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authorpriyanka2015-06-24 15:03:17 +0530
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-rwxr-xr-x497/CH15/EX15.1/Chap15_Ex1.sce25
-rwxr-xr-x497/CH15/EX15.2/Chap15_Ex2.sce59
-rwxr-xr-x497/CH15/EX15.3/Chap15_Ex3.sce36
-rwxr-xr-x497/CH15/EX15.4/Chap15_Ex4.sce55
-rwxr-xr-x497/CH15/EX15.5/Chap15_Ex5.sce58
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diff --git a/497/CH15/EX15.1/Chap15_Ex1.sce b/497/CH15/EX15.1/Chap15_Ex1.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-15, Example 1, Page 369
+//Title: Circulation Rate when Deactivation Controls
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+thalf=1;//Half life of catalyst in s
+F=960;//Feed rate of oil in tons/day
+W=50;//Weight of the bed in tons
+a=0.5;//Activity after time equal to half life
+abar=0.01;//Average activity of the catalyst
+
+//CALCULATION
+Ka=-log(a)/thalf;//Rate constant is s^-1, assuming I order kinetics from Eqn.(12)
+Fs=Ka*W*abar/(1-abar);//Circulation rate of solids from Eqn.(16)
+x=(Fs*60*60*24)/F;//Circulation rate per feed of oil
+
+//OUTPUT
+mprintf('\nSolid recirculation per feed of oil =%ftons of solid circulated/ton feed oil',x);
+
+//====================================END OF PROGRAM ====================================================== \ No newline at end of file
diff --git a/497/CH15/EX15.2/Chap15_Ex2.sce b/497/CH15/EX15.2/Chap15_Ex2.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-15, Example 2, Page 370
+//Title: Circulation Rate when Heat Duty Controls
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+deltaHr1=1260;//Enthalpy change during endothermic reaction in kJ/kg
+deltaHr2=-33900;//Enthal[y change during exothermic reaction in kJ/kg
+H1=703;//Enthalpy of feed oil in kJ/kg
+T1=260;//Temperature of feed oil in degree celcius
+H3=1419;//Enthalpy of cracked product in kJ/kg
+T3=500;//Temperature of cracked product in degree celcius
+Ta=20;//Temperature of entering air in degree celcius
+Cpa=1.09;//Specific heat of entering air in kJ/kg K
+Cpf=1.05;//Specific heat of flue gases in kJ/kg K
+Cps=1.01;//Specific heat of solids in kJ/kg K
+Cpv=3.01;//Specific heat of vaporized feed in kJ/kg K
+T4=[520;540;560;580;600;620;640;660];//Temperature of flue gas in degree celcius
+V=22.4;//Volume of 1 mole of Carbon dioxide gas in N-m^3
+M=12;//Molecular weight of carbon in kg
+rho=1.293;//Density of carbon dioxide gas in kg/N-m^3
+xa=0.21;//Mass fraction of oxygen in air
+betac=0.07;//Mass fraction of carbon
+
+//CALCULATION
+n=length(T4);
+i=1;
+
+x2min=betac*(V*rho/(M*xa));//Minimum amount of air required for complete combustion
+while i<=n
+ x1(i)=(deltaHr1+0.93*H3-H1)/(Cps*(T4(i)-T3));//Fs/F1 by simplifying the overall energy balance
+ x2(i)=[(0.07*(-deltaHr2)-(deltaHr1+0.93*H3-H1))/(Cpf*(T4(i)-Ta))]-0.07;//F2/F1 by simplifying the energy balance for regenerator
+ if x2(i)>x2min then excess_air(i)=(x2(i)-x2min)/x2min; //Excess air used
+ else excess_air(i)=0;
+ end
+ i=i+1;
+end
+
+//OUTPUT
+printf('\nT4(degree celcius)');
+printf('\tFs/F1');
+printf('\t\tF2/F1');
+printf('\t\tExcess air(percentage)');
+i=1;
+while i<=n
+ mprintf('\n%f',T4(i));
+ mprintf('\t\t%f',x1(i));
+ mprintf('\t%f',x2(i));
+ mprintf('\t%f',excess_air(i)*100);
+ i=i+1;
+end
+
+//Disclaimer: The values of F2/F1 obtained by manual calculation has close correspondance to the ones obtained as the output, whereas it deviates largely from the values given in textbook.
+
+//====================================END OF PROGRAM ====================================================== \ No newline at end of file
diff --git a/497/CH15/EX15.3/Chap15_Ex3.sce b/497/CH15/EX15.3/Chap15_Ex3.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-15, Example 3, Page 379
+//Title: Aeration of Fine Particle Downcomer
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Fs=100;//Solid flowrate in kg/s
+ephsilon1=0.55;
+ephsilon2=0.5;
+p1=120;//Pressure at upper level in kPa
+rhos=1000;//Density of solid in kg/m^3
+rhog=1;//Density of gas in kg/m^3
+gc=1;//Conversion factor
+g=9.81;//Acceleration due to gravity in m/s^2
+di=0.34;//Diameter of downcomer in m
+pi=3.14;
+
+//CALCULATION
+x=(ephsilon1/ephsilon2)*((1-ephsilon2)/(1-ephsilon1));//To find pressure at lower level using Eqn.(30)
+p2=x*p1;//Pressure at lower level using Eqn.(30)
+deltap=p2-p1;
+ephsilonbar=0.5*(ephsilon1+ephsilon2);
+deltah=(deltap*10^3*gc)/(rhos*(1-ephsilonbar)*g);//Static head height from Eqn.(28)
+At=0.25*pi*di^2;//Area of downcomer
+Gs=Fs/At;//Flux of solids in downcomer
+Gg=Gs*(ephsilon1/(1-ephsilon1))*(rhog/rhos)*(x-1);//Required gas aeration rate from Eqn.(31)
+Fg=Gg*At;//Flow rate of gas required
+
+//OUTPUT
+mprintf('\nThe required flow rate of gas required for location of %fm below downcomer is %fkg/s',deltah,Fg);
+
+//====================================END OF PROGRAM ====================================================== \ No newline at end of file
diff --git a/497/CH15/EX15.4/Chap15_Ex4.sce b/497/CH15/EX15.4/Chap15_Ex4.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-15, Example 4, Page 380
+//Title: Circulation in Side-by-Side Beds
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Fs=600;//Solid circulation rate in kg/s
+dpbar=60;//Mean size of solids in micrometer
+pA=120;//Pressure in vessel A in kPa
+pB=180;//Pressure in vessel B in kPa
+LfA=8;//Bed height in vessel A in m
+LfB=8;//Bed height in vessel B i m
+//Bulk densities in kg/m^3
+rho12=100;
+rho34=400;
+rho45=550;
+rho67=200;
+rho78=200;
+rho910=400;
+rho1011=400;
+rho1112=550;
+rho13=100;
+deltapdA=7;//Pressure drop across the distributor in regenerator in kPa
+deltapdB=8;//Pressure drop across the distributor in reactor in kPa
+deltap12=(9+4);//Friction loss and pressure difference required to accelerate the solids in transfer lines in kPa
+deltap78=(15+3);//Friction loss and pressure difference required to accelerate the solids in transfer lines in kPa
+deltap45=20;//Friction loss across the reactor's stripper downcomer in kPa
+deltap1112=4;//Friction loss across the regenerator's downcomer in kPa
+deltapvA=5;//Pressure drop assigned for the control valve in regenerator in kPa
+deltapvB=15;//Pressure drop assigned for the control valve in reactor in kPa
+deltah12=15;//Height of the riser in m
+deltah86=30;//Height of the riser in m
+deltah1011=7;//Height difference h10-h11 in m
+g=9.81;//Acceleration due to gravity in m/s^2
+gc=1;//Conversion factor
+pi=3.14;
+
+//CALCULATION
+Gs=900;//From Fig.(8), to find dt
+dt=sqrt((4/pi)*Fs/Gs);//Diameter of the downcomer
+//Height of downcomer A from Eqn.(7)
+deltahA=(1/(rho1112*g))*[(pB-pA)*gc*(10^3)+(deltap12+deltapdB+deltap1112+deltapvA)*gc*10^3-rho12*g*(-deltah12)-rho34*g*(-LfB)-rho1011*g*deltah1011];
+//Height of downcomer B from Eqn.(8)
+deltahB=(1/(rho45*g))*[-(pB-pA)*gc*10^3+(deltap45+deltapvB+deltap78+deltapdA)*gc*10^3+rho78*g*deltah86+rho910*g*LfA];
+
+//OUTPUT
+printf('\nHeight of downcomer for:');
+mprintf('\n\tRegenerator:%fm',deltahA);
+mprintf('\n\tReactor:%fm',deltahB);
+
+//====================================END OF PROGRAM ====================================================== \ No newline at end of file
diff --git a/497/CH15/EX15.5/Chap15_Ex5.sce b/497/CH15/EX15.5/Chap15_Ex5.sce
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+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-15, Example 5, Page 381
+//Title: Steam Seal of a Coarse Particle Downcomer
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dp=10^-3;//Particle diameter in m
+dt=0.8;//Diameter of reactor in m
+us=0.15;//Descend velocityo of solids in m/s
+L=15;//Length of downcomer
+deltap1=300;//Pressure in lower vessel in kPa
+deltap2=240;//Pressure in upper vessel in kPa
+phis=0.8;//Sphericity of solids
+ephsilonm=0.45;//Void fraction of bed
+myu=4E-5;//Viscosity of gas in kg/m s
+rhogl=2;//Density of gas in lower vessel in kg/m^3
+rhogu=1.6;//Density of gas in upper vessel in kg/m^3
+rhogbar=0.5*(rhogl+rhogu);//Average density in kg/m^3
+gc=1;//Conversion factor
+
+//CALCULATION
+//(a)Without steam seal
+deltapfr=(deltap1-deltap2)*10^3;//Frictional pressure drop between two levels in Pa
+deluguess=50;//Guess value of deltau
+function[fn]=solver_func(delu)//Function defined for solving the system
+ fn=(deltapfr*gc/L)-(150*(1-ephsilonm)^2*myu*delu/(ephsilonm^2*(phis*dp)^2))-(1.75*(1-ephsilonm)*rhogbar*delu^2/(ephsilonm*phis*dp));
+endfunction
+[delu]=fsolve(deluguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(25) for deltau
+uo=(delu-us)*ephsilonm;//Superficial gas velocity
+Fg=rhogbar*uo*(pi/4)*dt^2;//Flow rate of gs up the tube
+
+//(c)With steam seal
+//For section 1 to 3
+L1=10;
+deluguess1=50;//Guess value of deltau
+function[fn]=solver_func1(delu1)//Function defined for solving the system
+ fn=(deltapfr*gc/L1)-(150*(1-ephsilonm)^2*myu*delu1/(ephsilonm^2*(phis*dp)^2))-(1.75*(1-ephsilonm)*rhogbar*delu1^2/(ephsilonm*phis*dp));
+endfunction
+[delu1]=fsolve(deluguess1,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(25) for deltau
+uou=(delu1-us)*ephsilonm;//Upward superficial gas velocity
+Fgu=rhogbar*uou*(pi/4)*dt^2;//Upward flow rate of gs up the tube
+//For section 3 to 2
+ugd=0.15;//Downward velocity of gas
+uod=ugd*ephsilonm;//Downward superficial gas velocity
+Fgd=rhogbar*uod*(pi/4)*dt^2;//Downward flow rate of gas up the tube
+Fgt=Fgu+Fgd;//Total flow rate of gas
+
+//OUTPUT
+printf('\nWithout steam seal');
+printf('\n\tFlow rate of gas up the tube:%fkg/s',Fg);
+printf('\nWith steam seal');
+printf('\n\tTotal flow rate of gas:%fkg/s',Fgt);
+
+//====================================END OF PROGRAM ====================================================== \ No newline at end of file