From 64d949698432e05f2a372d9edc859c5b9df1f438 Mon Sep 17 00:00:00 2001 From: kinitrupti Date: Fri, 12 May 2017 18:40:35 +0530 Subject: Revised list of TBCs --- .../Chapter3.ipynb | 628 +++++++++++++++++++++ 1 file changed, 628 insertions(+) create mode 100755 backup/Mass_-_Transfer_Operations_version_backup/Chapter3.ipynb (limited to 'backup/Mass_-_Transfer_Operations_version_backup/Chapter3.ipynb') diff --git a/backup/Mass_-_Transfer_Operations_version_backup/Chapter3.ipynb b/backup/Mass_-_Transfer_Operations_version_backup/Chapter3.ipynb new file mode 100755 index 00000000..36f53f4d --- /dev/null +++ b/backup/Mass_-_Transfer_Operations_version_backup/Chapter3.ipynb @@ -0,0 +1,628 @@ +{ + "metadata": { + "name": "", + "signature": "sha256:64d9a62e17838716bd10cd86f93be8c39dc69462337a3d3adc3d6ea158cbc575" + }, + "nbformat": 3, + "nbformat_minor": 0, + "worksheets": [ + { + "cells": [ + { + "cell_type": "heading", + "level": 1, + "metadata": {}, + "source": [ + "Chapter 3: Mass-Transfer Coefficients" + ] + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.1:Page 53" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.1\n", + "# Page: 53\n", + "\n", + "print'Illustration 3.1 - Page: 53\\n\\n'\n", + "\n", + "# solution\n", + "\n", + "#****Data*****#\n", + "# a = CO2 b = H2O\n", + "Ca0 = 0;#[kmol/cubic m]\n", + "Cai = 0.0336;#[kmol/cubic m]\n", + "Dab = 1.96*10**(-9);# [square m/s]\n", + "#*******#\n", + "\n", + "density = 998.0;# [kg/cubic m]\n", + "viscosity = 8.94*10**(-4);#[kg/m.s]\n", + "rate = 0.05;#[kg/m.s] mass flow rate of liquid\n", + "L = 1;#[m]\n", + "g = 9.81;#[m/square s]\n", + "# From Eqn. 3.10\n", + "Del = ((3*viscosity*rate)/((density**2)*g))**(1.0/3);# [m]\n", + "Re = 4*rate/viscosity;\n", + "# Flow comes out to be laminar\n", + "# From Eqn. 3.19\n", + "Kl_avg = ((6*Dab*rate)/(3.141*density*Del*L))**(1.0/2);#[kmol/square m.s.(kmol/cubic m)]\n", + "bulk_avg_velocity = rate/(density*Del);#[m/s]\n", + "# At the top: Cai-Ca = Cai_Ca0 = Cai\n", + "#At the bottom: Cai-Cal\n", + "# From Eqn. 3.21 & 3.22\n", + "Cal = Cai*(1-(1.0/(exp(Kl_avg/(bulk_avg_velocity*Del)))));# [kmol/cubic m]\n", + "rate_absorption = bulk_avg_velocity*Del*(Cal-Ca0);# [kmol/s].(m of width)\n", + "print'The rate of absorption is ',round(rate_absorption,8),' kmol/sec.(m of width)'\n", + "# The actual value may be substantially larger." + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.1 - Page: 53\n", + "\n", + "\n", + "The rate of absorption is 7.2e-07 kmol/sec.(m of width)\n" + ] + } + ], + "prompt_number": 8 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.2: Page 56" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.2\n", + "# Page: 56\n", + "\n", + "print'Illustration 3.2 - Page: 56\\n\\n'\n", + "\n", + "# solution\n", + "\n", + "#***Data****#\n", + "d = 0.025;# [m]\n", + "avg_velocity = 3;# [m/s]\n", + "viscosity = 8.937*10**(-4);# [kg/m.s]\n", + "density = 997;# [kg/m**3]\n", + "#*********#\n", + "\n", + "kinematic_viscosity = viscosity/density;# [square m/s]\n", + "Re = d*avg_velocity*density/viscosity;\n", + "# Reynold's number comes out to be 83670\n", + "# At this Reynold's number fanning factor = 0.0047\n", + "f = 0.0047;\n", + "L = 1;# [m]\n", + "press_drop = 2*density*f*L*(avg_velocity**2)/(d);# [N/square m]\n", + "P = 3.141*(d**2)*avg_velocity*press_drop/4;# [N.m/s] for 1m pipe\n", + "m = 3.141*(d**2)*L*density/4;\n", + "# From Eqn. 3.24\n", + "Ld = ((kinematic_viscosity**3)*m/P)**(1.0/4);# [m]\n", + "# From Eqn. 3.25\n", + "Ud = (kinematic_viscosity*P/m)**(1.0/4);# [m/s]\n", + "print'Velocity of small eddies is',round(Ud,4),'m/s'\n", + "print'Length scale of small eddies is',round(Ld,7),'m'" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.2 - Page: 56\n", + "\n", + "\n", + "Velocity of small eddies is 0.0549 m/s\n", + "Length scale of small eddies is 1.63e-05 m\n" + ] + } + ], + "prompt_number": 17 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.3: Page 69" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.3\n", + "# Page: 69\n", + "\n", + "print'Illustration 3.3 - Page: 69\\n\\n'\n", + "\n", + "# solution\n", + "\n", + "# Heat transfer analog to Eqn. 3.12\n", + "# The Eqn. remains the same with the dimensionless conc. ratio replaced by ((tl-to)/(ti-to))\n", + "\n", + "# The dimensionless group:\n", + "# eta = 2*Dab*L/(3*del**2*velocity);\n", + "# eta = (2/3)*(Dab/(del*velocity))*(L/del);\n", + "# Ped = Peclet no. for mass transfer\n", + "# eta = (2/3)*(1/Ped)*(L/del);\n", + "\n", + "# For heat transfer is replaced by\n", + "# Peh = Peclet no. for heat transfer\n", + "# eta = (2/3)*(1/Peh)*(L/del);\n", + "# eta = (2/3)*(alpha/(del*velocity))*(L/del);\n", + "# eta = (2*alpha*L)/(3*del**2*velocity);\n", + "print'Heat transfer analog to Eqn. 3.21 is eta = (2*alpha*L)/(3*del**2*velocity)'" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.3 - Page: 69\n", + "\n", + "\n", + "Heat transfer analog to Eqn. 3.21 is eta = (2*alpha*L)/(3*del**2*velocity)\n" + ] + } + ], + "prompt_number": 1 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.4: Page-69" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.4\n", + "# Page: 69\n", + "\n", + "import math\n", + "print'Illustration 3.4 - Page: 69\\n\\n'\n", + "\n", + "# solution\n", + "\n", + "#***Data****#\n", + "# a = UF6 b = air\n", + "# The average heat transfer coefficient: Nu_avg = 0.43+0.532(Re^0.5)(Pr^0.31)\n", + "# The analogus expression for mass transfer coefficient: Sh_avg = 0.43+0.532(Re^0.5)(Sc^0.31)\n", + "d = 0.006;# [m]\n", + "velocity = 3.0;# [m/s]\n", + "surf_temp = 43.0;# [C]\n", + "bulk_temp = 60.0;# [C]\n", + "avg_temp = (surf_temp+bulk_temp)/2; #[C]\n", + "density = 4.10;# [kg/cubic m]\n", + "viscosity = 2.7*10**(-5);# [kg/m.s]\n", + "Dab = 9.04*10**(-6);# [square m/s]\n", + "press = 53.32;# [kN/square m]\n", + "tot_press = 101.33;# [kN/square m]\n", + "#******#\n", + "\n", + "avg_press = press/2.0; # [kN/square m]\n", + "Xa = avg_press/tot_press;\n", + "Xb = 1-Xa;\n", + "Re = d*velocity*density/viscosity;\n", + "Sc = viscosity/(density*Dab);\n", + "Sh_avg = 0.43+(0.532*(2733**0.5)*(0.728**0.5));\n", + "c = 273.2/(22.41*(273.2+avg_temp));# [kmol/cubic m]\n", + "F_avg = Sh_avg*c*Dab/d;#[kmol/cubic m]\n", + "Nb = 0.0;\n", + "Ca1_by_C = press/tot_press;\n", + "Ca2_by_C = 0.0;\n", + "Flux_a = 1.0;\n", + "# Using Eqn. 3.1\n", + "Na = Flux_a*F_avg*math.log((Flux_a-Ca2_by_C)/(Flux_a-Ca1_by_C));#[kmol UF6/square m.s]\n", + "print'Rate of sublimation is',round(Na,8),' kmol UF6/square m.s'\n", + "# the answer is slightly different in textbook due to approximation" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.4 - Page: 69\n", + "\n", + "\n", + "Rate of sublimation is 0.00102088 kmol UF6/square m.s\n" + ] + } + ], + "prompt_number": 21 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.5: Page 73" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.5\n", + "# Page: 73\n", + "\n", + "print'Illustration 3.5 - Page: 73\\n\\n'\n", + "\n", + "# solution\n", + "\n", + "#****Data****#\n", + "velocity = 15.0;# [m/s]\n", + "G = 21.3;# [kg/square m.s]\n", + "#******#\n", + "\n", + "# Since the experimental data do not include the effects of changing Prandtl number.\n", + "\n", + "# Jh = (h/(Cp*density*viscosity)) = (h/Cp*G)*(Pr^(2/3)) = Shi(Re);\n", + "\n", + "# Shi(Re) must be compatible with 21.3*(G**0.6);\n", + "# Let Shi(Re) = b*(Re**n);\n", + "# Re = (l*G)/viscosity;\n", + "\n", + "# h = (Cp*G/(Pr**(2/3)))*b*(Re**n);\n", + "# h = (Cp*G/(Pr**(2/3)))*b*((l*b/viscosity)**n) = 21.3*(G**0.6);\n", + "\n", + "n = 0.6-1;\n", + "# b = 21.3*((Pr**(2/3))/Cp)*((l/viscosity)**(-n));\n", + "\n", + "# Using data for air at 38 C & 1 std atm.\n", + "Cp1 = 1002;# [kJ/kg.K]\n", + "viscosity1 = 1.85*10**(-5);#[kg/m.s]\n", + "k1 = 0.0273;#[W/m.K]\n", + "Pr1 = (Cp1*viscosity1)/k1;\n", + "b_prime = 21.3*(Pr1**(2.0/3)/Cp1)*((1/viscosity1)**0.4);\n", + "# b = b_prime*l**(0.4);\n", + "# Jh = (h/(Cp*G))*Pr**(2/3) = b_prime*((l/Re)**(0.4)) = Shi(Re);\n", + "\n", + "# The heat mass transfer analogy will be used to estimate the mass transfer coefficient. (Jd = Jh)\n", + "\n", + "# Jd = (KG*Pbm*Mav*Sc**(2/3))/(density*viscosity) = Shi(Re) = b_prime*((l/Re)**0.4);\n", + "\n", + "# KG*Pbm = F = (b_prime*density*viscosity)/(Re^0.4*Mav*Sc**(2/3)) = (b_prime*(density*velocity)**0.6*(viscosity^0.4))/(Mav*Sc**(2/3));\n", + "\n", + "# For H2-H20, 38 C, 1std atm\n", + "viscosity2 = 9*10**(-6);# [kg/m.s]\n", + "density2 = 0.0794;# [kg/cubic m]\n", + "Dab = 7.75*10**(-5);# [square m/s]\n", + "Sc = viscosity2/(density2*Dab);\n", + "\n", + "# Assuming desity, Molecular weight and viscosity of the gas are essentially those of H2\n", + "\n", + "Mav = 2.02;# [kg/kmol]\n", + "F = (b_prime*(density2*velocity)**0.6*(viscosity2**0.4))/(Mav*Sc**(2.0/3));# [kmol/square m.s]\n", + "print'The required mass transfer: ',round(F,5),' kmol/square m.s'" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.5 - Page: 73\n", + "\n", + "\n", + "The required mass transfer: 0.00525 kmol/square m.s\n" + ] + } + ], + "prompt_number": 27 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.6:Page 77" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.6\n", + "# Page: 77\n", + "\n", + "print'Illustration 3.6 - Page: 77\\n\\n'\n", + "\n", + "# solution\n", + "from scipy import integrate\n", + "import math \n", + "#***Data***#\n", + "Dp = 0.0125;# [m]\n", + "viscosity = 2.4*10**(-5);# [kg/m.s]\n", + "Sc = 2.0;\n", + "E = 0.3;\n", + "Go = (2*10**(-3))/0.1;# molar superficial mass velocity [kmol/square m.s]\n", + "#********#\n", + "\n", + "# a = CO b = Ni(CO)4\n", + "# Nb = -(Na/4);\n", + "Flux_a = 4.0/3;\n", + "Ca2_by_C = 0;# At the metal interface\n", + "# Ca1_by_C = Ya #mole fraction of CO in the bulk\n", + "\n", + "# Eqn. 3.1 becomes: Na = (4/3)*F*log((4/3)/((4/3)-Ya));\n", + "\n", + "# Let G = kmol gas/(square m bed cross section).s\n", + "# a = specific metal surface\n", + "# z = depth \n", + "# Therefore, Na = -(diff(Ya*G))/(a*diff(z));# [kmol/((square m metal surface).s)];\n", + "# For each kmol of CO consumed, (1/4)kmol Ni(CO)4 forms, representing a loss of (3/4) kmol per kmol of CO consumed.\n", + "# The CO consumed through bed depth dz is therefore (Go-G)(4/3) kmol;\n", + "# Ya = (Go-(Go-G)*(4/3))/G;\n", + "# G = Go/(4-(3*Ya));\n", + "# diff(YaG) = ((4*Go)/(4-3*Ya)**2)*diff(Ya);\n", + "\n", + "# Substituting in Eqn. 3.64\n", + "# -(4*Go/((4-3*Ya)**2*a))*(diff(Ya)/diff(z)) = (4/3)*F*log(4/(4-3*Ya));\n", + "\n", + "# At depth z:\n", + "# Mass velocity of CO = (Go-(Go-G)/(4/3))*28;\n", + "# Mass velocity of Ni(CO)4 = ((Go-G)*(1/3))*170.7;\n", + "# G_prime = 47.6*Go-19.6G; # total mass velocity [kg/square m.s]\n", + "# Substituting G leads to:\n", + "# G_prime = Go*(47.6-19.6*(4-3*Ya));# [kg/m.s]\n", + "# Re = (Dp*G')/viscosity\n", + "\n", + "# With Go = 0.002 kmol/square m.s & Ya in the range 1-0.005, the range of Re is 292-444;\n", + "# From table 3.3:\n", + "# Jd = (F/G)*(Sc**(2/3)) = (2.06/E)*Re**(-0.575);\n", + "# F = (2.06/E*(Sc)**(2/3))*(Go/(4-3*Ya))*Re**(-0.575);\n", + "\n", + "a = 6*(1-E)/Dp;\n", + "\n", + "# Result after arrangement:\n", + "\n", + "X2=lambda Ya:-((4*Go)/((4-(3*Ya))**2.0*a))*(3.0/4)*(E*(Sc**(2.0/3))*(4-(3*Ya))/(2.06*Go)*(1/math.log(4.0/(4-(3*Ya)))))*(((Dp/viscosity)*(Go*(47.6-(19.6/(4.0-(3*Ya))))))**0.575);# [m]\n", + "Z = integrate.quad(X2,1,0.005);\n", + "print'The bed depth required to reduce the CO content to 0.005 is',round(Z[0],3),'m'\n", + "#the answers are slightly different in textbook due to approximation while here answers are precise" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.6 - Page: 77\n", + "\n", + "\n", + "The bed depth required to reduce the CO content to 0.005 is 0.132 m\n" + ] + } + ], + "prompt_number": 7 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.7: Page 80" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.7\n", + "# Page: 80\n", + "\n", + "print'Illustration 3.7 - Page: 80\\n\\n'\n", + "\n", + "# solution\n", + "\n", + "#****Data*****#\n", + "# a = water b = air\n", + "out_dia = 0.0254;# [m]\n", + "wall_thick = 0.00165;# [m]\n", + "avg_velocity = 4.6;# [m/s]\n", + "T1 = 66.0;# [C]\n", + "P = 1.0;# [atm]\n", + "Pa1 = 0.24;# [atm]\n", + "k1 = 11400.0;# [W/(square m.K)]\n", + "T2 = 24.0;# [C]\n", + "k2 = 570.0;# [W/square m.K]\n", + "k_Cu = 381.0;# [w/square m.K]\n", + "#******#\n", + "\n", + "# For the metal tube\n", + "int_dia = out_dia-(2*wall_thick);# [m]\n", + "avg_dia = (out_dia+int_dia)/2;# [mm]\n", + "Nb = 0;\n", + "Flux_a = 1;\n", + "Ya1 = 0.24;\n", + "Yb1 = 1-Ya1;\n", + "Mav = (Ya1*18.02)+(Yb1*29);# [kg/kmol]\n", + "density = (Mav/22.41)*(273/(273+T1));# [kg/cubic m]\n", + "viscosity = 1.75*10**(-5);# [kg/m.s]\n", + "Cpa = 1880.0;# [J/kg.K]\n", + "Cpmix = 1145.0;# [J/kg.K]\n", + "Sc = 0.6;\n", + "Pr = 0.75;\n", + "G_prime = avg_velocity*density;# [kg/square m.s]\n", + "G = G_prime/Mav;# [kmol/square m.s]\n", + "Re = avg_dia*G_prime/viscosity;\n", + "# From Table 3.3:\n", + "# Jd = Std*Sc**(2/3) = (F/G)*Sc**(2/3) = 0.023*Re**(-0.17);\n", + "Jd = 0.023*Re**(-0.17);\n", + "F = (0.023*G)*(Re**(-0.17)/Sc**(2.0/3));\n", + "\n", + "# The heat transfer coeffecient in the absence of mass transfer will be estimated through Jd = Jh\n", + "# Jh = Sth*Pr^(2/3) = (h/Cp*G_prime)*(Pr^(2/3)) = Jd\n", + "h = Jd*Cpmix*G_prime/(Pr**(2.0/3));\n", + "\n", + "U = 1/((1/k1)+((wall_thick/k_Cu)*(int_dia/avg_dia))+((1/k2)*(int_dia/out_dia)));# W/square m.K\n", + "\n", + "# Using Eqn. 3.70 & 3.71 with Nb = 0\n", + "# Qt = (Na*18.02*Cpa/1-exp(-(Na*18.02*Cpa/h)))*(T1-Ti)+(Lambda_a*Na);\n", + "# Qt = 618*(Ti-T2);\n", + "# Using Eqn. 3.67, with Nb = 0, Cai/C = pai, Ca1/C = Ya1 = 0.24;\n", + "# Na = F*log(((Flux_a)-(pai))/((Flux_a)-(Ya1));\n", + "\n", + "# Solving above three Eqn. simultaneously:\n", + "Ti = 42.2;# [C]\n", + "pai = 0.0806;# [atm]\n", + "Lambda_a = 43.4*10**6;# [J/kmol]\n", + "Na = F*log(((Flux_a)-(pai))/((Flux_a)-(Ya1)));# [kmol/square m.s]\n", + "Qt1 = 618*(Ti-T2);# [W/square m]\n", + "Qt2 = ((Na*18.02*Cpa/(1-exp(-(Na*18.02*Cpa/h))))*(T1-Ti))+(Lambda_a*Na);# [W/square m]\n", + "\n", + "# since the value of Qt1 & Qt2 are relatively close\n", + "print'The local rate of condensation of water is ',round(Na,6),' kmol/square m.s'" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.7 - Page: 80\n", + "\n", + "\n", + "The local rate of condensation of water is 0.000232 kmol/square m.s\n" + ] + } + ], + "prompt_number": 36 + }, + { + "cell_type": "heading", + "level": 2, + "metadata": {}, + "source": [ + "Ex3.8: Page 81" + ] + }, + { + "cell_type": "code", + "collapsed": false, + "input": [ + "\n", + "\n", + "# Illustration 3.8\n", + "# Page: 81\n", + "\n", + "import math\n", + "print'Illustration 3.8 - Page: 81\\n\\n'\n", + "print'Illustration 3.8 (a)\\n\\n'\n", + "\n", + "# Solution (a)\n", + "\n", + "#***Data****#\n", + "# a = water b = air\n", + "Nb = 0;\n", + "h = 1100.0;# [W/square m]\n", + "#*****#\n", + "\n", + "Ma = 18.02;# [kg/kmol]\n", + "Cpa = 2090;# [J/kg.K]\n", + "T1 = 600.0;# [C]\n", + "Ti = 260;# [C]\n", + "# The positive dirn. is taken to be from the bulk gas to the surface.\n", + "Has = 2.684*(10**6);# enthapy of saturated steam at 1.2 std atm, rel. to the liquid at 0 C in [J/kg]\n", + "Hai = 2.994*(10**6);# enthalpy of steam at 1 std atm, 260 C in [J/kg]\n", + "\n", + "# Radiation contributions to the heat transfer from the gas to the surface are negligible. Eqn. 3.70 reduces to\n", + "Na = -((h/(Ma*Cpa))*log(1-((Cpa*(T1-Ti))/(Has-Hai))));# [kmol/square m.s]\n", + "print'The rate of steam flow reqd. is',round(Na,4),' kmol/square m.s\\n\\n'\n", + "# negative sign indicates that the mass flux is into the gas\n", + "\n", + "print'Illustration 3.8 (b)\\n\\n'\n", + " \n", + "# Solution (b)\n", + "\n", + "#***Data****#\n", + "# a = water b = air\n", + "h = 572.0;# [W/square m]\n", + "T1 = 25.0;# [C]\n", + "#******#\n", + "\n", + "Ti = 260.0;# [C]\n", + "# The positive dirn. is taken to be from the bulk gas to the surface.\n", + "Has = 1.047*10**(5);# enthapy of saturated steam at 1.2 std atm, rel. to the liquid at 0 C in [J/kg]\n", + "Hai = 2.994*(10**6);# enthalpy of steam at 1 std atm, 260 C in [J/kg]\n", + "\n", + "# Radiation contributions to the heat transfer from the gas to the surface are negligible. Eqn. 3.70 reduces to\n", + "Na = -((h/(Ma*Cpa))*math.log(1-((Cpa*(T1-Ti))/(Has-Hai))));# [kmol/square m.s]\n", + "print'The rate of steam flow reqd. is',round(Na,4),' kmol/square m.s'\n", + "# negative sign indicates that the mass flux is into \n", + "# the answer of part B in textbook is incorrect" + ], + "language": "python", + "metadata": {}, + "outputs": [ + { + "output_type": "stream", + "stream": "stdout", + "text": [ + "Illustration 3.8 - Page: 81\n", + "\n", + "\n", + "Illustration 3.8 (a)\n", + "\n", + "\n", + "The rate of steam flow reqd. is -0.0348 kmol/square m.s\n", + "\n", + "\n", + "Illustration 3.8 (b)\n", + "\n", + "\n", + "The rate of steam flow reqd. is 0.0028 kmol/square m.s\n" + ] + } + ], + "prompt_number": 42 + } + ], + "metadata": {} + } + ] +} \ No newline at end of file -- cgit