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diff --git a/TRANSPORT_PROCESSES_AND_UNIT_OPERATIONS/GeankoplisChapter08.ipynb b/TRANSPORT_PROCESSES_AND_UNIT_OPERATIONS/GeankoplisChapter08.ipynb new file mode 100755 index 00000000..8a328185 --- /dev/null +++ b/TRANSPORT_PROCESSES_AND_UNIT_OPERATIONS/GeankoplisChapter08.ipynb @@ -0,0 +1,390 @@ +{
+ "metadata": {
+ "name": "",
+ "signature": "sha256:fc87d6d9b6be61c481eaede8b73c8cf240680807ed293ac553e78b065098e01d"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+ {
+ "cells": [
+ {
+ "cell_type": "heading",
+ "level": 1,
+ "metadata": {},
+ "source": [
+ "Chapter 8: Evaporation"
+ ]
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 8.4-1, Page number 498"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Heat Transfer Area in a Single-Effect Evaporator\n",
+ "\n",
+ "#Variable declaration\n",
+ "F = 9072. #Feed rate to the evaporator, kg/hr\n",
+ "xF = 1. #weight percent of salt, kg/kg\n",
+ "TF = 311.0 #Temperature of feed, K\n",
+ "xL = 1.5 #Weight percentage of concentrated product, kg/kg \n",
+ "P = 101.325 #Pressure of vapor space, kPa\n",
+ "Ps = 143.3 #Pressure of saturated steam used for heating, kPa\n",
+ "U = 1704. #Overall heat transfer coefficient, W/m2K\n",
+ "cpF = 4.140 #Specific heat of Feed to the evaporator, kJ/(kg.K)\n",
+ "Hv373 = 2257. #Latent heat of evaporation of water at 373.2 K\n",
+ "Hv143 = 2230. #Latent heat of evaporation of saturated water at 143.3 kPa\n",
+ "Ts = 383.2 #Temperature of Saturated steam at 143.3 kPa\n",
+ "TL = 373.2 #Temperature of concentrated Liquid enthalpy calculation, K\n",
+ "Tref = 373.2 #Reference temperature for enthalpy calculation, K\n",
+ "\n",
+ "#Calculation \n",
+ "L = F*xF/xL\n",
+ "V = F-L\n",
+ " #Energy Balance\n",
+ "hF = F*cpF*(TF-Tref)\n",
+ "hL = L*cpF*(TL-Tref)\n",
+ "hV = Hv373*V\n",
+ "#hF + q = hL + hV\n",
+ "q = (hL+hV-hF)\n",
+ "S = q/(Hv143)\n",
+ "qsi = q*1000/3600\n",
+ "A = qsi/(U*(Ts-TL))\n",
+ "\n",
+ "#Result\n",
+ "print 'Concetrated liquid Rate: %5.1f kg/h'%L\n",
+ "print 'Vapor rate from evaporator: %5.1f kg/h'%V\n",
+ "print 'Heat Transfer area required: %4.1f m2'%(A)"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Concetrated liquid Rate: 6048.0 kg/h\n",
+ "Vapor rate from evaporator: 3024.0 kg/h\n",
+ "Heat Transfer area required: 149.3 m2\n"
+ ]
+ }
+ ],
+ "prompt_number": 3
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 8.4-2, Page Number 499"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Use of Duhring Chart for Boiling point rise\n",
+ "\n",
+ "#Variable declaration\n",
+ "P = 25.6 #Pressure in the evaporator, kPa\n",
+ "C = 30 #Weight % of NaOH in solution, K\n",
+ "Tb256 = 65.6 #Boiling point of water at 25.6 kPa, \u00b0C or 150 \u00b0C\n",
+ "\n",
+ "#Calculation\n",
+ "#From Fig. 8.4-2 for 30% wt of NaoOH and boiling point of water 150 \u00b0F\n",
+ "Ts = 175 #Boiling point of solution \u00b0F\n",
+ "TsC = 79.5 #Boiling point of solution \u00b0C\n",
+ "BPR = TsC-Tb256\n",
+ "#Result\n",
+ "\n",
+ "print \"Boiling point rise: \",BPR,\"\u00b0C\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Boiling point rise: 13.9 \u00b0C\n"
+ ]
+ }
+ ],
+ "prompt_number": 4
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 8.4-3, Page number 501"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Evaporation of NaOH Solution\n",
+ "\n",
+ "# Variable declaration\n",
+ "F = 4536. #Feed rate to the evaporator, kg/hr\n",
+ "xF = 0.2 #weight percent of NaOH, kg/kg\n",
+ "TF = 60.0 #Temperature of feed, \u00b0C\n",
+ "xL = 0.5 #Weight percentage of concentrated product, kg/kg \n",
+ "P = 11.7 #Pressure of vapor space, kPa\n",
+ "Ps = 172.4 #Pressure of saturated steam used for heating, kPa\n",
+ "U = 1560. #Overall heat transfer coefficient, W/m2K\n",
+ "cpS = 1.884 #Specific heat of steam 11.7 kPa , kJ/(kg.K)\n",
+ "Hv895 = 2667. #Enthalpy of steam at 11.7 kPa and 89.5\u00b0C\n",
+ "Hv489 = 2590. #Enthalp of steam at 11.7 kPa and 49.5\u00b0C\n",
+ "LambdaV1724 = 2214 #Latent heat of evaporation of water at 172.4 kPa and at 115.6\u00b0C\n",
+ "Ts = 115.6 #Saturation temperature of 172.4kPa in \u00b0C\n",
+ "\n",
+ "# Calculation\n",
+ "L = F*xF/xL\n",
+ "V = F - L\n",
+ "BPw117 = 48.9 #BP of Water From steam table, \u00b0C\n",
+ "BPs117 = 89.5 #BP of Soln From Duhring Chart Fig 8.4-2, \u00b0C\n",
+ "BPR = BPs117-BPw117\n",
+ "hF = 214. #Enthalpy of 20% feed at 60\u00b0C, KJ/Kg from fig 8.4-3 \n",
+ "hL = 505. #Enthalpy of 50% feed at 89.5\u00b0C, KJ/Kg\n",
+ "HV = Hv489 + cpS*BPR\n",
+ "S = (L*hL+V*HV-F*hF)/LambdaV1724\n",
+ "Q = S*LambdaV1724/3600 #Heat addition rate in kW\n",
+ "#Newtons law of cooling \n",
+ "\n",
+ "A = Q*1000/(U*(Ts-BPs117))\n",
+ "SteamEco = V/S\n",
+ "#Result\n",
+ "print \"The steam used\",round(S,1),\"kg steam/h\"\n",
+ "print \"The calculated steam economy is \",round(SteamEco,3)\n",
+ "print \"The heating surface area is \", round(A,1),\"m2\"\n",
+ "print 'Difference in answers is due to machin precision'"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The steam used 3253.2 kg steam/h\n",
+ "The calculated steam economy is 0.837\n",
+ "The heating surface area is 49.1 m2\n"
+ ]
+ }
+ ],
+ "prompt_number": 1
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 8.5-1, Page number 505"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Evaporation of Sugar Solution in a Triple-Effect Evaporator\n",
+ "import numpy as np\n",
+ "from scipy.interpolate import interp1d\n",
+ "\n",
+ "# Variable declaration\n",
+ "xF = 0.1 #wt fraction of sugar in Feed\n",
+ "xP = 0.5 #wt fraction of sugar in Product\n",
+ "Ts1 = 121.1 #Saturation temperature of the steam at 205.5kPa in \u00b0C\n",
+ "F = 22680. #Feed Rate kg/hr\n",
+ "TF = 26.7 #Temperature of the feed, \u00b0C\n",
+ "U1 = 3123. #Overall heat transfer coefficient for evaporator 1, W/(m2K) \n",
+ "U2 = 1987. #Overall heat transfer coefficient for evaporator 2, W/(m2K)\n",
+ "U3 = 1136. #Overall heat transfer coefficient for evaporator 3, W/(m2K)\n",
+ "T = np.array([50.,60.,70.,80.,90.,100.,110.,120,126.])\n",
+ "H = np.array([2592.2,2609.7,2626.9,2643.8,2660.1,2676.0,2691.3,2706.0,2714.4])\n",
+ "h = np.array([209.3,251.1,293.0,334.9,376.9,419.1,461.3,503.7,529.2])\n",
+ "lamb = np.array([2382.9,2358.6,2334.0,2308.8,2283.2,2256.9,2230.0,2202.2,2185.2])\n",
+ "cp = np.array([])\n",
+ "\n",
+ "# Calculation\n",
+ "def BPRDegC(xw):\n",
+ " return 1.78*xw+6.22*xw*xw\n",
+ "\n",
+ "def SpecHeat(xw):\n",
+ " return 4.19-2.35*xw\n",
+ "\n",
+ "fH = interp1d(T,H)\n",
+ "fh = interp1d(T,h)\n",
+ "flamb = interp1d(T,lamb)\n",
+ "\n",
+ "#Step 1\n",
+ "BPR3 = BPRDegC(xP)\n",
+ "Tvs3 = 51.67 #Saturation temperature of steam at 13.4 kPa for 3rd evaporator\n",
+ "T3 = Tvs3 + BPR3\n",
+ "\n",
+ "#Step 2\n",
+ "L3 = F*xF/xP #Concentrated product rate, kg/hr\n",
+ "V = F - L3 #Total water vaporised from three evaporators (V = V1 + v2 +v3 ), kg/hr\n",
+ "V1 = V/3 #Assuming V1 = V2 = V3\n",
+ "V2 = V1\n",
+ "V3 = V1\n",
+ "#Making liquid balance on each evaporator \n",
+ "L1 = F - V1 #Concentrated liquid rate from evaporator 1, kg/hr\n",
+ "L2 = L1 - V2 #Concentrated liquid rate from evaporator 2, kg/hr\n",
+ "L3 = L2 - V3\n",
+ "#Making Solid balance on each evaporator \n",
+ "x1 = F*xF/L1\n",
+ "x2 = L1*x1/L2\n",
+ "x3 = xP\n",
+ "\n",
+ "#Step 3\n",
+ "BPR1 = BPRDegC(x1)\n",
+ "BPR2 = BPRDegC(x2)\n",
+ "BPR3 = BPRDegC(x3)\n",
+ "SDelT = Ts1 - Tvs3 - (BPR1+BPR2+BPR3)\n",
+ "ISU13 = 1/U1+1/U2+1/U3\n",
+ "DelT1 = SDelT*(1/U1)/ISU13\n",
+ "DelT2 = SDelT*(1/U2)/ISU13\n",
+ "DelT3 = SDelT*(1/U3)/ISU13\n",
+ "T1 = Ts1 - DelT1\n",
+ "T2 = T1 - BPR1 - DelT2\n",
+ "Ts2 = T1 - BPR1\n",
+ "T3 = T2 -BPR2 - DelT3\n",
+ "Ts3 = T2 - BPR2\n",
+ "Ts4 = T3 - BPR3\n",
+ "\n",
+ "#Step4: \n",
+ "CpF = SpecHeat(xF) #Calculate Heat Capacities\n",
+ "Cp1 = SpecHeat(x1)\n",
+ "Cp2 = SpecHeat(x2)\n",
+ "Cp3 = SpecHeat(x3)\n",
+ "\n",
+ "H1 = fH(Ts2) + 1.884*BPR1 #for effect 1\n",
+ "lambdas1 = fH(Ts1)-fh(Ts1) \n",
+ "H2 = fH(Ts3) + 1.884*BPR2 #for effect 2\n",
+ "lambdas2 = fH(Ts2)-fh(Ts2) \n",
+ "H3 = fH(Ts4) + 1.884*BPR3 #for effect 3\n",
+ "lambdas3 = fH(Ts3)-fh(Ts3) \n",
+ "\n",
+ "a11 = Cp1*T1 - lambdas2 - H2\n",
+ "a12 = -(Cp2*T2 - H2)\n",
+ "b1 = -F*lambdas2\n",
+ "a21 = lambdas3\n",
+ "a22 = Cp2*T2 - lambdas3 - H3\n",
+ "b2 = L3*Cp3*T2 - L3*H3\n",
+ "\n",
+ "\n",
+ "a = np.array([[a11,a12], [a21,a22]])\n",
+ "b = np.array([b1,b2])\n",
+ "L1,L2 = np.linalg.solve(a, b)\n",
+ "V1 = F - L1\n",
+ "V2 = L1 - L2\n",
+ "V3 = L2 - L3\n",
+ "S = (L1*Cp1*T1 + V1*H1 - F*CpF*TF)/lambdas1\n",
+ "\n",
+ "#Step5:\n",
+ "q1 = S*lambdas1*1000/3600\n",
+ "q2 = V1*lambdas2*1000/3600\n",
+ "q3 = V2*lambdas3*1000/3600\n",
+ "\n",
+ "A1 = q1/(U1*DelT1)\n",
+ "A2 = q2/(U2*DelT2)\n",
+ "A3 = q3/(U3*DelT3)\n",
+ "\n",
+ "Am = Am1 = (A1+A2+A3)/3\n",
+ "\n",
+ "#Step6:\n",
+ "x1 = F*xF/L1\n",
+ "x2 = L1*x1/L2\n",
+ "x3 = L2*x2/L3\n",
+ "\n",
+ "#Step7:\n",
+ "BPR1 = BPRDegC(x1)\n",
+ "BPR2 = BPRDegC(x2)\n",
+ "BPR3 = BPRDegC(x3)\n",
+ "SDelT = Ts1 - Tvs3 - (BPR1+BPR2+BPR3)\n",
+ "\n",
+ "DelT1 = DelT1*A1/Am\n",
+ "DelT2 = DelT2*A2/Am\n",
+ "DelT3 = DelT3*A3/Am\n",
+ "\n",
+ "T1 = Ts1 - DelT1\n",
+ "T2 = T1 - BPR1 - DelT2\n",
+ "Ts2 = T1 - BPR1\n",
+ "T3 = T2 -BPR2 - DelT3\n",
+ "Ts3 = T2 - BPR2\n",
+ "Ts4 = T3 - BPR3\n",
+ "\n",
+ "\n",
+ "#Step8: \n",
+ "CpF = SpecHeat(xF) #Calculate Heat Capacities\n",
+ "Cp1 = SpecHeat(x1)\n",
+ "Cp2 = SpecHeat(x2)\n",
+ "Cp3 = SpecHeat(x3)\n",
+ "\n",
+ "H1 = fH(Ts2) + 1.884*BPR1 #for effect 1\n",
+ "lambdas1 = fH(Ts1)-fh(Ts1) \n",
+ "H2 = fH(Ts3) + 1.884*BPR2 #for effect 2\n",
+ "lambdas2 = fH(Ts2)-fh(Ts2) \n",
+ "H3 = fH(Ts4) + 1.884*BPR3 #for effect 3\n",
+ "lambdas3 = fH(Ts3)-fh(Ts3) \n",
+ "\n",
+ "a11 = Cp1*T1 - lambdas2 - H2\n",
+ "a12 = -(Cp2*T2 - H2)\n",
+ "b1 = -F*lambdas2\n",
+ "a21 = lambdas3\n",
+ "a22 = Cp2*T2 - lambdas3 - H3\n",
+ "b2 = L3*Cp3*T2 - L3*H3\n",
+ "\n",
+ "a = np.array([[a11,a12], [a21,a22]])\n",
+ "b = np.array([b1,b2])\n",
+ "L1,L2 = np.linalg.solve(a, b)\n",
+ "V1 = F - L1\n",
+ "V2 = L1 - L2\n",
+ "V3 = L2 - L3\n",
+ "S = (L1*Cp1*T1 + V1*H1 - F*CpF*TF)/lambdas1\n",
+ "\n",
+ "q1 = S*lambdas1*1000/3600\n",
+ "q2 = V1*lambdas2*1000/3600\n",
+ "q3 = V2*lambdas3*1000/3600\n",
+ "\n",
+ "A1 = q1/(U1*DelT1)\n",
+ "A2 = q2/(U2*DelT2)\n",
+ "A3 = q3/(U3*DelT3)\n",
+ "Am = (A1+A2+A3)/3\n",
+ "SEconomy = (V1+V2+V3)/S\n",
+ "\n",
+ "#Results\n",
+ "print 'Area A1 A2 and A3 for 1st 2nd and 3rd effect are %4.3f, %4.3f,and %4.3f'%(A1,A2,A3) \n",
+ "print \"The Average area of each effect\",round(Am,2),\"as compared to average area\",round(Am1,2),\"in first trial\" \n",
+ "print \"Steam Economy for tripple effect evaporator:\", round(SEconomy,3) \n",
+ "print 'Difference in answers is due to machin precision'"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Area A1 A2 and A3 for 1st 2nd and 3rd effect are 111.421, 113.714,and 111.640\n",
+ "The Average area of each effect 112.26 as compared to average area 112.08 in first trial\n",
+ "Steam Economy for tripple effect evaporator: 1.999\n"
+ ]
+ }
+ ],
+ "prompt_number": 1
+ }
+ ],
+ "metadata": {}
+ }
+ ]
+}
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