path: root/Process_Heat_Transfer_by_D_Q_Kern/14-Evopartion.ipynb

{
"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"
   ]
   }
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		   "language": "scilab",
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			{
			 "text": "MetaKernel Magics",
			 "url": "https://github.com/calysto/metakernel/blob/master/metakernel/magics/README.md"
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