initial commit / add all books

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+clc;

+clear;

+//Example 6.16

+bpr=40.6;        //[K]

+Cpf=1.88;       //[kJ/kg.K]

+Hf=214;     //[kJ/kg]

+H1=505;     //[kJ/kg]

+mf_dot=4536;    //[kg/h] of feed solution

+ic=0.2;      //Initial conc

+fc=0.5;      //Final concentration

+m1dot_dash=(ic/fc)*mf_dot       //Thisck liquor flow arte[kg/h]

+mv_dot=mf_dot-m1dot_dash        //[kg/H]

+Ts=388.5;        //Saturation temperature of steam in [K]

+bp=362.5        //b.P of solution in [K]

+lambda_s=2214;     //[kJ/kg]

+P=21.7;      //Vapor space in [kPa]

+Hv=2590.3;       //[kJ/kg]

+

+//Enthalpy balance over evaporator

+ms_dot=(m1dot_dash*H1+mv_dot*Hv-mf_dot*Hf)/lambda_s     //[kg/h

+printf("\nSteam consumption is %f kg/h\n",ms_dot);

+dT=Ts-bp        //[K]

+U=1560      //[W/sq m.K]

+Q=ms_dot*lambda_s           //[kJ/h]

+Q=Q*1000/3600               //[W]

+A=Q/(U*dT)      //[sq m]

+printf("\nHeat transfer area is %f sq m\n",A);

+

+//Calculations considering enthalpy of superheated vapour

+

+Hv=Hv+Cpf*bpr   //[kJ/kg]

+ms_dot=(m1dot_dash*H1+mv_dot*Hv-mf_dot*Hf)/lambda_s     //[kg/h]

+printf("\n Now,Steam consumption is %f kg/h\n",ms_dot);

+eco=mv_dot/ms_dot       //Steam economy

+printf("\nEconomy of evaporator %f\n",eco);

+Q=ms_dot*lambda_s       //[kJ/h]

+Q=Q*1000/3600           //[w]

+A2=Q/(U*dT)              //Area

+printf("\nNow,Area is %f\n",A);

+perc=(A2-A)*100/A           //%error in the heat transfer area 

+printf("\n If enthalpy of water vapour Hv were based on the saturated vapour at the pressure\nthe error introduced is only %f percent\n",perc);