initial commit / add all books

3 files changed, 286 insertions, 0 deletions

diff --git a/497/CH17/EX17.1/Chap17_Ex1.sce b/497/CH17/EX17.1/Chap17_Ex1.sce
new file mode 100755
index 000000000..280e306ee
--- /dev/null
+++ b/497/CH17/EX17.1/Chap17_Ex1.sce
@@ -0,0 +1,110 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-17, Example 1, Page 434

+//Title: Reactor Development Program

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

+

+clear

+clc

+

+//INPUT

+dt=[0.081;0.205;3.6];//Reactor diameter for the three reactors in m

+dte=[0.04;0.12;0.70];//Equivalent diameters for the three reactors in m

+db=[0.05;0.057;0.07];//Estimated bubble size in the three reactors in m

+Kr1=1.3889;//Kinetic constant for Reaction 1 in s^-1

+Kr2=0.6111;//Kinetic constant for Reaction 2 in s^-1

+Kr3=0.022;//Kinetic constant for Reaction 3 in s^-1

+dp=60;//Particle size in micrometer

+ephsilonm=0.50;//Void fraction of fixed bed

+ephsilonmf=0.55;//Void fraction at minimum fluidized condition

+umf=0.006;////Velocity at minimum fluidization condition in m/s

+D=2E-5;//Diffusion coefficient of gas in m^2/s

+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase

+uo=0.2;//Superficial gas velocity in m/s

+XA=0.9;//Conversion

+g=9.81;//Acceleration due to gravity in square m/s^2

+

+//CALCULATION

+Kr12=Kr1+Kr2;

+n=length(dt);

+i=1;

+while i<=n

+    //Preliminary Calcualtions

+    ubr(i)=0.711*(g*db(i))^0.5;//Rise velocity of bubble from Eqn.(6.7)

+    ub(i)=1.55*{(uo-umf)+14.1*(db(i)+0.005)}*dte(i)^0.32+ubr(i);//Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)

+    delta(i)=uo/ub(i);//Fraction of bed in bubbles from Eqn.(6.29)

+    ephsilonf(i)=1-(1-delta(i))*(1-ephsilonmf);//Void fraction of fixed bed from Eqn.(6.20)

+    fw=0.6;//Wake volume to bubble volume from Fig.(5.8)

+    gammac(i)=(1-ephsilonmf)*((3/(ubr(i)*ephsilonmf/umf-1))+fw);//Volume of solids in cloud to that of the bubble from Eqn.(6.36)

+    gammae(i)=((1-ephsilonmf)*((1-delta(i))/delta(i)))-gammab-gammac(i);//Volume of solids in emulsion to that of the bubble from Eqn.(6.35)

+    Kbc(i)=4.5*(umf/db(i))+5.85*((D^0.5*g^0.25)/db(i)^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)

+    Kce(i)=6.77*((D*ephsilonmf*0.711*(g*db(i))^0.5)/db(i)^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)

+    //Effective rate constant from Eqn.(12.32)

+    Kf12(i)=(gammab*Kr12+1/((1/Kbc(i))+(1/(gammac(i)*Kr12+1/((1/Kce(i))+(1/(gammae(i)*Kr12)))))))*(delta(i)/(1-ephsilonf(i)));

+    //Rate of reaction 2 for fluidized bed from Eqn.(12.14)

+    Kf3(i)=(gammab*Kr3+1/((1/Kbc(i))+(1/(gammac(i)*Kr3+1/((1/Kce(i))+(1/(gammae(i)*Kr3)))))))*(delta(i)/(1-ephsilonf(i)));

+    //Rate of raection with respect to A from Eqn.(12.35)

+    KfA(i)=[[Kbc(i)*Kce(i)/gammac(i)^2+(Kr12+Kce(i)/gammac(i)+Kce(i)/gammae(i))*(Kr3+Kce(i)/gammac(i)+Kce(i)/gammae(i))]*delta(i)*Kbc(i)*Kr12*Kr3/(1-ephsilonf(i))]    /[[(Kr12+Kbc(i)/gammac(i))*(Kr12+Kce(i)/gammae(i))+Kr12*Kce(i)/gammac(i)]*[(Kr3+Kbc(i)/gammac(i))*(Kr3+Kce(i)/gammae(i))+Kr3*Kce(i)/gammac(i)]];

+    KfAR(i)=((Kr1/Kr12)*Kf12(i))-KfA(i);//Rate of reaction from Eqn.(12.34)

+    KfAR1(i)=((Kr1/Kr12)*Kf12(i));//Since KfA is small

+    

+    //(b)Relate Selectivity with conversion in three reactors

+    x=-log(1-XA);//The term Kf12*tou in Eqn.(12.26)

+    tou(i)=x/Kf12(i);//Residence time from Eqn.(12.26)

+    y(i)=(KfAR1(i)/(Kf3(i)-Kf12(i)))*(exp(-x)-exp(-tou(i)*Kf3(i)));//CR/CAi from Eqn.(12.27)

+    SR(i)=y(i)/XA;//Selectivity of R

+    

+    //(c)Relate exit composition to space time

+    tou1=5;//Space time in s

+    XA1(i)=1-exp(-Kf12(i)*tou1);//Conversion from Eqn.(12.26)

+    y1(i)=((KfAR1(i)/(Kf12(i)-Kf3(i)))*[exp(-Kf3(i)*tou1)-exp(-Kf12(i)*tou1)]);//CR/CAi R from Eqn.(12.27)

+    

+    //(d)Calculate height of bed needed to maximize production

+    y2(i)=(KfAR1(i)/Kf12(i))*(Kf12(i)/Kf3(i))^(Kf3(i)/(Kf3(i)-Kf12(i)));//CRmax/CAi R from Eqn.(12.37)

+    tou2(i)=log(Kf3(i)/Kf12(i))/(Kf3(i)-Kf12(i));//Space time from Eqn.(38)

+    Lf(i)=(uo/(1-ephsilonf(i)))*tou2(i);//Length of bed at fully fluidized condition from Eqn.(12.5)

+    Lm(i)=Lf(i)*(1-ephsilonf(i))/(1-ephsilonm);//Length of bed when settled

+    XA2(i)=1-exp(-Kf12(i)*tou2(i));//Conversion from Eqn.(12.26)

+    i=i+1;

+end

+

+//OUTPUT

+printf('\nLet Laboratory, Pilot plant, Semicommercial unit be Reactor 1,2 & 3 respectively'); 

+printf('\n(a)Relation between effective rate constant(Kf12) to the gas flow rate(uo)');

+printf('\n\tReactor No.\tKf12(s^-1)\tuo(m/s)');

+i=1;

+while i<=n

+     mprintf('\n\t%1.0f',i);

+     mprintf('\t\t%f',Kf12(i));

+     mprintf('\t%f',uo);

+     i=i+1;

+end

+printf('\n(b)Relation between selectivity with conversion');

+printf('\n\tReactor No.\tKf12(s^-1)\tSR(mol R formed/mol A reacted)');

+i=1;

+while i<=n

+     mprintf('\n\t%1.0f',i);

+     mprintf('\t\t%f',Kf12(i));

+     mprintf('\t%f',SR(i));

+     i=i+1;

+end

+printf('\n(c)Relation between exit compostion and space time');

+printf('\n\tReactor No.\tXA\t\tCR/CAi');

+i=1;

+while i<=n

+     mprintf('\n\t%1.0f',i);

+     mprintf('\t\t%f',XA1(i));

+     mprintf('\t%f',y1(i));

+     i=i+1;

+end

+printf('\n(d)Height of bed needed to maximize the production of acrylonitrile');

+printf('\n\tReactor No.\tLm(m)\t\tXA');

+i=1;

+while i<=n

+     mprintf('\n\t%1.0f',i);

+     mprintf('\t\t%f',Lm(i));

+     mprintf('\t%f',XA2(i));

+     i=i+1;

+end

+

+//====================================END OF PROGRAM ======================================================
\ No newline at end of file
diff --git a/497/CH17/EX17.2/Chap17_Ex2.sce b/497/CH17/EX17.2/Chap17_Ex2.sce
new file mode 100755
index 000000000..935f6e6d0
--- /dev/null
+++ b/497/CH17/EX17.2/Chap17_Ex2.sce
@@ -0,0 +1,65 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-17, Example 2, Page 438

+//Title: Design of a Commercial Acrylonitrile Reactor

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

+

+clear

+clc

+

+//INPUT

+deltaHr=5.15E8;//Heat of reaction in J/k mol

+W=5E4;//Weight of acrylonitirle produced per 334-day year in tonnes

+db=0.07;//Estimated bubble size in m

+dte=0.7;//Equivalent diameter in m

+Kf12=0.35;//Effective rate constant in s^-1 from Example 1

+dp=60;//Particle size in micrometer

+ephsilonm=0.50;//Void fraction of fixed bed

+ephsilonmf=0.55;//Void fraction at minimum fluidized condition

+T=460;//Temperature in reactor in degree C

+Pr=2.5;//Pressure inside reactor in bar

+//Feed gas composition

+x1=1;//Propylene

+x2=1.1;//Ammonia

+x3=11;//Air

+do1=0.08;//OD of heat exchanger tubes in m\

+L=7;//Length of tubes in m

+ho=300;//Outside heat transfer coefficient in W/m^2 K

+hi=1800;//Inside heat transfer coefficient in W/m^2 K

+Tc=253.4;//Temperature of coolant in degree C

+pi=3.14;

+

+//CALCULATION

+//Preliminary calculation

+uo=0.46;//Superficial gas velocity from Fig.E1(a) for the value of Kf12 & db

+tou=8;//Space time from Fig.E2(b) for highest concentraion of product R

+Lm=uo*tou/(1-ephsilonm);

+y=0.58;//CR/CAi from Fig.E1(c) for the value of tou & Kf12

+XA=0.95//From Fig.E1(c) for the value of tou & Kf12

+SR=y/XA;//Selectivity of R

+

+//Cross-sectional area of the reactor

+P=W*10^3/(334*24*3600);//Production rate of acrylonitrile

+F=(P/0.053)/(SR*XA/0.042);//Feed rate of propylene

+V=((F*22.4*(T+273)*(x1+x2+x3))/(42*273*Pr));

+At=V/uo;//Cross-sectional area of reactor needed for the fluidized bed

+

+//Heat exchanger calculation

+q=F*XA*deltaHr/42;//Rate of heat liberation in the reactor

+U=(ho^-1+hi^-1)^-1;//Overall heat transfer coefficient

+deltaT=T-Tc;//Driving force for heat transfer

+Aw=q/(U*deltaT);//Heat exchanger area required to remove q

+Nt=Aw/(pi*do1*L);

+li1=(At/Nt)^0.5;//Pitch for square pitch arrangement

+dte1=4*[li1^2-(pi/4)*do1^2]/(pi*do1);

+if dte1>dte then li=(pi/4*dte*do1+pi/4*do1^2)^0.5;//Pitch if we add dummy tubes

+end

+f=li^2-pi/4*do1^2;//Fraction of bed cross section taken up by tubes

+dt1=sqrt(4/pi*At/(1-f));//Reactor diameter including all its tubes

+

+//OUTPUT

+printf('\nSuperficial gas velocity=%fm/s',uo);

+printf('\nNo. of %1.0fm tubes required=%1.0f',L,Nt);

+printf('\nReactor diameter=%fm',dt1);

+

+//====================================END OF PROGRAM ======================================================
\ No newline at end of file
diff --git a/497/CH17/EX17.3/Chap17_Ex3.sce b/497/CH17/EX17.3/Chap17_Ex3.sce
new file mode 100755
index 000000000..827816aa3
--- /dev/null
+++ b/497/CH17/EX17.3/Chap17_Ex3.sce
@@ -0,0 +1,111 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491

+

+//Chapter-17, Example 3, Page 444

+//Title: Reactor-Regenerator with Circulating Catalyst: Catalytic Cracking

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

+

+clear

+clc

+

+//INPUT

+db=0.08;//Estimated bubble size in m

+dte=2;//Equivalent diameter in m

+F1=55.6;//Feed rate of oil in kg/s

+XA=0.63;//Conversion

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

+T1=500;//Temperature of reactor in degree C

+T2=580;//Temperature of regenerator in degree C

+Fs=F1*23.3;//Solid circulation rate from Ex.(15.2)

+rhos=1200;//Density of catalyst in kg/m^3

+dpbar=60;//Average particle size in micrometer

+ephsilonm=0.50;//Void fraction of fixed bed

+ephsilonmf=0.55;//Void fraction at minimum fluidized condition

+umf=0.006;////Velocity at minimum fluidization condition in m/s

+dt=8;//Diameter of reactor in m

+D=2E-5;//Diffusion coefficient of gas in m^2/s

+Kr=8.6;//Rate constant for reaction at 500 degree C in s^-1

+Ka1=0.06;//Rate constant for deactivatiion at 500 degree C in s^-1

+Ka2=0.012;//Rate constant for regeneration at 580 degree C in s^-1

+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase

+g=9.81;//Acceleration due to gravity in square m/s^2

+pi=3.14;

+

+//CALCULATION

+//Parameters for the fluidized reactor

+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)

+ub=1.55*{(uo-umf)+14.1*(db+0.005)}*dte^0.32+ubr;//Bubble velocity for Geldart A particles from Equation from Eqn.(6.11)

+delta=uo/ub;//Fraction of bed in bubbles from Eqn.(6.29)

+ephsilonf=1-(1-delta)*(1-ephsilonmf);//Void fraction of fixed bed from Eqn.(6.20)

+fw=0.6;//Wake volume to bubble volume from Fig.(5.8)

+gammac=(1-ephsilonmf)*((3/(ubr*ephsilonmf/umf-1))+fw);//Volume of solids in cloud to that of the bubble from Eqn.(6.36)

+gammae=((1-ephsilonmf)*((1-delta)/delta))-gammab-gammac;//Volume of solids in emulsion to that of the bubble from Eqn.(6.35)

+Kbc=4.5*(umf/db)+5.85*((D^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)

+Kce=6.77*((D*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)

+

+//Bed height versus catalyst activity in reactor

+a1bar=0.07;//Guess value for average activity in reactor

+x=Kr*a1bar;//Value of Kra1 to be used in the following equation

+Kf=(gammab*x+1/((1/Kbc)+(1/(gammac*x+1/((1/Kce)+(1/(gammae*x)))))))*(delta/(1-ephsilonf));//Effective rate constant from Eqn.(12.14)

+tou=-log(1-XA)/Kf;//Space time from Eqn.(12.16)

+Lm=tou*uo/(1-ephsilonm);//Length of fixed bed for guess value of a1bar

+a1bar1=[0.0233;0.0465;0.0698;0.0930;0.116;0.140];//Various activity values to find Lm

+n=length(a1bar1);

+i=1;

+while i<=n

+    x1(i)=Kr*a1bar1(i);

+    Kf1(i)=(gammab*x1(i)+1/((1/Kbc)+(1/(gammac*x1(i)+1/((1/Kce)+(1/(gammae*x1(i))))))))*(delta/(1-ephsilonf));//Effective rate constant from Eqn.(12.14)

+    tou1(i)=-log(1-XA)/Kf1(i);//Space time from Eqn.(12.16)

+    Lm1(i)=tou1(i)*uo/(1-ephsilonm);//Length of fixed bed for guess value of a1bar...Condition (i)

+    i=i+1;

+end

+

+//Find the optimum size ratio for various a1bar

+Lm=[5;6;7;8;10;12];

+m=length(Lm);

+i=1;

+while i<=m

+    W1(i)=(pi/4)*dt^2*rhos*(1-ephsilonm)*Lm(i);//Bed weight

+    t1bar(i)=W1(i)/Fs;//Mean residence time of solids in reactor

+    t2bar(i)=t1bar(i)*(Ka1/Ka2)^0.5;//Mean residence time of soilds at optimum from Eqn.(16)

+    a1bar2(i)=(Ka2*t2bar(i))/(Ka1*t1bar(i)+Ka1*t1bar(i)*Ka2*t2bar(i)+Ka2*t2bar(i));//From Eqn.(15)...Condition (ii)

+    i=i+1;

+end

+

+//Final design values

+Lm4=7.3;//For satisfying condition (i) & (ii)

+a1bar3=0.0744;//By interpolation

+x2=a1bar3*Kr;

+W11=(pi/4)*dt^2*rhos*(1-ephsilonm)*Lm4;//Bed weight for reactor

+t1bar1=W11/Fs;//Mean residence time of solids in reactor

+a2bar=(1+Ka1*t1bar1)*a1bar3;//Average activity in regenrator from Eqn.(10)

+t2bar1=t1bar1*(Ka1/Ka2)^0.5;//Mean residence time of solids in regenerator from Eqn.(16)

+W2=W11*(t2bar1/t1bar1);//Bed weight for regenerator

+dt2=dt*(W2/W11)^0.5;//Diameter of regenerator assuming same static bed height for reactor and regerator

+

+//OUTPUT

+printf('\nBed height versus catalyst activity in reactor');

+printf('\n\tAverage activity');

+printf('\tLength of fixed bed(m)');

+i=1;

+while i<=n

+    mprintf('\n\t%f',a1bar1(i));

+    mprintf('\t\t%f',Lm1(i));

+    i=i+1;

+end

+printf('\nOptimum size ratio for various activity in reactor');

+printf('\n\tLength of fixed bed(m)');

+printf('\tAverage activity');

+i=1;

+while i<=m

+    mprintf('\n\t%f',Lm(i));

+    mprintf('\t\t%f',a1bar2(i));

+    i=i+1;

+end

+printf('\nFinal design values');

+printf('\n\tDiameter of reactor(m):%f',dt);

+printf('\n\tBed weight for reactor(tons):%f',W11/10^3);

+printf('\n\tBed weight for regenerator(tons):%f',W2/10^3);

+printf('\n\tDiameter of regenerator(m):%f',dt2);

+printf('\n\tSolid circulation rate(tons/hr):%f',Fs*3.6);

+

+//====================================END OF PROGRAM ======================================================
\ No newline at end of file