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diff --git a/Process_Heat_Transfer_by_D_Q_Kern/14-Evopartion.ipynb b/Process_Heat_Transfer_by_D_Q_Kern/14-Evopartion.ipynb new file mode 100644 index 0000000..7e78a0a --- /dev/null +++ b/Process_Heat_Transfer_by_D_Q_Kern/14-Evopartion.ipynb @@ -0,0 +1,623 @@ +{ +"cells": [ + { + "cell_type": "markdown", + "metadata": {}, + "source": [ + "# Chapter 14: Evopartion" + ] + }, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.1: Calculation_of_Evaporator_Surface.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\t example 14.1 \n');\n", +"printf('\t approximate values are mentioned in the book \n');\n", +"\n", +"t1 = 300; //°F\n", +"t2 = 226; //°F\n", +"bs = 700; // Btu/((hr)(ft^2)(°F))\n", +"//Heat Balance\n", +"Qv = 10000 * 961; // Btu/hr\n", +"printf('\tQevap is %.2e Btu/hr\n',Qv);\n", +"Q3 = 10550 * 910; //Btu/hr\n", +"printf('\tQ300°F is %.2e Btu/hr\n',Q3);\n", +"\n", +"delT = t1-t2; //°F\n", +"printf('\tTemperature head = %.0f °F\n',delT);\n", +"Ud = bs * 0.865;\n", +"printf('\tOverall coefficient %.0f\n',Ud);\n", +"A = Qv/(Ud * delT); //ft^2\n", +"printf('\tSurface required is %.0f ft^2\n',A); //Wrong calculation in book\n", +"//end" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.2: Calculation_of_a_Triple_effect_Forward_feed_Evaporator.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\t example 14.2 \n');\n", +"printf('\t approximate values are mentioned in the book \n');\n", +"\n", +"wf = 50000; // lb/hr\n", +"sf = wf * 0.10; // lb/hr\n", +"tp = sf/0.50; // lb/hr\n", +"printf('\tTotal product is %.0f lb/hr\n',tp);\n", +"te = wf - tp;\n", +"printf('\tTotal evaporation is %.0f lb/hr\n',te);\n", +"cf = 1.0;\n", +"tF = 100; // °F\n", +"T1 = 244; // °F\n", +"T2 = 125; // °F\n", +"U1=600; // Btu/((hr)*(ft^2)*(°F))\n", +"U2=250; // Btu/((hr)*(ft^2)*(°F))\n", +"U3=125; // Btu/((hr)*(ft^2)*(°F))\n", +"\n", +"T = T1-T2;\n", +"printf('\tTotal temperature difference is delT%.0f °F\n',T);\n", +"df = (26.70- 1.95)/3; // psi/effect\n", +"printf('\tAverage pressure difference is delP%.2f psi/effect \n',df);\n", +"\n", +"printf('\n\t\t\t\t\tPressure, psia\t\t delP, psi \t Steam or vapor, °F \t lambda, Btu/lb\n\tSteam chest, 1st effect \t 26.70 \t\t\t .... \t\t Ts = 244 \t\t ls = 949 \n\tSteam chest, 2nd effect \t 18.45 \t\t\t 8.25 \t\t t1 = 224 \t\t l1 = 961 \n\tSteam chest, 3rd effect \t 10.20(20.7 in. Hg) \t 8.25 \t\t t2 = 194 \t\t l1 = 981 \n\tVapor to condenser \t\t 1.95(26 in. Hg) \t 8.25 \t\t t2 = 125 \t\t l1 = 1022 \n');\n", +"\n", +"printf('\t949*Ws + 50000*(100-224) = 961*w1\n\t961*w1 + (50000 - w1)*(224-194) = 981 * w2\n\t981*w2 + (50000-w1-w2)(194-125) = 1022 * w2\n\tw1+w2+w3 = 40000\n');\n", +"printf('\tSolving simultaneously\n');\n", +"w1=12400;\n", +"printf('\tw1 = %.2e \n',w1);\n", +"w2=13300;\n", +"printf('\tw2 = %.2e \n',w2);\n", +"w3=14300;\n", +"printf('\tw3 = %.2e \n',w3);\n", +"\n", +"Wt = w1+w2+w3;\n", +"printf('\tW1-3 is %.0e \n',Wt);\n", +"Ws = 19100;\n", +"lms = 949;\n", +"lm1 = 961;\n", +"lm2 = 981;\n", +"lm3 = 1022;\n", +"Ts = 244;\n", +"t1 = 224;\n", +"t2 = 194;\n", +"t3 = 125;\n", +"\n", +"A1 = (Ws * lms)/(U1*(Ts-t1)); //ft^2\n", +"printf('\tA1 is %.0f ft^2 \n',A1);\n", +"A2 = (w1*lm1)/(U2*(t1-t2)); //ft^2\n", +"printf('\tA2 is %.0f ft^2 \n',A2);\n", +"A3 = (w2 * lm2)/(U3*(t2-t3)); //ft^2\n", +"printf('\tA3 is %.0f ft^2 \n',A3);\n", +"\n", +"hc = w3 * lm3; // Btu/hr, WRONG CALCULATION IN TEXT BOOK\n", +"printf('\tHeat to condenser is %.3e Btu/hr\n',hc);\n", +"wr = hc/(120-85); //lb/hr\n", +"printf('\tWater requirement is %.1e lb/hr\n',wr);\n", +"wr1 = wr/500;\n", +"printf('\t= %.0f gpm \n',wr1);\n", +"//end" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.3: Backward_feed_Multiple_effect_Evaporator.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\t example 14.3 \n');\n", +"printf('\t approximate values are mentioned in the book \n');\n", +"//Same conditions as example 14.2\n", +"U1 = 400; //Btu/((hr)*(ft^2)*(°F))\n", +"U2 = 250; //Btu/((hr)*(ft^2)*(°F))\n", +"U3 = 175; //Btu/((hr)*(ft^2)*(°F))\n", +"\n", +"w1 = 50000; // lb/hr From example 14.2\n", +"wt = 40000; // lb/hr From example 14.2\n", +"cf = 1; // From example 14.2\n", +"\n", +"printf('\t981*w2 + 50000*(100-125) = 1022*w3\n\t961*w1 + (50000 - w3)*(125-194) = 981 * w2\n\t949*Ws + (50000-w3-w2)(194-224) = 961 * w1\n\tw1+w2+w3 = 40000\n');\n", +"printf('\tSolving simultaneously\n');\n", +"w1 = 15950;\n", +"w2 = 12900;\n", +"w3 = 11150;\n", +"lms = 949;\n", +"lm1 = 961;\n", +"lm2 = 981;\n", +"lm3 = 1022;\n", +"\n", +"wt = w1+w2+w3;\n", +"printf('\tw1-3 = %.0f \n',wt);\n", +"Ws = 16950;\n", +"A1 = (Ws*lms)/(U1*20); //ft^2\n", +"printf('\tA1 is %.0f ft^2\n',A1);\n", +"A2 = (w1*lm1)/(U2*30); //ft^2\n", +"printf('\tA2 is %.0f ft^2\n',A2);\n", +"A3 = (w2*lm2)/(U3*69); //ft^2\n", +"printf('\tA3 is %.0f ft^2\n',A3);\n", +"\n", +"Avs = (A1 + A2 + A3)/3; //ft^2\n", +"printf('\tAverage surface is %.0f ft^2\n',Avs);\n", +"Av1 = 3 * Avs; //ft^2\n", +"printf('\n\tWith a better distribution temperatures and pressure, Average surface is %.0f ft^2\n',Av1);\n", +"printf('\tRecalculation\n');\n", +"Av2 = 1500; //ft^2, assume\n", +"dT1 = 28; //°F\n", +"A4 = (20/dT1)*A1; //ft^2\n", +"printf('\tA1 is %.0f ft^2\n',A4);\n", +"dT2 = 41; //°F\n", +"A5 = (30/dT2)*A2; //ft^2\n", +"printf('\tA2 is %.0f ft^2\n',A5);\n", +"dT3 = 50; //°F\n", +"A6 = (69/50)*A3; //ft^2\n", +"printf('\tA3 is %.0f ft^2\n',A6);\n", +"del1 = 119; //°F\n", +"printf('\tTs-t3 is %.0f °F\n',del1);\n", +"printf('\t\t\t\t\tPressure, psia\t\t Steam or vapor, °F \t lambda, Btu/lb\n\tSteam chest, 1st effect \t 26.70 \t\t\tTs = 244 \t\t 949 \n\tSteam chest, 2nd effect \t 16.0 \t\t\t t1 = 216 \t\t 968 \n\tSteam chest, 3rd effect \t 16.4 in. Hg) \t\t t2 = 175 \t\t 992 \n\tVapor to condenser \t\t 26 in. Hg \t\t t3 = 125 \t\t l1 = 1022 \n');\n", +"\n", +"w1 = 15450; //Solving again for \n", +"printf('\tw1 is %.0f\n',w1);\n", +"w2 = 13200;\n", +"printf('\tw2 is %.0f\n',w2);\n", +"w3 = 11350;\n", +"printf('\tw3 is %.0f\n',w3);\n", +"Ws = 16850;\n", +"printf('\tWs is %.0f\n',Ws);\n", +"Hc = w3 * 1022;\n", +"printf('\tHeat to condenser is %.2e Btu/hr\n',Hc);\n", +"wr = Hc/(120-85); //lb/hr\n", +"printf('\tWater requirement %.2e lb/hr\n',wr);\n", +"wr1 = wr/500;\n", +"printf('\t\t\t= %.0fgpm\n',wr1);\n", +"ec = wt/Ws;\n", +"printf('\tEconomy, lb evaporation/lb steam %.2f\n',ec);\n", +"\n", +"//comparision of forward and backward feed\n", +"printf('\t\t\t\tForward\t\tBackward\n\tTotal steam, lb/hr\t19100\t\t16850\n\tCooling water, gpm\t840\t\t664\n\tTotal surface, ft^2\t4800\t\t4500');\n", +"" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.4: evoparator_installer.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\texample 14.4 \n');\n", +"printf('\tapproximate values are mentioned in the book \n');\n", +"//Assumed that 37500 lb/hr of 15 psig vapor is bled from the first effect for use in thevaccum pans\n", +"printf('\n\tAVERAGE EVAPORATION PER SQUARE FOOT HEATING SURFACE FOR SUGAR EVAPORATORS\n');\n", +"printf('\tEffects\t\tWater evaporated(lb/(hr)*(ft^2))\n');\n", +"printf('\t1\t\t14-16\n\t2\t\t6-8\n\t3\t\t5-6\n\t4\t\t4-5\n\t5\t\t3-4\n');\n", +"printf('\n\tEVAPORATOR SUMMARY\n');\n", +"printf('\t------------------------------------------------------------------------------------------------------------------------------\n');\n", +"printf('\tItem\t\t\t\t\t\t\t\t\tEffects\nt\t\t\t\t\t----------------------------------------------------------------------------------------------\n\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\n');\n", +"printf('\t------------------------------------------------------------------------------------------------------------------------------\n');\n", +"printf('\t1.Steam flow, lb/hr\t\t42600\t\t38000\n\t2.Steam pressure, psi/in.Hg\t30\t\t30\t\t15\t\t5\t\t4\t\t14.5\n');\n", +"printf('\t3.Steam temp,°F\t\t\t274\t\t274\t\t250\t\t227\t\t205\t\t181\n');\n", +"printf('\t4.delT,°F\t\t\t23\t\t23\t\t21\t\t20\t\t20\t\t27\n\t5.Liquor temp, °F\t\t251\t\t251\t\t229\t\t207\t\t185\t\t164\n\t6.BPR, °F\t\t\t1\t\t1\t\t2\t\t2\t\t4\t\t7\n\t7.Vapor temp, °F\t\t250\t\t250\t\t227\t\t205\t\t181\t\t147\n\t8.Vapor pressure, pis/in.Hg\t15\t\t15\t\t5\t\t4\t\t14.5\t\t23\n\t9.Lambda, Btu/lb\t\t946\t\t946\t\t960\t\t975\t\t990\t\t1010\n\t10.Liquor in, lb/hr\t\t229000\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\n\t11.Liqour out, lb/hr\t\t190200\t\t154000\t\t117100\t\t87800\t\t64000\t\t49600\n\t12.Evaporation,lb/hr\t\t38800\t\t36200\t\t36900\t\t29300\t\t23800\t\t14400\n\t13.°Brix(out)\t\t\t15.7\t\t19.4\t\t25.5\t\t34.4\t\t46.5\t\t50.0\n\t14.A,ft^2\t\t\t3500\t\t3500\t\t5000\t\t5000\t\t5000\t\t3500\n\t15.UD,Btu/(hr)*(ft^2)*(°F)\t478\t\t425\t\t310\t\t264\t\t219\t\t138\n\t16.UD delT,Btu/(hr)*(ft^2)\t11000\t\t9780\t\t6520\t\t5270\t\t4390\t\t3740\n');//BPR values from fig 14.34a\n", +"//Saturate vapor pressure above the liquour determined from Table 7\n", +"//Saturated steam pressure in the following effect determined from Table 7\n", +"\n", +"t1 = 274; //°F\n", +"t2 = 147; //°F\n", +"t = t1-t2; //°F\n", +"printf('\tTotal temperature difference in the evaporator system = %.0f °F\n',t);\n", +"bpr1 = 1; //°F\n", +"bpr2 = 2; //°F\n", +"bpr3 = 2; //°F\n", +"bpr4 = 4; //°F\n", +"bpr5 = 7; //°F\n", +"bpr = bpr1 + bpr2 + bpr3 + bpr4 + bpr5; //°F\n", +"printf('\tThe sum of all the BPR(from effect 1B to the fifth effect inclusive) = %.0f °F\n',bpr);\n", +"tf = t-bpr; //°F\n", +"printf('\tTotal EFFECTIVE temperature difference = %.0f °F\n',tf);\n", +"lbh = 229000; //lb/hr\n", +"tp1=212; //°F\n", +"tp2=184; //°F\n", +"tp3=144; //°F\n", +"tp4=82; //°F\n", +"tj1=243; //°F\n", +"tj2=220; //°F\n", +"tj3=200; //°F\n", +"Ud1=231;\n", +"Ud2=243;\n", +"Ud3=230;\n", +"Ud4=214;\n", +"Ud5=217;\n", +"printf('\n\t\t\t\tSUGAR-JUICE HEATERS\n');\n", +"printf('\tRaw-juice heaters\t\t\t\tClear=juice heaters\n\t-----------------------------------------------------------------------------------------\n');\n", +"rj1=lbh*(tp1-tp2)*(0.91); //Btu/hr\n", +"printf('\t1.%.0f(%.0f-%.0f)(0.91) = %.2e Btu/hr',lbh,tp1,tp2,rj1);\n", +"rj2=lbh*(tj1-tj2)*(0.91); //Btu/hr\n", +"printf('\t1.%.0f(%.0f-%.0f)(0.91) = %.1e Btu/hr\n',lbh,tj1,tj2,rj2);\n", +"printf('\tVapor temp. = 227°F\tdelT=26.6°F\t\tVapor temp. = 250°F\tdelT=15.8°F\n');\n", +"printf('\tUD=%.0f\t\t\t\t\t\tUD=%.0f\n',Ud1,Ud2);\n", +"A1=rj1/(26.6*Ud1);//ft^2\n", +"A2=rj2/(15.8*Ud2);//ft^2\n", +"printf('\tSurface,A=%.0f ft^2\t\t\t\tSurface,A=%.0f ft^2\n\n',A1,A2);\n", +"\n", +"rj3=lbh*(tp2-tp3)*(0.90);//Btu/hr\n", +"printf('\t2.%.0f(%.0f-%.0f)(0.91) = %.2e Btu/hr',lbh,tp2,tp3,rj3);\n", +"rj4=lbh*(tj2-tj3)*(0.90);//Btu/hr\n", +"printf('\t2.%.0f(%.0f-%.0f)(0.91) = %.2e Btu/hr\n',lbh,tj2,tj3,rj4);\n", +"printf('\tVapor temp. = 205°F\tdelT=37.6°F\t\tVapor temp. = 227°F\tdelT=14.8°F\n');\n", +"printf('\tUD=%.0f\t\t\t\t\t\tUD=%.0f\n',Ud3,Ud4);\n", +"A3=rj3/(37.6*Ud3);//ft^2\n", +"A4=rj4/(14.8*Ud4);//ft^2\n", +"printf('\tSurface,A=%.0f ft^2\t\t\t\tSurface,A=%.0f ft^2\n\n',A3,A4);\n", +"\n", +"rj5=lbh*(tp3-tp4)*(0.90);//Btu/hr\n", +"printf('\t2.%.0f(%.0f-%.0f)(0.91) = %.2e Btu/hr',lbh,tp3,tp4,rj4);\n", +"printf('\t(Use 2 heaters at 1300 ft^2 each plus 1\n\t\t\t\t\t\t\theater at 1300 ft^2 as spare)\n');\n", +"A5=rj5/(62.2*Ud5);//ft^2\n", +"printf('\tVapor temp. = 181°F\tdelT=62.2°F\n\tSurface,A=%.0f\n',A5);\n", +"printf('\t(Use 3 heaters at 100 ft^2\n\teach plus 1 heater as spare)\n\n');\n", +"\n", +"v1=42600;//lb/hr\n", +"tt1=251;//°F\n", +"printf('\t\t\t\tHEAT BALANCE\n');\n", +"printf('\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n');\n", +"printf('\t----------------------------------------------------\n');\n", +"hia=v1*929*0.97;//Btu/hr\n", +"printf('\t1A.Heat in steam........%.2e\n',hia);\n", +"hla=lbh*(tt1-tj1)*0.91;//Btu/hr\n", +"hh=hia-hla;//Btu/hr\n", +"lb1=946;//Btu/lb\n", +"dif=hh/lb1;//lb/hr\n", +"printf('\t Heating liquor.......%.2e\n\t\t\t\t%.3e\t%.0f\n',hla,hh,dif);\n", +"ltob=lbh-dif;//lb/hr\n", +"printf('\t Liqour to 1B\n\t = %.0f lb/hr\n',ltob);\n", +"hia1=dif*929*0.97;//Btu/hr\n", +"printf('\t1B.Heat in steam........%.2e\n',hia1);\n", +"hla1=ltob*(tt1-tt1)*0.91;//Btu/hr\n", +"hh1=hia1;//Btu/hr\n", +"dif1=hh1/lb1;//lb/hr\n", +"printf('\t Heating liquor........%.0f\n\t\t\t\t%.3e\t%.0f\n',hla1,hh1,dif1);\n", +"dif2=ltob-dif1;//lb/hr\n", +"printf('\t Liqour to 2d \n\t effect=%.0f lb/hr\n',dif2);\n", +"//Similarily the values in the table are calculated\n", +"\n", +"printf('\t\t\t\t\t\t\t\tLb/hr\n');\n", +"aa=179400;//lb/hr\n", +"bb=145500;//lb/hr\n", +"cc=19700;//lb/hr\n", +"dd=30600;//lb/hr\n", +"ee=17900;//lb/hr\n", +"ff=13100;//lb/hr\n", +"tto=aa+bb+cc+dd+ee+ff;//lb/hr\n", +"printf('\t(a) Actual evaporation..................................%.0f\n',aa);\n", +"printf('\t(b) Equivalent evaporation from vapors of \n\t 1st effect used for vaccum pans.....................%.0f\n',bb);\n", +"printf('\t(c) Equivalent evaporation from 1st effect \n\t vapors used for clarified-juice heaters.............%.0f\n',cc);\n", +"printf('\t(d) Equivalent evaporation from 2d effect \n\t vapors used for clarified-and raw-juice heaters.....%.0f\n',dd);\n", +"printf('\t(e) Equivalent evaporation from 3d effect \n\t vapors used for raw-juice heaters...................%.0f\n',ee)\n", +"printf('\t(f) Equivalent evaporation from 4th effect \n\t vapors used for raw-juice heaters...................%.0f\n',ff);\n", +"printf('\t -----\n')\n", +"printf('\t Extrapolated evaporation...........................%.0f\n',tto);\n", +"esq=tto/5;//lb/hr\n", +"printf('\t\tEstimated steam quantity = %.0f lb/hr\n',esq);\n", +"aesq=80600;//lb/hr\n", +"err = esq-aesq;//lb/hr\n", +"printf('\t\tActual steam required from final heat balance = %.0f lb/hr\n',aesq);\n", +"printf('\t\t\t\t\t\t\tError = %.0f lb/hr\n',err);\n", +"ta=15;\n", +"Q=14575000; //Btu/hr Total hourly evaporation\n", +"Gpm=Q/(500*(t2-tp4-ta));//From equation 14.4\n", +"printf('\tGallons per minute of Water required = %.0f gpm',Gpm);" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.5: unit_calculation.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\texample 14.5\n');\n", +"printf('\tapproximate values are mentioned in the book \n');\n", +"st1=280; //°F\n", +"vt6=125; //°F\n", +"odT=st1-vt6; //°F\n", +"printf('\tOverall temperature difference = %.0f °F\n',odT); //corresponding to 35 psig and 26 in. Hg\n", +"bpr(1)=10; //°F\n", +"bpr(2)=8; //°F\n", +"bpr(3)=7; //°F\n", +"bpr(4)=6; //°F\n", +"bpr(5)=5; //°F\n", +"bpr(6)=5; //°F\n", +"i=1;\n", +"tbpr=0;\n", +"while(i<7)\n", +" tbpr=tbpr+bpr(i);\n", +" i=i+1;\n", +"end\n", +"printf('\tThe estimated total BPR = %.0f °F\n',tbpr); //from fig. 14.36a\n", +"edT=odT-tbpr;\n", +"printf('\tEffective temperature difference = %.0f °F\n',edT);\n", +"printf('\n\t\t\t\tEVAPORATOR SUMMARY\n\tAll bodies will consist of 300 2 in. OD, 10 BWG tubes 24 long\n');\n", +"printf('\t------------------------------------------------------------------------------------------------------------------------------\n');\n", +"printf('\tItem\t\t\t\t\t\t\t\t\tEffects\n\t\t\t\t\t----------------------------------------------------------------------------------------------\n\t\t\t\t\t1A\t\t1B\t\t2\t\t3\t\t4\t\t5\n');\n", +"printf('\t------------------------------------------------------------------------------------------------------------------------------\n');\n", +"printf('\t1.Steam flow, lb/hr\t\t20000\n\t2.Steam pressure, psi/in.Hg\t35\t\t14.5\t\t4\t\t7\t\t16.5\t\t22\n\t3.Steam temp,°F\t\t\t280\t\t249\t\t224\t\t199\t\t174\t\t151\n\t4.delT,°F\t\t\t21\t\t17\t\t18\t\t19\t\t18\t\t21\n\t5.Liquor temp, °F\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\n\t6.BPR, °F\t\t\t10\t\t8\t\t7\t\t6\t\t5\t\t5\n\t7.Vapor temp, °F\t\t259\t\t232\t\t206\t\t180\t\t156\t\t130\n\t8.Vapor pressure, pis/in.Hg\t14.5\t\t4\t\t7\t\t6\t\t5\t\t5\n\t9.Lambda, Btu/lb\t\t946\t\t962\t\t978\t\t994\t\t1008\t\t1022\n\t10.Liquor in, lb/hr\t\t73400\t\t88300\t\t101000\t\t113000\t\t72000\t\t72000\n\t11.Liqour out, lb/hr\t\t56200\t\t73400\t\t88300\t\t101100\t\t58300\t\t54700\n\t12.Evaporation,lb/hr\t\t17200\t\t14900\t\t12800\t\t11900\t\t13700\t\t17300\n\t13.Total solids, \t\t38.9\t\t29.8\t\t24.7\t\t21.6\t\t18.7\t\t20.0\n\t14.A,ft^2\t\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\t\t3250\n\t15.UD,Btu/(hr)*(ft^2)*(°F)\t262\t\t295\t\t252\t\t251\t\t221\t\t221\n\t16.UD delT,Btu/(hr)*(ft^2)\t5510\t\t5000\t\t4530t\t\t4770\t\t3980\t\t4650\n');//BPR values from fig 14.36a\n", +"//Specific-heat data are given in Fig. 14.36b\n", +"ev(1)=17200; //lb/hr\n", +"ev(2)=14900; //lb/hr\n", +"ev(3)=12800; //lb/hr\n", +"ev(4)=11900; //lb/hr\n", +"ev(5)=13700; //lb/hr\n", +"ev(6)=17300; //lb/hr\n", +"i=1;\n", +"tev =0;\n", +"while(i<7)\n", +" tev = tev+ev(i);\n", +" i=i+1;\n", +"end\n", +"printf('\n\tTotal amount of water evaporated = %.0f lb/hr\n',tev);\n", +"ttev=tev/6;//lb/hr\n", +"printf('\tTheoretical amount of steam for a six-effect evaporator = %.0f lb/hr\n',ttev);\n", +"tev2=tev/(6*0.75); //lb/hr . order of 75 percent of theoretical\n", +"printf('\tSteam used for trail balance = %.0f lb/hr\n',tev2);\n", +"lq=(tev/6);\n", +"lq=lq+(lq*0.15);\n", +"printf('\tEstimate of the amount of evaporation in the first effect = %.0f lb/hr\n',lq);\n", +"lout6=54000;//lb/hr\n", +"lq2=lout6+lq+2200;//lb/hr\n", +"printf('\tEstimated discharge from second effect = %.0f lb/hr\n',lq2);\n", +"printf('\n\t\t\t\tHEAT BALANCE\n');\n", +"cw = 17750000/(500*(125-15-60)); //gpm, values from table 14.6\n", +"printf('\t\tCooling water at 60 °F = %.0f gpm\n',cw);\n", +"printf('\t--------------------------------------------------------\n');\n", +"printf('\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n');\n", +"printf('\t--------------------------------------------------------\n');\n", +"sf=20000;//lb/hr\n", +"lqi=73400;//lb/hr\n", +"lqi2=88300\n", +"lt1=259;//°F\n", +"lt2=232;//°F\n", +"lt3=206;//°F\n", +"ev=17200;//lb/hr\n", +"his=sf*924*0.97;//Btu/hr\n", +"printf('\t1.a.Heat in steam \t%.2e\n',his);\n", +"hl=lqi*(lt1-lt2)*0.82;//Btu/hr\n", +"printf('\t b.Heating liquor \t%.2e\n',hl);\n", +"hh=his-hl;\n", +"ev1=(hh)/946;//lb/hr\n", +"printf('\t c.Evaporation\t\t\t\t%.0f\n',ev1);\n", +"dif=lqi-ev1;\n", +"tft=(dif)*(lt1-209)*0.78;\n", +"printf('\t d.To flash tank\t%.1e',tft);\n", +"ev2=tft/978;//lb/hr\n", +"printf('\t\t%.0f\n',ev2);\n", +"printf('\t e.Flashed vapor=%.0f\n',ev2);\n", +"p=dif-ev2;\n", +"printf('\t f.product %.1e\n',p);\n", +"printf('\n\t2.a.Heat in 1st vapors\t%.3e\n',hh);\n", +"hl2=lqi2*(lt2-lt3)*0.85;\n", +"printf('\t b.Heating liqour\t%.2e\n',hl2);\n", +"ev3=(hh-hl2)/962;\n", +"printf('\t c.Evaporation=%.0f',ev3);\n", +"\n", +"printf('\t\t\t%.0f\n',ev3);\n", +"lto1=lqi2-ev3;\n", +"printf('\t d.Liquor to 1b=%.0f\n',lto1);\n", +"//end" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.6: Evoparator_specificatio.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\texample 14.6\n');\n", +"printf('\tapproximate values are mentioned in the book \n');\n", +"st1=274; //°F\n", +"vt6=115; //°F\n", +"odT=st1-vt6; //°F\n", +"printf('\tTotal temperature difference = %.0f °F\n',odT); //corresponding to 35 psig\n", +"eb1=77;//°F, From fig.14.38\n", +"eb2=26;//°F, From fig.14.38\n", +"etd=odT-(eb1+eb2);//°F\n", +"printf('\tThe effective temperature difference is %.0f °F\n',etd);\n", +"printf('\n\t\t\tCAUSTIC EVAPORATOR MATERIAL BALANCE\n');\n", +"//Basis: 1 ton/hr NaOH\n", +"printf('\tCell liquour at 120°F \t\tWash at 80°F\n');\n", +"printf('\t---------------------------------------------\n');\n", +"l1=2000;//Lb\n", +"l2=3800;//Lb\n", +"l3=17050;//Lb\n", +"lq=l1+l2+l3;//Lb\n", +"w1=340;//Lb\n", +"w2=1020;//Lb\n", +"w=w1+w2;//Lb\n", +"printf('\t8.75 prcnt NaOH = %.0f\n\t16.6 prcnt NaCl = %.0f\t\t25 prcnt NaCl = %.0f\n',l1,l2,w1);\n", +"printf('\t74.65 prcnt H20 = %.0f\t\t75 prcnt H20 = %.0f\n',l3,w2);\n", +"printf('\tTotal cell liquor = %.0f\tTotoal wash = %.0f\n',lq,w);\n", +"printf('\n\t-------------------------------------------------------------------------\n');\n", +"printf('\t\t\t\tNaOH\t\tNaCl\t\tH20,Lb\tTotal,Lb\n\t\t\t\tprcnt\tLb\tprcnt\tLb\n');\n", +"printf('\t-------------------------------------------------------------------------\n');\n", +"printf('\tOverall operation:\n\t Cell liquor.......... 8.75\t'+string(l1)+'\t16.60\t'+string(l2)+'\t'+string(l3)+'\t'+string(lq)+'\n');\n", +"printf('\t Wash................. ....\t....\t25.00\t'+string(w1)+'\t'+string(w2)+'\t'+string(w)+'\n');\n", +"wl1=l2+w1;//Lb\n", +"wl2=l3+w2;//Lb\n", +"wlt=lq+w;\n", +"printf('\t Total in............. ....\t'+string(l1)+'\t....\t'+string(wl1)+'\t'+string(wl2)+'\t'+string(wlt)+'\n');\n", +"prn=110;//Lb\n", +"prh=1890;//Lb\n", +"prt=4000;//Lb\n", +"printf('\t Product.............. 50.00\t'+string(l1)+'\t2.75\t'+string(prn)+'\t'+string(prh)+'\t'+string(prt)+'\n');\n", +"r1=wl1-prn;//Lb\n", +"r2=wl2-prh;//Lb\n", +"r3=wlt-prt;//Lb\n", +"gain=3200;//gpm\n", +"printf('\t Removed.............. ....\t....\t....\t%.0f\t%.0f\t%.0f\n',r1,r2,r3);\n", +"//Rest of the table is calculated similarily\n", +"printf('\n\t\t\t\t\tCAUSTIC EVAPORATOR SUMMARY\n');\n", +"printf('\t------------------------------------------------------------------------------------\n');\n", +"printf('\tItem\t\t\t\t\tEffects\nt\t\t\t\t\t--------------------\t\tFlash Tank\n\t\t\t\t\t\I\t\tII\n');\n", +"printf('\t------------------------------------------------------------------------------------\n');\n", +"printf('\t1.Steam pressure, psi/in.Hg\t30\n\t2.Steam temperature,°F\t\t274\t\t169\n\t3.delT,°F\t\t\t28\t\t28\n\t4.Liquor temperature, °F\t246\t\t141\t\t192\n\t5.BPR, °F\t\t\t77\t\t26\t\t77\n\t6.Vapor temperature, °F\t\t169\t\t115\t\t115\n\t7.Lambda, Btu/lb\t\t997\t\t1027\t\t1027\n\t8.Feed, lb/hr\t\t\t22788\t\t50602\t\t13367\n\t9.Product, lb/hr\t\t13367\t\t40352\t\t12813\n\t10.Evaporation,lb/hr\t\t9421\t\t10250\t\t554\n\t11.Heat flow, Btu/hr\t\t11890000\t11020000\n\t12.UD,Btu/((hr)*(ft^2)*(°F))\t700\n\t13.A,ft^2\t\t\t683\t\t683\n\t14.Tubes, OD, in. and BWG\t1,16\t\t1,16\n\t15.Tube length, ft\t\t7\t\t7\n\t16.No. tubes\t\t\t432\t\t432\n\t17.Circulating pump. gpm\t3200 at 20 ft\t3200 at 20ft\t167 at 45 ft\n\t18.Apparent efficiency, prcnt\t54\t\t64\n\t18.BHP\t\t\t\t38\t\t35\t\t8.2\n\t20.Motor,hp\t\t\t40\t\t40\t\t10.0\n');\n", +"printf('\t------------------------------------------------------------------------------------\n');\n", +"V=8;\n", +"s=1.5;\n", +"G=V*s*62.5*3600;//lb/((hr)*(ft^2))\n", +"printf('\tG = V(s*62.5*3600) = %.1e lb/((hr)*(ft^2))\n',G);\n", +"UD=700;//Btu/((hr)*(ft^2)*(°F))\n", +"//Combining with a steam film coefficient of approximately 1500\n", +"printf('\tUC or UD = %.0f Btu/((hr)*(ft^2)*(°F))\n',UD);\n", +"printf('\n\t-------------------------------------------------------------------------------------');\n", +"printf('\n\ttx,°F\tw,lb/hr\t\tdelT\tUC\tA,ft^2\tat,flow area\tGcalc\t\tUcalc\n\t\t\t\t\t\t\tper pass, ft^2\n');\n", +"printf('\t-------------------------------------------------------------------------------------\n');\n", +"printf('\t251\t2970000\t\t25.4\t700\t670\t0.87\t\t3420000\n\t252\t2480000\t\t25.0\t700\t680\t0.88\t\t2820000\n\t252.5\t2290000\t\t24.7\t700\t685\t0.89\t\t2570000\t\t700\n\t253\t2120000\t\t24.5\t700\t695\t0.90\t\t2520000\n');\n", +"printf('\tThee gain per minute is %.0f gpm\n',gain);\n", +"printf('\n\t\t\t\tCAUSTIC EVAPORATION HEAT BALANCE\n');\n", +"printf('\t\t\t\t(Basis = 1ton/hr NaOH)\n');\n", +"printf('\t-------------------------------------------------------------------------------------\n');\n", +"printf('\t\tEFFECT\t\t\tBtu/hr\t\tEvaopration, lb/hr\n');\n", +"hi=10500*930*0.974;//Btu/hr\n", +"hl=18230*(246-150)*0.83;//Btu/hr\n", +"rh=hi-hl;//Btu/hr\n", +"hc=300000;//Btu/hr\n", +"hv=rh-hc;//Btu/hr\n", +"evv=hv/997;//lb/hr\n", +"printf('\t1.a.Heat in steam\t\t%.1e\n\t b.Heating liquor\t\t%.2e\n\t c.Resultant heat\t\t%.2ef\n\t d.Heat of concentrate\t\t%.0e\n\t e.Heat of vapors\t\t%.2e\t%.0f\n',hi,hl,rh,hc,hv,evv);\n", +"s1=1.35;\n", +"G1=V*s1*62.5*3600;//lb/((hr)*(ft^2))\n", +"printf('\n\tG = V(s*62.5*3600) = %.2e lb/((hr)*(ft^2))\n',G1);\n", +"UD1=700;//Btu/((hr)*(ft^2)*(°F))\n", +"//Using thermal characteristics for this solution\n", +"printf('\tUD = %.0f Btu/((hr)*(ft^2)*(°F))\n',UD1);\n", +"//As for effect I:\n", +"printf('\n\t-------------------------------------------------------------------------------------');\n", +"printf('\n\ttx,°F\tw,lb/hr\t\tdelT\tUC\tA,ft^2\tat,flow area\tGcalc\t\tUcalc\n\t\t\t\t\t\t\tper pass, ft^2\n');\n", +"printf('\t-------------------------------------------------------------------------------------\n');\n", +"printf('\t146\t2400000\t\t25.4\t700\t620\t0.80\t\t2790000\t\t700\n\t146.5\t2160000\t\t25.2\t700\t683\t0.89\t\t2430000\n');\n", +"//end" + ] + } +, +{ + "cell_type": "markdown", + "metadata": {}, + "source": [ + "## Example 14.7: heat_and_steam.sce" + ] + }, + { +"cell_type": "code", + "execution_count": null, + "metadata": { + "collapsed": true + }, + "outputs": [], +"source": [ +"printf('\texample 14.7\n');\n", +"printf('\tapproximate values are mentioned in the book \n');\n", +"M2=14300;//From fig.14.43 and heat balance above\n", +"M1=32200-14300;//From fig.14.43 and heat balance above\n", +"printf('\tM1 = %.0f lb\n',M1);\n", +"printf('\n\t\t\t\tEVAPORATOR SUMMARY\n');\n", +"printf('\t------------------------------------------------------------------------------------------------------------------------------\n');\n", +"printf('\tEffects\t\t\t\t\tStraight triple effect\t\t\t\tThermocompression\nt\t\t\t\t\t----------------------------------------------------------------------------------------------\n\t\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n');\n", +"printf('\t------------------------------------------------------------------------------------------------------------------------------\n');\n", +"printf('\tSteam flow, lb/hr\t\t22400\t\t\t\t\t\t17900\n\tSteam pressure, psi in.Hg\t20\t\t9\t\t2\t\t20\t\t9\t\t2\n\tSteam temp,°F\t\t\t258\t\t237\t\t217\t\t258\t\t237\t\t217\n\ttdelT,°F\t\t\t20\t\t18\t\t22\t\t20\t\t18\t\t22\n\tLiquor temp, °F\t\t\t238\t\t219\t\t195\t\t238\t\t219\t\t195\n\tBPR, °F\t\t\t\t1\t\t2\t\t3\t\t1\t\t2\t\t3\n\tVapor temp, °F\t\t\t237\t\t217\t\t192\t\t237\t\t215\t\t192\n\tVapor pressure, pis/in.Hg\t9\t\t2\t\t10\t\t9\t\t2\t\t10\n\tLambda, Btu/lb\t\t\t954\t\t965\t\t983\t\t954\t\t965\t\t983\n\tLiquor in, lb/hr\t\t100000\t\t79400\t\t56900\t\t109000\t\t70000\t\t52400\n\tLiqour out, lb/hr\t\t79400\t\t56900\t\t33300\t\t70000\t\t52400\t\t33300\n\tEvaporation,lb/hr\t\t20600\t\t22500\t\t23500\t\t30000\t\t17600\t\t19100\n\t°Brix(out)\t\t\t\t\t\t\t\t\t\t\t\t\t30\n\tCondenser water, gpm\t\t\t\t455\t\t\t\t\t\t365\n');\n", +"printf('\n\t\t\t\tHEAT BALANCE-STRAIGHT TRIPLE EFFECT\n\t\t\t\tCondenser water = 455 gpm\n');\n", +"printf('\t--------------------------------------------------------\n');\n", +"printf('\tEffect\t\t\tBtu/hr\t\tEvaporation,l/hr\n');\n", +"printf('\t--------------------------------------------------------\n');\n", +"sf=22400;//lb/hr\n", +"lc=100000;//lb/hr\n", +"t1=238;//°F\n", +"t2=230;//°F\n", +"his=sf*940*0.97;//Btu/hr\n", +"hlq=lc*(t1-t2)*0.92;//Btu/hr\n", +"hd=his-hlq;//Btu/hr\n", +"eva=(hd)/954;//lb/hr\n", +"l2d=lc-eva;\n", +"printf('\t1.a.Heat in steam\t%.2e\n\t b.Heating liquor\t%.2e\n\t c.Evaporation\t\t%.4e/954\t%.0f\n\t d.Liquor to 2d = %.0f',his,hlq,hd,eva,l2d);\n", +"//end" + ] + } +], +"metadata": { + "kernelspec": { + "display_name": "Scilab", + "language": "scilab", + "name": "scilab" + }, + "language_info": { + "file_extension": ".sce", + "help_links": [ + { + "text": "MetaKernel Magics", + "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md" + } + ], + "mimetype": "text/x-octave", + "name": "scilab", + "version": "0.7.1" + } + }, + "nbformat": 4, + "nbformat_minor": 0 +} |