);\n",
      "Q = round(Term1-Term2-del_m*H,0);\n",
      "\n",
      "print 'Heat Required',Q,'KJ'\n",
      "print ('Note: The Answer Varies With That of The Book because the calculations as \\\n",
      " in Book do not give the Answer the Book results')\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Heat Required 93518.0 KJ\n",
        "Note: The Answer Varies With That of The Book because the calculations as  in Book do not give the Answer the Book results\n"
       ]
      }
     ],
     "prompt_number": 10
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.8 page no : 98"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "import math \n",
      "from numpy import array,linalg\n",
      "\n",
      "\n",
      "def SRB(Tr,Pr,omega):\n",
      "    B0 = 0.083-(0.422/(Tr**1.6));\n",
      "    diffr_B0 = 0.675/(Tr**2.6);\t\t\t#dB0/dTr\n",
      "    B1 = 0.139-(0.172/(Tr**4.2));\n",
      "    diffr_B1 = 0.722/(Tr**5.2);\t\t\t#dB0/dTr\n",
      "    Q = -Pr*(diffr_B0+(omega*diffr_B1));\n",
      "    return Q\n",
      "\n",
      "def HRB(Tr,Pr,omega):\n",
      "    B0 = 0.083-(0.422/(Tr**1.6));\n",
      "    diffr_B0 = 0.675/(Tr**2.6);\t\t\t#dB0/dTr\n",
      "    B1 = 0.139-(0.172/(Tr**4.2));\n",
      "    diffr_B1 = 0.722/(Tr**5.2);\t\t\t#dB0/dTr\n",
      "    H = Pr*(B0-(Tr*diffr_B0)+(omega*(B1-(Tr*diffr_B1))));\n",
      "    return H\n",
      "\n",
      "def ICPS(T0,T,A,B,C,D):\n",
      "    t = T/T0;\n",
      "    return ((A)*math.log(t))+(((B*T0)+(((C*T0*T0)+(D/(t*t*T0*T0)))*(t+1)/2))*(t-1))\n",
      "\n",
      "def ICPH(T0,T,A,B,C,D):\n",
      "    t = T/T0;\n",
      "    return (A+((B/2)*T0*(t+1))+((C/3)*T0*T0*((t**2)+t+1))+(D/(t*T0*T0)))*(T-T0)\n",
      "\n",
      "# Variables(from steam tables)\n",
      "Tc = 420.;\t\t\t#[K]\n",
      "Pc = 40.43;\t\t\t#[bar]\n",
      "omega = 0.191;\n",
      "Tn = 266.9;\t\t\t#[K]\n",
      "A0 = 1.967;\n",
      "B0 = 31.630*10**-3;\n",
      "C0 = -9.837*10**-6;\n",
      "D0 = 0;\n",
      "T1 = 473.15;\t\t\t#[K]\n",
      "P = 70.;\t\t\t#[bar]\n",
      "R = 8.314;\n",
      "#From Table(E.3) And Table(E.4)\n",
      "Z0 = 0.485;\n",
      "Z1 = 0.142;\n",
      "\n",
      "Tr = T1/Tc;\n",
      "Pr = P/Pc;\n",
      "Z = Z0+(omega*Z1);\n",
      "V = round((Z*R*T1*10**-2)/P,4);\t\t\t#[m**3/Kmol]\n",
      "\n",
      "#step(a) vaporization at T1 and P1 = P_saturated\n",
      "#umath.sing eqn(6.70)  lnP_sat = A-(B/T)\n",
      "#Solving eqn ln(1.0133) = A-(B/266.9) and ln(40.43) = A-(B/420)\n",
      "a = array([[1,(-1/266.9)],[1,(-1./420)]])\n",
      "b = array([math.log(1.0133),math.log(40.43)]);\n",
      "x = linalg.solve(a,b)\n",
      "A = x[0]\n",
      "B = x[1]\n",
      "#umath.sing eqn(4.12)  del_Hn/RTn = 1.092*(ln Pc-1.013)/(0.930-Tr_n)\n",
      "Tr_n = Tn/Tc;\n",
      "del_Hn = R*Tn*(1.092*(math.log(Pc)-1.013)/(0.93-Tr_n));\t\t\t#[J/mol]\n",
      "T2 = 273.15;\t\t\t#[K]\n",
      "Tr = T2/Tc;\n",
      "#Umath.sing Eqn(4.13)  del_H/del_Hn = ((1-Tr)/(1-Tr_n))**0.38\n",
      "del_H_a = del_Hn*((1-Tr)/(1-Tr_n))**0.38;\n",
      "del_S_a = round(del_H_a/T2,2);\n",
      "\n",
      "#Step(b)transition to ideal gas State at(T1,P1)\n",
      "P_sat = math.exp(A-(B/273.15));\n",
      "Pr = P_sat/Pc;\n",
      "Tr = T2/Tc;\n",
      "Hr_b = round(R*Tc*HRB(Tr,Pr,omega),0)\t\t\t#[J/mol]\n",
      "Sr_b = round(R*SRB(Tr,Pr,omega),2)\t\t\t#[J/mol/K]\n",
      "\n",
      "#Step(c) Change to (T2,P2) in ideal-gas state\n",
      "\n",
      "H_c = round(R*ICPH(T2,T1,A0,B0,C0,D0),0);\t\t\t#[J/mol]\n",
      "S = R*ICPS(T2,T1,A0,B0,C0,D0);\t\t\t#[J/mol/K]\n",
      "del_S_c = round(S-(R*math.log(P/P_sat)),2);\t\t\t#[J/mol/K]\n",
      "\n",
      "#Step(d) Transition to actual final state at(T2,P2)\n",
      "#Umath.sing eqn(6.76) and eqn(6.77)\n",
      "#Hr/RTc = Hr0/RTc+(omega*Hr1/RTc)\n",
      "#Sr/R = Sr0/R+(omega*Sr1/R)  Sr0,Sr1 from Tables(E.5)\n",
      "Tr = T1/Tc;\n",
      "Pr = P/Pc;\n",
      "Hr_d = R*Tc*(-2.294+(omega*-0.713));\n",
      "Sr_d = R*(-1.566+(omega*-0.726));\n",
      "\n",
      "H = round(del_H_a-Hr_b+H_c+Hr_d,0);\n",
      "S = round(del_S_a-Sr_b+del_S_c+Sr_d,2);\n",
      "U = round(H-(P*V*10**2),0);\n",
      "\n",
      "print 'Volume(V) = ',V,'m**3/Kmol'\n",
      "print 'Internal energy(U) = ',U,'J/mol'\n",
      "print 'Enthalpy(H) = ',H,'J/mol'\n",
      "print 'Entropy(S) = ',S,'J/mol/K'\n",
      "\n",
      "print ('Note: The Answer here Slightly Varies with That of Book because of the different approximation')\n",
      "\n",
      "\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Volume(V) =  0.2878 m**3/Kmol\n",
        "Internal energy(U) =  32163.0 J/mol\n",
        "Enthalpy(H) =  34178.0 J/mol\n",
        "Entropy(S) =  88.55 J/mol/K\n",
        "Note: The Answer here Slightly Varies with That of Book because of the different approximation\n"
       ]
      }
     ],
     "prompt_number": 13
    },
    {
     "cell_type": "heading",
     "level": 2,
     "metadata": {},
     "source": [
      "Example 6.9 page no : 97"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "# Variables\n",
      "T = 450.;\t\t\t#[K]\n",
      "P = 140;\t\t\t#[bar]\n",
      "\n",
      "#pseudo parameters\n",
      "Tc1 = 304.2;\t\t\t#[K]\n",
      "Tc2 = 369.8;\t\t\t#[K]\n",
      "Pc1 = 73.83;\t\t\t#[bar]\n",
      "Pc2 = 42.48;\t\t\t#[bar]\n",
      "Tpc = (0.5*Tc1)+(0.5*Tc2);\n",
      "Ppc = (0.5*Pc1)+(0.5*Pc2);\n",
      "\n",
      "# Calculations\n",
      "Tpr = T/Tpc;\n",
      "Ppr = P/Ppc;\n",
      "\n",
      "Z0 = 0.697;\n",
      "Z1 = 0.205;\n",
      "\n",
      "omega1 = 0.224;\n",
      "omega2 = 0.152;\n",
      "omega = (0.5*omega1)+(0.5*omega2);\n",
      "\n",
      "Z = Z0+(omega*Z1);\n",
      "\n",
      "V = round(Z*R*T*10/P,1);\t\t\t#[cm**3/mol]\n",
      "\n",
      "#(H/RT)0 = -1.73 (H/RT)1 = -0.169\n",
      "H = round(R*Tpc*(-1.73+(omega*-0.169)),0);\t\t\t#[J/mol]\n",
      "S = round(R*(-0.967+(omega*-0.330)),2);\t\t\t#[J/mol/K]\n",
      "\n",
      "# Results\n",
      "print 'Volume(V) = ',V,'cm**3/mol'\n",
      "print 'Residual Enthaply(H) = ',H,'J/mol'\n",
      "print 'Residual Entropy(S) = ',S,'J/mol/K'\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "Volume(V) =  196.6 cm**3/mol\n",
        "Residual Enthaply(H) =  -4936.0 J/mol\n",
        "Residual Entropy(S) =  -8.56 J/mol/K\n"
       ]
      }
     ],
     "prompt_number": 14
    }
   ],
   "metadata": {}
  }
 ]
}