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diff --git a/497/CH16/EX16.1/Chap16_Ex1.sce b/497/CH16/EX16.1/Chap16_Ex1.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-16, Example 1, Page 404

+//Title: Single-Stage Limestone Calciner

+//==========================================================================================================

+

+clear

+clc

+

+//INPUT

+T=1000;//Operating temperature of calciner in degree celcius

+deltaHr=1795;//Heat of reaction in kJ/kg

+M1=0.1;//Molecular weight of Calcium carbonate in kg/mol

+M2=0.056;//Molecular weight of CaO in kg/mol

+M3=0.044;//Molecular weight of Carbon dioxide  in kg/mol

+M4=0.029;//Molecular weight of Air in kg/mol

+M5=0.029;//Molecular weight of Combustion gas in kg/mol

+Cp1=1.13;//Specific heat of Calcium carbonate in kJ/kg K

+Cp2=0.88;//Specific heat of CaO in kJ/kg K

+Cp3=1.13;//Specific heat of Carbon dioxide in kJ/kg K

+Cp4=1.00;//Specific heat of Air in kJ/kg K

+Cp5=1.13;//Specific heat of Calcium carbonate in kJ/kg K

+Tf=20;//Temperature of feed in degree celcius

+ma=15;//Air required per kg of fuel in kg

+Hc=41800;//Net combustion heat of fuel in kJ/kg

+Tpi=20;//Initial temperature of solids in degree C

+Tgi=1000;//Initial temperature of gas in degree C

+

+//CALCULATION

+mc=1;//Based on 1 kg of Calcium carbonate

+B=(1/(Hc-(ma+mc)*Cp5*(T-Tpi)))*[M3*Cp3*(T-Tf)+M2*Cp2*(T-Tf)+deltaHr]//Fuel consumption(kg fuel/kg calcium carbonate)

+B1=B*M3/M2;//Fuel consumption(kg fuel/kg Cao)

+H=Hc*B1;//Heat required for calcination

+eta=deltaHr/(B*Hc);//Thermal efficiency

+

+//OUTPUT

+mprintf('\nFuel consumption:%f kg fuel/kg Cao',B1);

+mprintf('\nHeat requirement for calcination:%f kJ/kg Cao',H);

+mprintf('\nThermal efficiency:%f percentage',eta*100);

+

+//====================================END OF PROGRAM ======================================================
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diff --git a/497/CH16/EX16.2/Chap16_Ex2.sce b/497/CH16/EX16.2/Chap16_Ex2.sce
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index 000000000..c8a5c8864
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-16, Example 2, Page 405

+//Title: Multistage Limestone Calciner

+//==========================================================================================================

+

+clear

+clc

+

+//INPUT

+F=400;//Feed rate of Calcium carbonate in tons/day

+T=1000;//Operating temperature of calciner in degree celcius

+deltaHr=1795;//Heat of reaction in kJ/kg

+M1=0.1;//Molecular weight of Calcium carbonate in kg/mol

+M2=0.056;//Molecular weight of CaO in kg/mol

+M3=0.044;//Molecular weight of Carbon dioxide  in kg/mol

+M4=0.029;//Molecular weight of Air in kg/mol

+M5=0.029;//Molecular weight of Combustion gas in kg/mol

+Cp1=1.13;//Specific heat of Calcium carbonate in kJ/kg K

+Cp2=0.88;//Specific heat of CaO in kJ/kg K

+Cp3=1.13;//Specific heat of Carbon dioxide in kJ/kg K

+Cp4=1.00;//Specific heat of Air in kJ/kg K

+Cp5=1.17;//Specific heat of Combustion gas in kJ/kg K

+Tf=20;//Temperature of feed in degree celcius

+ma=15;//Air required per kg of fuel in kg

+uo=0.8;//Superficial gas velocity in m/s

+Hc=41800;//Net combustion heat of fuel in kJ/kg

+Tpi=20;//Initial temperature of solids in degree C

+Tgi=1000;//Initial temperature of gas in degree C

+rhoa=1.293;//Density of air in kg/m^3

+pi=3.14;

+

+//CALCULATION

+mc=1;//Based on 1 kg of Calcium carbonate

+Bguess=2;//Guess value of B

+function[fn]=solver_func(B)//Function defined for solving the system

+    phi=((ma+mc)*Cp5*B+(M3*Cp3))/Cp1;

+    T3=(Tpi+(phi+phi^2+phi^3)*Tgi)/(1+phi+phi^2+phi^3);

+    phiplus=30.6*B

+    Tr=(T+Tpi*phiplus)/(1+phiplus);

+    fn=Hc*B+Cp3*(T3-Tpi)+ma*B*Cp4*(Tr-20)-(ma+mc)*Cp5*(T-Tpi)-M3*Cp3*(T-Tpi)-M2*Cp2*(T-Tpi)-deltaHr;

+    //fn=(1/20800)*(2470-T3-13.34*(Tr-20));

+endfunction

+[B]=fsolve(Bguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou

+phi=((ma+mc)*Cp5*B+(M3*Cp3))/Cp1;

+//Temperature of various stages

+T1=(Tpi+(phi)*Tgi)/(1+phi);

+T2=(Tpi+(phi+phi^2)*Tgi)/(1+phi+phi^2);

+T3=(Tpi+(phi+phi^2+phi^3)*Tgi)/(1+phi+phi^2+phi^3);

+phiplus=30.6*B

+Tr=(T+Tpi*phiplus)/(1+phiplus);

+eta=deltaHr/(B*Hc);//Thermal efficiency

+H=B*Hc/M2;//Heat requirement

+//For lower heat recovery section

+Ql=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(Tr+273)));//Volumetric flow rate of gas in the lower heat recovery section

+dtl=sqrt(4/pi*Ql/uo);//Diameter of lower bed

+//For calcination section

+Qc=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T+273)));//Volumetric flow rate of gas in the calcination section

+dtc=sqrt(4/pi*Qc/uo);//Diameter of calcination section

+//For I stage

+Q1=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T1+273)));//Volumetric flow rate of gas in the I stage

+dt1=sqrt(4/pi*Q1/uo);//Diameter of I stage

+//For II stage

+Q2=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T2+273)));//Volumetric flow rate of gas in the II stage

+dt2=sqrt(4/pi*Q2/uo);//Diameter of II stage

+//For III stage

+Q3=(F*10^3/(24*3600))*B*ma/(rhoa*(273/(T3+273)));//Volumetric flow rate of gas in the III stage

+dt3=sqrt(4/pi*Q3/uo);//Diameter of III stage

+

+//OUTPUT

+printf('\nDiameter of lower bed:%fm',dtl);

+printf('\nDiameter of calcination section:%fm',dtc);

+printf('\nBed no.\t\t1\t2\t\t3');

+printf('\nDiameter(m)%f\t%f\t%f',dt1,dt2,dt3);

+

+//The value of diameter of each section is largely deviating from the values in the textbook. This is because the fuel consumption B have not been included in the energy balance equation. And the value of molecular weight is wrong by one decimal point.

+

+//====================================END OF PROGRAM ======================================================
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diff --git a/497/CH16/EX16.3/Chap16_Ex3.sce b/497/CH16/EX16.3/Chap16_Ex3.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-16, Example 3, Page 413

+//Title: Multistage Adsorber

+//==========================================================================================================

+

+clear

+clc

+

+//INPUT

+T=20;//Temeprature in degree C

+M=0.018;//Molecular weight of water in kg/mol

+Q=10;//Flow rate of dry air in m^3/s

+R=82.06E-6;//Universal gas constant

+pi=0.0001;//Initial moisture content in atm

+pj=0.01;//Final moisture content in atm

+

+//CALCULATION

+a=Q*(273+T)/273;//Term At*uo

+b=a*M/(R*(T+273));//Term C*At*uo

+//The value of slope can be found only by graphical mehtod. Hence it has been taken directly from the book(Page no.414,Fig.E3)

+m=10.2;

+Fo=b/m;//Flow rate of solids

+Q3=(b/Fo)*(pj-pi);//Moisture content of leaving solids

+

+//OUTPUT

+printf('\nMoisture content of leaving solids:%f kg H2O/kg dry solids',Q3);

+

+//====================================END OF PROGRAM ======================================================
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diff --git a/497/CH16/EX16.4/Chap16_Ex4.sce b/497/CH16/EX16.4/Chap16_Ex4.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-16, Example 4, Page 422

+//Title: Dryer Kinetics and Scale-up

+//==========================================================================================================

+

+clear

+clc

+

+//INPUT

+Qfi=0.20;//Initial moisture fraction

+Qfbar=0.04;//Average final moisture fraction

+rhos=2000;//Density of solid in kg/m^3

+Cps=0.84;//Specific heat of solids in kJ/kg K

+Fo=7.6E-4;//Flow rate of solids in kg/m^3

+Tsi=20;//Inital temperature of solids in degree C

+rhog=1;//Density of gas in kg/m^3

+Cpg=1;//Specific heat of gas in kJ/kg K

+uo=0.3;//Superficial gas velocity in m/s

+Tgi=200;//Initial temperature of gas in degee C

+L=2370;//Enthalpy of liquid in kJ/kg

+Cpl=4.2;//Specific heat of liquid in kJ/kg K

+dt=0.1;//Diameter of reactor in m

+Lm=0.1;//Length of fixed bed in m

+ephsilonm=0.45;//Void fraction of fixed bed

+pi=3.14;

+Fo1=1;//Feed rate for commercial-scale reactor in kg/s

+

+//CALCULATION

+//(a)Bed temperature

+Teguess=50;//Guess value of Te

+function[fn]=solver_func(Te)//Function defined for solving the system

+    fn=(pi/4)*dt^2*uo*rhog*Cpg*(Tgi-Te)-Fo*(Qfi-Qfbar)*[L+Cpl*(Te-Tsi)]-Fo*Cps*(Te-Tsi);

+endfunction

+[Te]=fsolve(Teguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(53) for Te

+

+//(b)Drying time for a particle

+xguess=2;//Guess value of x, ie term tou/tbar

+function[fn]=solver_func1(x)//Function defined for solving the system

+    fn=1-(Qfbar/Qfi)-(1-exp(-x))/x;

+endfunction

+[x]=fsolve(xguess,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(61) for x

+W=(pi/4)*dt^2*Lm*(1-ephsilonm)*rhos;//Weight of soilds in bed

+tbar=W/Fo;//Mean residence time of solids from Eqn.(59)

+tou=tbar*x;//Time for complete drying of a particle

+

+//(c)Commercial-scale dryer

+W1=Fo1*tbar;

+Atguess=5;//Guess value of area

+function[fn]=solver_func3(At)//Function defined for solving the system

+    fn=At*uo*rhog*Cpg*(Tgi-Te)-Fo1*(Qfi-Qfbar)*[L+Cpl*(Te-Tsi)]-Fo1*Cps*(Te-Tsi);

+endfunction

+[At]=fsolve(Atguess,solver_func3,1E-6);//Using inbuilt function fsolve for solving Eqn.(53) for At

+dt1=sqrt(4/pi*At);//Diameter of commercial-scale dryer

+Q1=At*uo*rhog;//Flow rate necessary for the operation

+

+//OUTPUT

+printf('\nBed temperature:%f degree C',Te);

+printf('\nTime for complete drying of particle:%fs',tou);

+printf('\nFlow rate of gas necessary for Commercial-scale dryer:%fkg/s',Q1);

+

+//====================================END OF PROGRAM ======================================================
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diff --git a/497/CH16/EX16.5/Chap16_Ex5.sce b/497/CH16/EX16.5/Chap16_Ex5.sce
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index 000000000..19b0b730b
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+++ b/497/CH16/EX16.5/Chap16_Ex5.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-16, Example 5, Page 425

+//Title: Solvent Recovery from Polymer Particles

+//==========================================================================================================

+

+clear

+clc

+

+//INPUT

+rhos=1600;//Density of solid in kg/m^3

+Cps=1.25;//Specific heat of solids in kJ/kg K

+Fo=0.5;//Flow rate of solids in kg/s

+Tsi=20;//Inital temperature of solids in degree C

+Qwi=1;//Initial moisture fraction in water

+Qwf=0.2;//Final moisture fraction in water

+Qhi=1.1;//Initial moisture fraction in heptane

+Qhf=0.1;//Final moisture fraction in heptane

+Tgi=240;//Initial temperature of gas in degee C

+Te=110;//Bed temperature in degree C

+ephsilonm=0.45;//Void fraction of fixed bed

+ephsilonf=0.75;//Void fraction of fluidized bed

+uo=0.6;//Superficial gas velocity in m/s

+di=0.08;//Diameter of tubes in m

+li=0.2;//Pitch for square arrangement

+hw=400;//Heat transfer coefficient in W/m^2 K

+Tc=238;//Temperature at which steam condenses in degree C

+//Specific heats in kJ/kg K

+Cwl=4.18;//Water liquid

+Cwv=1.92;//Water vapor

+Chl=2.05;//Heptane liquid

+Chv=1.67;//Heptane vapor

+//Latent heat of vaporization in kJ/kg

+Lw=2260;//Water

+Lh=326;//Heptane

+//Density of vapor in kg/m^3 at operating conditions

+rhow=0.56;//Water

+rhoh=3.1;//Heptane

+Lf=1.5;//Length of fixed bed in m

+t=140;//Half-life of heptane in s

+L=1.5;//Length of tubes in heat exchanger

+pi=3.14;

+

+//CALCULATION

+//(a) Dryer without Internals

+xw=(Qwi-Qwf)/(Qhi-Qhf);//Water-heptane weight ratio

+xv=((Qwi-Qwf)/18)/((Qhi-Qhf)/100);//Water-heptane volume ratio

+T=(Qwi-Qwf)/18+(Qhi-Qhf)/100;//Total volume

+rhogbar=((Qwi-Qwf)/18)/T*rhow+((Qhi-Qhf)/100)/T*rhoh;//Mean density of the vapor mixture

+Cpgbar=(((Qwi-Qwf)/18)/T)*rhow*Cwv+(((Qhi-Qhf)/100)/T)*rhoh*Cwv;//Mean specific heat of vapor mixture

+//Volumetric flow of recycle gas to the dryer in m^3/s from Eqn.(53)

+x=(Cpgbar*(Tgi-Te))^-1*[Fo*(Qwi-Qwf)*[Lw+Cwl*(Te-Tsi)]+Fo*(Qhi-Qhf)*[Lh+Chl*(Te-Tsi)]+Fo*(Cps*(Te-Tsi))];

+r=Fo*[(Qwi-Qwf)/rhow+(Qhi-Qhf)/rhoh};//Rate of formation of vapor in bed

+uo1=uo*(x/(x+r));//Superficial velocity just above the distributor

+At=x/uo1;//Cross-sectional area of bed

+dt=sqrt(4/pi*At);//Diameter of bed

+B=-log(Qwf/Qwi)/t;//Bed height from Eqn.(63)

+tbar=((Qhi/Qhf)-1)/B;//Mean residence time of solids

+W=Fo*tbar;//Weight of bed

+Lm=W/(At*(1-ephsilonm)*rhos);//Static bed height

+Lf=(Lm*(1-ephsilonm))/(1-ephsilonf);//Height of fluidized bed

+

+//(b) Dryer with internal heaters

+f=1/8;//Flow rate is 1/8th the flow rate of recirculation gas as in part (a)

+x1=f*x;//Volumetric flow of recycle gas to the dryer in m^3/s from Eqn.(53)

+uo2=uo*(x1/(x1+r));//Superficial velocity just above the distributor

+Abed=x1/uo2;//Cross-sectional area of bed

+q=[Fo*(Qwi-Qwf)*[Lw+Cwl*(Te-Tsi)]+Fo*(Qhi-Qhf)*[Lh+Chl*(Te-Tsi)]+Fo*(Cps*(Te-Tsi))]-Abed*uo2*Cpgbar*(Tgi-Te);//Heat to be added from energy balance of Eqn.(53)

+Aw=q*10^3/(hw*(Tc-Te));//Total surface area of heat exchanger tubes

+Lt=Aw/(pi*di);//Total length of tubes

+Nt=Lt/L;//Total number of tubes

+Atubes=Nt*(pi/4*di^2);//Total cross-sectional area of tubes

+Atotal=Abed+Atubes;//Total cross-sectional area of tube filled dryer

+d=sqrt(Atotal*pi/4);//Diameter of vessel

+li=sqrt(Atotal/Nt);//Pitch for square array of tubes

+

+//OUTPUT

+printf('\n\t\t\tBed diameter(m)\tRecycle vapor flow(m^3/s)');

+printf('\nWithout internal heater\t%f\t%f',dt,x);

+printf('\nWith heating tubes\t%f\t%f',d,x1);

+

+//====================================END OF PROGRAM ======================================================
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