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+ "metadata": {
+ "name": "",
+ "signature": "sha256:49c580cddfa6fee61cb89005e8162fda0d32dc5e946341e173242a32280cb578"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+ {
+ "cells": [
+ {
+ "cell_type": "heading",
+ "level": 1,
+ "metadata": {},
+ "source": [
+ "Chapter 1: Introduction to Engineering Principles and Units"
+ ]
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.3-1, Page number 6"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Finding mole mass or weight fraction of solution \n",
+ "\n",
+ "#Variable declaration\n",
+ "mNaOH = 50. #Mass of NaOH in solution in gram\n",
+ "mH2O = 50. #Mass of H2O in solution in gram\n",
+ "MWNaOH = 40 #Molecular weight of NaOH\n",
+ "MWH2O = 18.02 #Molecular weight of H2O\n",
+ "masstolbm = 1/453.6 #Conversion factor for Mass to Lb mass\n",
+ "\n",
+ "#Calculation\n",
+ "mT = mNaOH + mH2O #Total mass of solution\n",
+ "mfNaOH = mNaOH/mT #mfNaOH mass fraction of NaOH \n",
+ "mfH2O = mH2O/mT #mfNaOH mass fraction of H2O\n",
+ "nNaOH = mNaOH/MWNaOH #Number of moles of NaOH\n",
+ "nH2O = mH2O/MWH2O #Number of moles of H2O\n",
+ "nT = nNaOH + nH2O #Total number of moles in solution\n",
+ "xNaOH = nNaOH/nT #xNaOH mole fraction of NaOH\n",
+ "xH2O = nH2O/nT #xH2O mole fraction of H2O\n",
+ "lbmNaOH = mNaOH*masstolbm \n",
+ "lbmH2O = mH2O*masstolbm\n",
+ "\n",
+ "#Result\n",
+ "print \"Mass fraction of NaOH\", mfNaOH\n",
+ "print \"Mass fraction of H2O\", mfH2O \n",
+ "print \"Mole fraction of NaOH\", round(xNaOH,3) \n",
+ "print \"Mole fraction of H2O\", round(xH2O,3)\n",
+ "print \"Mass of NaOH in Lb mass\",round(lbmNaOH,4), \"lbm\"\n",
+ "print \"Mass of H2O in Lb mass\", round(lbmH2O,4), \"lbm\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Mass fraction of NaOH 0.5\n",
+ "Mass fraction of H2O 0.5\n",
+ "Mole fraction of NaOH 0.311\n",
+ "Mole fraction of H2O 0.689\n",
+ "Mass of NaOH in Lb mass 0.1102 lbm\n",
+ "Mass of H2O in Lb mass 0.1102 lbm\n"
+ ]
+ }
+ ],
+ "prompt_number": 17
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.4-1, Page number 8"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Calculate the value of gas law constant\n",
+ "\n",
+ "#Variable declaration \n",
+ "P = 14.7 #Pressure (psia)\n",
+ "V = 359. #Volume of gas(ft3)\n",
+ "Tf = 32 #Temperature in (degF)\n",
+ "n = 1. #Number of moles of Ideal Gas (lbmol)\n",
+ "\n",
+ "#Calculation\n",
+ "Tr = 460 + Tf #Deg F to deg Rankine conversion\n",
+ "R = P*V/(n*Tr) #R Gas constant in ft3.psia/(lbmol.degR)\n",
+ "\n",
+ "#Result\n",
+ "print 'Gas law constant in lbmole, ft3, \u00b0R, and psia units %5.2f ft3.psia/(lbmol.degR)'%(R)\n",
+ "\n",
+ "#Variable declarationSI units\n",
+ "P = 101325 #Pressure (Pa)\n",
+ "V = 22.414 #Volume of gas(m3)\n",
+ "T = 0 #Temperature in (deg C)\n",
+ "n = 1. #Number of moles of Ideal Gas (kgmol)\n",
+ "\n",
+ "#Calculation\n",
+ "TK = 273.15 + T #Deg C to Kelvin conversion\n",
+ "R = P*V/(n*TK) #R Gas constant in m3.pa/(kgmol.K)\n",
+ "\n",
+ "#Result\n",
+ "print 'Gas law constant in kgmole, m3, K, and pa units %5.2f m3.pa/(kgmol.K)'%(R)"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Gas law constant in lbmole, ft3, \u00b0R, and psia units 10.73 ft3.psia/(lbmol.degR)\n",
+ "Gas law constant in kgmole, m3, K, and pa units 8314.47 m3.pa/(kgmol.K)\n"
+ ]
+ }
+ ],
+ "prompt_number": 18
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.4-2, Page number 9"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Composition of Gas\n",
+ "\n",
+ "#Variable declaration\n",
+ "pCO2 = 75. #Partial pressure of CO2 (mmHg)\n",
+ "pCO = 50. #Partial pressure of CO (mmHg)\n",
+ "pN2 = 595. #Partial pressure of N2 (mmHg) \n",
+ "pO2 = 26. #Partial pressure of O2 (mmHg)\n",
+ "\n",
+ "#Calculation\n",
+ "#Total pressure by Dalton's law\n",
+ "P = pCO2 + pCO + pN2 + pO2\n",
+ "xCO2 = pCO2/P\n",
+ "xCO = pCO/P\n",
+ "xN2 = pN2/P\n",
+ "xO2 = pO2/P\n",
+ "\n",
+ "\n",
+ "#Result\n",
+ "print \"Total Pressure P\",P, \"mmHg\"\n",
+ "print \"mole fraction of CO2\", round(xCO2,3)\n",
+ "print \"mole fraction of CO\", round(xCO,3)\n",
+ "print \"mole fraction of N2\", round(xN2,3)\n",
+ "print \"mole fraction of O2\", round(xO2,3)"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Total Pressure P 746.0 mmHg\n",
+ "mole fraction of CO2 0.101\n",
+ "mole fraction of CO 0.067\n",
+ "mole fraction of N2 0.798\n",
+ "mole fraction of O2 0.035\n"
+ ]
+ }
+ ],
+ "prompt_number": 19
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.5-1, Page number 10"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Concentration of Orange Juice using evaporator\n",
+ "\n",
+ "#Variable declaration\n",
+ "F = 1000. #Feed rate of orange juice to evaporator (kg/hr)\n",
+ "MpSi = 7.08 #Mass percent of solids in incomming juice\n",
+ "MpSo = 58. #Mass percent of solids in concentrated juice\n",
+ "xW = 0.0\n",
+ "#Calculation\n",
+ " #Overall Mass Balance\"\n",
+ " #$F = W + C$\"\n",
+ " #Component Mass Balance on solids\"\n",
+ " #$F.xF = W.xW + C.xC$\n",
+ "\n",
+ "C = F*MpSi/(100)/(MpSo/100)\n",
+ "#Using overall Balance equation\n",
+ "W = 1000-C\n",
+ "\n",
+ "#Results\n",
+ "print \"Flow rate of Concentrated juice stream\", round(C,1) ,\"kg/hr\"\n",
+ "print \"Flow rate of evaporated water stream\", round(W,1) ,\"kg/hr\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Flow rate of Concentrated juice stream 122.1 kg/hr\n",
+ "Flow rate of evaporated water stream 877.9 kg/hr\n"
+ ]
+ }
+ ],
+ "prompt_number": 20
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.5-2, Page number 11"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Crystallization of KNO3 and Recycle\n",
+ "\n",
+ "#Variable declaration\n",
+ "\n",
+ "F = 1000. #F: Feed to the process, kg/hr\n",
+ "xW = 0. #xW: Weight % of KNO3 in water vaopor stream\n",
+ "xF = 20. #xF: Weight % of KNO3 in Feed\n",
+ "xP = 96. #xP: Weight % of KNO3 in product stream\n",
+ "xR = 37.5 #xR: Weight % of KNO3 in Recycle\n",
+ "xS = 50. #xS: Weight % of KNO3 in stream from evaporator to crystallizer\n",
+ "#Calculation\n",
+ " #Overall material Balance\n",
+ " # F = W + P\n",
+ " # Component material balance on KNO3\n",
+ " # F.xF = W.xW + P.xP\n",
+ " # Solving for P\n",
+ "P = (F*xF/100)/(xP/100) #P: Product rate from process, kg/hr\n",
+ " #Balance over crystallizer\n",
+ " # S = R + P --> P = S - R\n",
+ " #Component balance over crystallizer\n",
+ " # S.xS = R.xR + P.xP --> (R + P).xS = R.xR + P.xP --> ((R + P).xS - P.xP )/xR = \n",
+ "R = P*(xP-xS)/(xS-xR) #R: REcycle rate, kg/hr\n",
+ "S = R + P #S: Concentrate rate from evaporator to crystallizer, kg/hr\n",
+ "\n",
+ "#Result\n",
+ "print \"Product rate from the process is\",round(P,1), \"kg/hr\"\n",
+ "print \"Recycle rate from the process is\",round(R,1), \"kg/hr\"\n",
+ "print \"Stream leaving evaporator \",round(S,1), \"kg/hr\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Product rate from the process is 208.3 kg/hr\n",
+ "Recycle rate from the process is 766.7 kg/hr\n",
+ "Stream leaving evaporator 975.0 kg/hr\n"
+ ]
+ }
+ ],
+ "prompt_number": 21
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.5-3, Page number 12"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Combustion of fuel gas\n",
+ "\n",
+ "#Variable declaration\n",
+ " #Basis 100 kg mol of feed, moles = mole%x100/100\n",
+ "H2=3.1 #Moles of H2 in feed\n",
+ "CO=27.2 #moles of CO in feed\n",
+ "CO2=5.6 #Moles of CO2 in feed\n",
+ "O2=0.5 #Moles of O2 in feed\n",
+ "N2=63.6 #Moles of N2 in feed\n",
+ " #98% CO reacts to form CO2\n",
+ "\n",
+ "#Calculation\n",
+ " #CO + (0.5)O2 ----> CO2\n",
+ " #H2 +(0.5)O2 ----> H2O\n",
+ " #Accounting the total number of moles of O2 in the fuel gas theoretically\n",
+ "\n",
+ "MthO2=(0.5)*CO + 0.5*H2 - O2 #theoretically required O2 moles\n",
+ "\n",
+ " #For 20% excess moles required \n",
+ "MactO2=(1.2)*MthO2 #Actual moles of O2 required \n",
+ "\n",
+ " #Since air contains 79 mol% of N2\n",
+ "MN2=(79./21)*MactO2 #moles of N2 in air\n",
+ " #2% CO does not react\n",
+ "MTN2 = MN2 + N2\n",
+ "MO2in = O2 + MactO2\n",
+ "#Mflueg = moles of water + unreacted CO + CO2 (from reacted CO and CO2 in feed ) + N2 + O2 \n",
+ "MH2Oflueg = H2\n",
+ "MN2flueg = MTN2\n",
+ "MCOflueg = 0.02*CO\n",
+ "MCO2flueg = CO2 + 0.98*CO\n",
+ "MO2flueg = MO2in - (0.5*H2 + 0.98*CO/2 )\n",
+ "\n",
+ "Mflueg = MH2Oflueg + 0.02*CO + CO2 + 0.98*CO + MTN2 + (MO2in - (0.5*H2 + 0.98*CO/2 ))\n",
+ "\n",
+ "\n",
+ "#Result\n",
+ "print \"Moles of CO in exit flue\",round(MCOflueg,2),\"mol\"\n",
+ "print \"Moles of CO2 in exit flue\",round(MCO2flueg,2),\"mol\"\n",
+ "print \"Moles of O2 in exit flue\",round(MO2flueg,2),\"mol\"\n",
+ "print \"Moles of N2 in exit flue\",round(MTN2,1),\"mol\"\n",
+ "print \"Moles of H2O in exit flue\",round(MH2Oflueg,2),\"mol\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Moles of CO in exit flue 0.54 mol\n",
+ "Moles of CO2 in exit flue 32.26 mol\n",
+ "Moles of O2 in exit flue 3.2 mol\n",
+ "Moles of N2 in exit flue 129.7 mol\n",
+ "Moles of H2O in exit flue 3.1 mol\n"
+ ]
+ }
+ ],
+ "prompt_number": 22
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.6-1, Page number 14"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Heating of N2 Gas\n",
+ "\n",
+ "#Variable declaration\n",
+ "\n",
+ "M=3. #Moles of N2\n",
+ "T1=298. #Temperature of N2 gas (K)\n",
+ "T2=673. #Temperature of N2 gas (K)\n",
+ "T3=1123. #Temperature of N2 gas (K)\n",
+ "\n",
+ "# Data\n",
+ "Cpm1=29.68 #Mean heat capacity of N2 gas ranging 298K-673K (J/gmol.k)\n",
+ "Cpm2=31.00 #Mean heat capacity of N2 gas ranging 298K-1123K (J/gmol.k)\n",
+ "\n",
+ "#Calculation\n",
+ "#Heat required (Hi)=M*Cpmi*(del T)\n",
+ "H1 = M*Cpm1*(T2-T1) #Heat required in (J)\n",
+ "H2 = M*Cpm2*(T3-T1) #Heat required in (J)\n",
+ "H3 = H2-H1 #Heat required in (J) Since there is no mean heat capacity for the interval 673K-1123K\n",
+ "\n",
+ "#Result\n",
+ "print \"(a) Heat required to raise the temperature from 298K-673K\",H1,\"J\"\n",
+ "print \"(b) Heat required to raise the temperature from 298K-1123K\",H2,\"J\"\n",
+ "print \"(c) Heat required to raise the temperature from 673K-1123K\",H3,\"J\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "(a) Heat required to raise the temperature from 298K-673K 33390.0 J\n",
+ "(b) Heat required to raise the temperature from 298K-1123K 76725.0 J\n",
+ "(c) Heat required to raise the temperature from 673K-1123K 43335.0 J\n"
+ ]
+ }
+ ],
+ "prompt_number": 23
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.6-2, Page number 16"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Heating of Milk\n",
+ "\n",
+ "#Variable declaration\n",
+ "\n",
+ "mdot = 4536. #Mass rate of kg/hr\n",
+ "Ti = 4.4 #Temeprature of incomming milk, deg C\n",
+ "To = 54.4 #Temperature of milk leaving exhanger, deg C\n",
+ "C = 3.85 #Heat capacity of cow milk, kJ/(kg.K)\n",
+ "#Data\n",
+ "\n",
+ "#Calculation\n",
+ "Mdot = mdot/3600 #Mass rate of kg/s\n",
+ "delT = To - Ti #delT: Temperature difference between milk temperature at outlet and inlet \n",
+ "Q = Mdot*C*delT #Q: Heat required, kW\n",
+ "#Result\n",
+ "print \"Rate of Heat Addition: \",Q, \"kJ/s or kW\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Rate of Heat Addition: 242.55 kJ/s or kW\n"
+ ]
+ }
+ ],
+ "prompt_number": 24
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.6-3, Page number 17"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Use of Steam Table\n",
+ "\n",
+ "#Variable declaration\n",
+ "\n",
+ "m = 1 # mass of water in kg or lbm\n",
+ "\n",
+ "#Part A SI Units\n",
+ "# Data\n",
+ "H21_11 = 88.60 # Enathalpy at 21.11 degC, kJ/kg\n",
+ "H60 = 251.13 # Enathalpy at 60 degC, kJ/kg \n",
+ "#Calculation\n",
+ "\n",
+ "delH = H60 - H21_11\n",
+ "\n",
+ "#Result\n",
+ "print \"Enthalpy change for heating 1kg of steam\", delH, \"kJ/kg\"\n",
+ "\n",
+ "#Part A British Units\n",
+ "# Data\n",
+ "H70 = 38.09 # Enathalpy at 70 degF, btu/lbm\n",
+ "H140 = 107.96 # Enathalpy at 140 degF, btu/lbm\n",
+ "\n",
+ "#Calculation\n",
+ "\n",
+ "delH = H140 - H70\n",
+ "\n",
+ "#Result\n",
+ "print \"Enthalpy change for heating 1 lbm of steam\", delH, \"Btu/lbm\"\n",
+ "\n",
+ "#Part B SI Units\n",
+ "# Data\n",
+ "H21_11 = 88.60 # Enathalpy at 21.11 degC, kJ/kg\n",
+ "H115_6 = 2699.9 # Enathalpy at 115.6 degC, kJ/kg at 172.2 kPa\n",
+ "\n",
+ "#Calculation\n",
+ "delH = H115_6 - H21_11\n",
+ "\n",
+ "#Result\n",
+ "print \"Enthalpy change for heating 1kg of steam\", delH, \"kJ/kg\"\n",
+ "\n",
+ "#Part B British Units\n",
+ "# Data\n",
+ "H70 = 38.09 # Enathalpy at 70 degF, btu/lbm\n",
+ "H240 = 1160.7 # Enathalpy at 140 degF, btu/lbm at 24.97 psia\n",
+ "\n",
+ "#Calculation\n",
+ "delH = H240 - H70\n",
+ "\n",
+ "#Result\n",
+ "print \"Enthalpy change for heating 1 lbm of steam\", delH, \"Btu/lbm\"\n",
+ "\n",
+ "#Part C SI Units\n",
+ "# Data\n",
+ "Hv_115_6 = 2699.9 # Enathalpy at 115.6 degC, kJ/kg at 172.2 kPa\n",
+ "Hl_115_6 = 484.9 # Enathalpy at 115.6 degC, kJ/kg at 172.2 kPa\n",
+ "\n",
+ "#Calculation\n",
+ "LambdaV = Hv_115_6 - Hl_115_6\n",
+ "\n",
+ "#Result\n",
+ "print \"Enthalpy of vaporization 1 kg of steam\", LambdaV, \"kJ/kg\"\n",
+ "\n",
+ "#Part C British Units\n",
+ "# Data\n",
+ "Hv_115_6 = 1160.7 #Enathalpy water vapor at 240 degF, Btu/lbm at 24.97 psia\n",
+ "Hl_115_6 = 208.44 #Enathalpy saturated water at 240 degF, Btu/lbm at 24.97 psia\n",
+ "\n",
+ "#Calculation\n",
+ "LambdaV = Hv_115_6 - Hl_115_6\n",
+ "#Result\n",
+ "print \"Enthalpy of vaporization 1 kg of steam\", LambdaV, \"Btu/lbm\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Enthalpy change for heating 1kg of steam 162.53 kJ/kg\n",
+ "Enthalpy change for heating 1 lbm of steam 69.87 Btu/lbm\n",
+ "Enthalpy change for heating 1kg of steam 2611.3 kJ/kg\n",
+ "Enthalpy change for heating 1 lbm of steam 1122.61 Btu/lbm\n",
+ "Enthalpy of vaporization 1 kg of steam 2215.0 kJ/kg\n",
+ "Enthalpy of vaporization 1 kg of steam 952.26 Btu/lbm\n"
+ ]
+ }
+ ],
+ "prompt_number": 25
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.6-4, Page number 18"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Combustion of Carbon\n",
+ "\n",
+ "#Variable declaration\n",
+ "n = 10. # gmol of Carbon \n",
+ "nCO2 = 90. #Percent of Carbon converted to CO2\n",
+ "nCO = 10. #Percent of Carbon converted to CO\n",
+ "DelHcCO2 = -393513 # Standard enthalpy change of combustion for CO2 in kJ/kmol\n",
+ "DelHcCO = -110523 # Standard enthalpy change of combustion for CO2 in kJ/kmol\n",
+ " \n",
+ "#Calculation\n",
+ "n1 = n/1000\n",
+ "delHc = n1*nCO2*DelHcCO2/100 + n1*nCO*DelHcCO/100\n",
+ "\n",
+ "#Result\n",
+ "print \" Entahlpy change on incomplete combustion of Carbon:\", round(delHc), \"kJ\"\n",
+ "\n",
+ "#Data kcal Units \n",
+ "DelHcCO2 = -94.0518 # Standard enthalpy change of combustion for CO2 in kcal/gmol\n",
+ "DelHcCO = -26.4157 # Standard enthalpy change of combustion for CO2 in kcal/gmol\n",
+ "\n",
+ "#Calculation\n",
+ "delHc = n*nCO2*DelHcCO2/100 + n*nCO*DelHcCO/100\n",
+ "\n",
+ "#Result\n",
+ "print \" Entahlpy change on incomplete combustion of Carbon:\", round(delHc), \"kcal\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ " Entahlpy change on incomplete combustion of Carbon: -3652.0 kJ\n",
+ " Entahlpy change on incomplete combustion of Carbon: -873.0 kcal\n"
+ ]
+ }
+ ],
+ "prompt_number": 26
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.6-5, Page number 18"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Reaction of Methane\n",
+ "\n",
+ "#Variable declaration\n",
+ "molCH4=1. #MOles of CH4 (kg)\n",
+ "press=101.32 #Pressure (kPa)\n",
+ "temp=298. #temperature (K)\n",
+ "delHfCH4=-74848. #Heat of Formation of CH4 (kJ/kg mol)\n",
+ "delHfH2O=-285840. #Heat of Formation of H2O (kJ/kg mol)\n",
+ "delHfCO=-110523. #Heat of Formation of CO (kJ/kg mol)\n",
+ "delHfH2=0 #Heat of Formation of H2 (kJ/kg mol)\n",
+ "\n",
+ "#Calculation\n",
+ " #delH= delHf(products)-delHf(reactants) \n",
+ "\n",
+ "delH= (delHfCO + 3*delHfH2) - (delHfCH4 + delHfH2O)\n",
+ "\n",
+ "#Result\n",
+ "print 'The standard heat of Formation %5.2e'%(delH),\"kJ/kg mol (Endothermic)\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The standard heat of Formation 2.50e+05 kJ/kg mol (Endothermic)\n"
+ ]
+ }
+ ],
+ "prompt_number": 27
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.7-1, Page number 19"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Heating of Fermentation Medium\n",
+ "\n",
+ "#Variable declaration SI Units \n",
+ "\n",
+ "F=2000. #Feed rate of Liquid (kg/h)\n",
+ "TLi=30. #Initial temperature of the liquid (\u00b0C)\n",
+ "TLo=70. #Final temperature of the liquid (\u00b0C)\n",
+ "TWi=95. #Temperature of water while entering (\u00b0C)\n",
+ "TWo=85. #Temperature of water while leaving (\u00b0C)\n",
+ "Tref=25. #Reference temperature (\u00b0C)\n",
+ "CL=4.06 #Enthalpy of liquid at 25 degC (kJ/kg)\n",
+ "Cw=4.21 #Enthalpy of water at 25 degC (kJ/kg)\n",
+ "\n",
+ "#Calculations \n",
+ "\n",
+ "delTLi=TLi-Tref\n",
+ "delTLo=TLo-Tref\n",
+ "delTW=TWi-Tref\n",
+ " #Input streams\n",
+ "HLi=F*CL*delTLi\n",
+ " #Output streams\n",
+ "HLo=F*CL*delTLo \n",
+ " #Heat gained by the system = Heat gained at outlet - heat at inlet\n",
+ "QL = HLo-HLi\n",
+ " #Heat gained by liquid = Heat lost by water \n",
+ "W = QL/(Cw*(TWi-TWo))\n",
+ "\n",
+ "#Result\n",
+ "print 'Rate Enthalpy of the liquid entering %5.2e kJ/kg'%HLi\n",
+ "print 'Rate Enthalpy of the liquid leaving %5.2e kJ/kg'%HLo\n",
+ "print 'Heat added to fermentation medium %5.4e'%(QL),\"kJ/h\"\n",
+ "print \"Feed rate of water supplied\",round(W,2),\"kg/h\"\n",
+ "print 'The answer has been checked using calculator and \\ndiffers from answer given in book because of truncation'\n",
+ "print \"Heat added to fermentation medium:\",round(QL/3600,2),\"kW\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Rate Enthalpy of the liquid entering 4.06e+04 kJ/kg\n",
+ "Rate Enthalpy of the liquid leaving 3.65e+05 kJ/kg\n",
+ "Heat added to fermentation medium 3.2480e+05 kJ/h\n",
+ "Feed rate of water supplied 7714.96 kg/h\n",
+ "The answer has been checked using calculator and \n",
+ "differs from answer given in book because of truncation\n",
+ "Heat added to fermentation medium: 90.22 kW\n"
+ ]
+ }
+ ],
+ "prompt_number": 28
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.7-2, Page number 21"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Heat and Material Balance in Combustion\n",
+ "\n",
+ "#Variable declaration SI Units \n",
+ "mCO = 1. #Moles of CO burnt in furnace (kmol/h)\n",
+ "delHc=-282989. #Standard heat of combustion of CO (kJ/kmol)\n",
+ "CpmCO = 29.38 #Mean Heat capacity of CO between temperature 298k-478k\n",
+ "CpmCO2 = 49.91 #Mean Heat capacity of CO2 between temperature 298k-478k\n",
+ "CpmN2 = 31.43 #Mean Heat capacity of N2 between temperature 298k-478k\n",
+ "CpmO2 = 33.25 #Mean Heat capacity of O2 between temperature 298k-478k\n",
+ "Cpmair = 29.29 #Mean Heat capacity of Air between temperature 298k-478k\n",
+ "Tref = 298. #Reference temperature for enthalpy calculation\n",
+ "TCOi = 473. #Temperature of CO inlet stream \n",
+ "Tair = 373. #Temperature of inlet air stream\n",
+ "Texit = 1273. #Temperature of outgoing stream\n",
+ "\n",
+ "#Calculation\n",
+ " #CO(g) + (0.5)O2(g) ---> CO2(g)\n",
+ " #Since from the above equation we get that 1 mole of CO will require 0.5 mole O2\n",
+ "MthO2 = (0.5)*1. #Theoretically required O2 moles (kmol/h)\n",
+ "MactO2 = (1.9)*(MthO2) #Moles of O2 actually added\n",
+ "MN2 = (0.79/0.21)*MactO2 #Moles of N2 added\n",
+ "xO2 = MactO2 - MthO2 #Moles of O2 in exit flue\n",
+ "xCO2 = mCO #Moles of CO2 formed is equal to moles of CO added\n",
+ "xN2 = MN2 #Moles of N2 in the exit flue\n",
+ "MAir = xN2 + MactO2\n",
+ "\n",
+ " #Input streams \n",
+ "HinAir = MAir*Cpmair*(Tair-Tref)\n",
+ "HinCO = mCO*CpmCO*(TCOi-Tref)\n",
+ "HCO2 = xCO2*CpmCO2*(Texit-Tref)\n",
+ "HN2 = xN2*CpmN2*(Texit-Tref)\n",
+ "HO2 = xO2*CpmO2*(Texit-Tref)\n",
+ "Qr = mCO*delHc #Heat removed = total enthalpy of leaving streams - total enthalpy of incoming streams + heat added due to reaction\n",
+ "q = HCO2 + HO2 + HN2 - (HinAir + HinCO-Qr)\n",
+ "\n",
+ "#Result\n",
+ "print 'moles of O2 actually added %4.3f kgmol/h'%MactO2\n",
+ "print 'moles of N2 added %4.3f kgmol/h, Notice this value differs from \\nthan in book hence following values also change but are correct'%xN2\n",
+ "print 'moles of air added %4.3f kgmol/h'%(MactO2+MN2)\n",
+ "print 'moles of O2 in exit flue gas %4.3f kgmol/h'%xO2\n",
+ "print 'Enthalpy of air entering %4.3f kJ/h'%HinAir\n",
+ "print 'Enthalpy of CO entering %4.3f kJ/h'%HinCO\n",
+ "print 'Enthalpy of CO2 leaving %4.3f kJ/h'%HCO2\n",
+ "print 'Enthalpy of N2 leaving %4.3f kJ/h'%HN2\n",
+ "print 'Enthalpy of O2 leaving %4.3f kJ/h'%HO2\n",
+ "print \"Heat Removed: \", round(q), \"kJ/hr\"\n",
+ "print \"Heat Removed: \", round(q*1000./3600.),\"W\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "moles of O2 actually added 0.950 kgmol/h\n",
+ "moles of N2 added 3.574 kgmol/h, Notice this value differs from \n",
+ "than in book hence following values also change but are correct\n",
+ "moles of air added 4.524 kgmol/h\n",
+ "moles of O2 in exit flue gas 0.450 kgmol/h\n",
+ "Enthalpy of air entering 9937.679 kJ/h\n",
+ "Enthalpy of CO entering 5141.500 kJ/h\n",
+ "Enthalpy of CO2 leaving 48662.250 kJ/h\n",
+ "Enthalpy of N2 leaving 109516.713 kJ/h\n",
+ "Enthalpy of O2 leaving 14588.437 kJ/h\n",
+ "Heat Removed: -125301.0 kJ/hr\n",
+ "Heat Removed: -34806.0 W\n"
+ ]
+ }
+ ],
+ "prompt_number": 29
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 1.7-3, Page number 22"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Oxidation of LactoseC12H22O11\n",
+ "\n",
+ "#Variable declaration\n",
+ " #HLact37, Total Enthalpy of Lactose stream in at 37 deg C \n",
+ " #HO237, Total Enthalpy of Oxygen stream in at 37 deg C \n",
+ " #HH2O37, Total Enthalpy of Water out at 37 deg C \n",
+ " #HCO237, Total Enthalpy of CO2 stream out at 37 deg C \n",
+ " #delHcLact37, Heat of combustion for Lactose, J/mol\n",
+ "\n",
+ "\n",
+ "nLact = 1. #Mass of Lactose in gmol\n",
+ "nO2 = 12. #Moles oo O2 fed\n",
+ "nCO2 = 12. #Moles oo CO2 \n",
+ "nH2O = 11. #Moles oo H2O \n",
+ "MWLact = 342.3 #Molecular weight of lactose\n",
+ "MWH2O = 18.02 #Molecular weight of water\n",
+ "CpmLact = 1.2 #Mean specific heat of Lactose, J/g.K\n",
+ "CpmO2 = 29.38 #Mean specific heat of O2, J/mol.K\n",
+ "CpmH2O = 4.18 #Mean specific heat of H2O, J/mol.K\n",
+ "CpmCO2 = 37.45 #Mean specific heat of CO2, J/mol.K\n",
+ "delHcLact = 5648.8e3 #Std. Heat of combustion for Lactose, J/mol\n",
+ "Tref = 25. #Reference temperature, deg C\n",
+ "Ts = 37. #Stream temperature, deg C\n",
+ "\n",
+ "\n",
+ "#Calculation\n",
+ " #H = n*Cpmi*(T-Tref)\n",
+ " #Del T in degC = Del T in K\n",
+ "mLact = nLact*MWLact\n",
+ "HLact37 = mLact*CpmLact*(Ts-Tref)\n",
+ "HO237 = nO2*CpmO2*(Ts-Tref)\n",
+ "HCO237 = nCO2*CpmCO2*(Ts-Tref)\n",
+ "HH2O37 = nH2O*MWH2O*CpmH2O*(Ts-Tref)\n",
+ "delHcLact37 = HCO237 + HH2O37 - (HLact37 + HO237 + delHcLact)\n",
+ "\n",
+ "#Result\n",
+ "\n",
+ "print \"Enthalpy of Lactose stream in at 37 deg C:\",round(HLact37),\"J/gmol\"\n",
+ "print \"Enthalpy of Oxygen stream in at 37 deg C :\",round(HO237), \"J/gmol\" \n",
+ "print \"Enthalpy of Water out at 37 deg C :\",round(HH2O37), \"J/gmol\" \n",
+ "print \"Enthalpy of CO2 stream out at 37 deg C :\",round(HCO237), \"J/gmol\"\n",
+ "print \"Heat of combustion for Lactose :\",round(HLact37),\"J/gmol\"\n",
+ "print 'Heat of combustion of Lactose at 37 deg C:%6.3e'%(delHcLact37),\"J/gmol\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Enthalpy of Lactose stream in at 37 deg C: 4929.0 J/gmol\n",
+ "Enthalpy of Oxygen stream in at 37 deg C : 4231.0 J/gmol\n",
+ "Enthalpy of Water out at 37 deg C : 9943.0 J/gmol\n",
+ "Enthalpy of CO2 stream out at 37 deg C : 5393.0 J/gmol\n",
+ "Heat of combustion for Lactose : 4929.0 J/gmol\n",
+ "Heat of combustion of Lactose at 37 deg C:-5.643e+06 J/gmol\n"
+ ]
+ }
+ ],
+ "prompt_number": 30
+ }
+ ],
+ "metadata": {}
+ }
+ ]
+}
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