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diff --git a/497/CH10/EX10.1/Chap10_Ex1.sce b/497/CH10/EX10.1/Chap10_Ex1.sce
new file mode 100755
index 000000000..95be23a0e
--- /dev/null
+++ b/497/CH10/EX10.1/Chap10_Ex1.sce
@@ -0,0 +1,60 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-10, Example 1, Page 253
+//Title: Estimate Interchange Coefficients in Bubbling Beds
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+umf=[0.01;0.045];//Velocity at minimum fluidization condition in m/s
+ephsilonmf=[0.5;0.5];//Void fraction at minimum fluidization condition
+D=[2E-5;7E-5];//Diffusion coefficient of gas in m^2/s
+g=9.81;//Acceleration due to gravity in m/s^2
+
+//CALCULATION
+db=[5;10;15;20];
+n=length(umf);
+m=length(db)'
+for i = 1:n
+    for j = 1:m
+            Kbc(i,j)=4.5*(umf(i)/db(j))+5.85*((D(i)^0.5*g^0.25)/db(j)^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(27)
+            Kce(i,j)=6.77*((D(i)*ephsilonmf(i)*0.711*(g*db(j))^0.5)/db(j)^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(34)
+            Kbe(i,j)=(Kbc(i,j)*Kce(i,j))/(Kbc(i,j)+Kce(i,j));//Gas interchange coefficient between bubble and emulsion from Eqn.(14)
+    end;
+end
+
+//OUTPUT
+i=1;
+j=1;
+k=1;
+while k<=m*n
+    printf('\n\t\tKbc for fine particles and He');
+    printf('\tKbc for coarse particles and ozone');
+    printf('\tKbe for fine particles and He');
+    printf('\tKbe for coarse particles and ozone');
+    while j<=m
+        mprintf('\ndb=%fm',db(j)*10^-2);
+        while i<=n
+            mprintf('\t%f',Kbc(k));
+            mprintf('\t\t\t%f',Kbe(k));
+            i=i+1;   
+            k=k+1;
+            printf('\t\t\t');
+        end
+    i=1;
+    j=j+1;
+    end
+end
+Kbe=Kbe';
+Kbc=Kbc';
+plot2d("ll",db,[Kbc Kbe]);
+xtitle('Plot of Kbc,Kbe vs db','db',['Kbc','Kbe']);
+printf('\nComparing the points with the plot of Kbc,Kbe vs db in Fig.(12), we can conlcude the following:');
+printf('\nKbc for fine particles and helium: line 2 in Fig.(12)');
+printf('\nKbc for coarser particles and ozone: line 3 in Fig.(12)');
+printf('\nKbe for fine particles and helium: line 4 in Fig.(12)');
+printf('\nKbe for coarser particles and ozone: line 5 in Fig.(12)');
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH10/EX10.1/Chap10_Ex1_R.jpg b/497/CH10/EX10.1/Chap10_Ex1_R.jpg
new file mode 100755
index 000000000..e71881544
--- /dev/null
+++ b/497/CH10/EX10.1/Chap10_Ex1_R.jpg
diff --git a/497/CH10/EX10.2/Chap10_Ex2.sce b/497/CH10/EX10.2/Chap10_Ex2.sce
new file mode 100755
index 000000000..bb6414d36
--- /dev/null
+++ b/497/CH10/EX10.2/Chap10_Ex2.sce
@@ -0,0 +1,44 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-10, Example 2, Page 254
+//Title: Compare the Relative Importance of Kbc and Kce
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+D=0.69;//Diffusion coefficient of gas in cm^2/s
+umf=1.0;//Velocity at minimum fluidization condition in cm/s
+ephsilonmf=0.5;//Void fraction at minimum fluidization condition
+db=[5;15];//Equilibrium bubble size in cm
+g=980;//Acceleration due to gravity in cm/s^2
+
+//CALCULATION
+n=length(db);
+i=1;
+while i<=n
+    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.(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.(34)
+    Kbe(i)=(Kbc(i)*Kce(i))/(Kbc(i)+Kce(i));//Gas interchange coefficient between bubble and emulsion from Eqn.(14)
+    e(i)=(Kce(i)-Kbe(i))/Kbe(i);//Error when minor resistance is ignored
+    i=i+1;
+end
+
+//OUTPUT
+printf('\ndb(cm)');
+printf('\t\tCalculated Kbc');
+printf('\tCalculated Kce');
+printf('\t\tKbe from Eqn.(14)');
+printf('\tErron when minor resistance is ignored (in percentage)');
+i=1;
+while i<=n
+    mprintf('\n%f',db(i));
+    mprintf('\t%f',Kbc(i));
+    mprintf('\t%f',Kce(i));
+    mprintf('\t\t%f',Kbe(i));
+    mprintf('\t\t%f',e(i)*100);
+    i=i+1;   
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH10/EX10.3/Chap10_Ex3.sce b/497/CH10/EX10.3/Chap10_Ex3.sce
new file mode 100755
index 000000000..3b5572357
--- /dev/null
+++ b/497/CH10/EX10.3/Chap10_Ex3.sce
@@ -0,0 +1,48 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-10, Example 3, Page 255
+//Title: Compare Interchange Rates for Adsorbed and Nonadsorbed Gases
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Kbe=[0.028;0.05];//Reported range for gas interchange coefficient between bubble and emulsion
+uo=0.30;//Superficial gas velocity in m/s
+db=0.13;//Equilibrium bubble size in m
+m=7;
+ephsilonmf=0.5;//Void fraction at minimum fluidization condition
+umf=0.0018;//Velocity at minimum fluidization condition in m/s
+D=[9E-6;22E-6];//Diffusion coefficient of gas in m^2/s
+g=9.81;//Acceleration due to gravity in m/s^2
+
+//CALCULATION
+n=length(Kbe);
+i=1;
+while i<=n
+    Kbem(i)=(6/db)*Kbe(i);//Gas interchange coefficient between bubble and emulsion from Eqn.(19)
+    Kbc(i)=4.5*(umf/db)+5.85*((D(i)^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(27)
+    Kce(i)=6.77*((D(i)*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(34)
+    Kbe(i)=(Kbc(i)*Kce(i))/(Kbc(i)+Kce(i));//Gas interchange coefficient between bubble and emulsion from Eqn.(14)
+    c(i)=(Kbem(i)/Kbe(i));
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nKbe from Eqn.(19)');
+printf('\tKbc from Eqn.(27)');
+printf('\tKce from Eqn.(34)');
+printf('\tKbe from Eqn.(14)');
+printf('\tComparison of Kbe from Eqn.(19) and that from Eqn.(14)');
+i=1;
+while i<=n
+    mprintf('\n%f',Kbem(i));
+    mprintf('\t\t%f',Kbc(i));
+    mprintf('\t\t%f',Kce(i));
+    mprintf('\t\t%f',Kbe(i));
+    mprintf('\t\t%f',c(i));
+    i=i+1;   
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH11/EX11.1/Chap11_Ex1.sce b/497/CH11/EX11.1/Chap11_Ex1.sce
new file mode 100755
index 000000000..56754f278
--- /dev/null
+++ b/497/CH11/EX11.1/Chap11_Ex1.sce
@@ -0,0 +1,56 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-11, Example 1, Page 265
+//Title: Fitting Reported Mass Transfer Data with the Bubbling Bed Model
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+db=0.37;//Equilibrium bubble size in cm
+dp=0.028;//Particle size in cm
+rhos=1.06;//Density of solids in g/cc
+ephsilonmf=0.5;//Void fraction at minimum fluidization condition
+phis=0.4;//Sphericity of solids
+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase
+rhog=1.18E-3;//Density of air in g/cc
+myu=1.8E-4;//Viscosity of gas in g/cm s
+D=0.065;//Diffusion coefficient of gas in cm^2/s
+Sc=2.35;//Schmidt number
+etad=1;//Adsorption efficiency factor
+y=1;
+umf=1.21;//Velocity at minimum fluidization condition in cm/s
+ut=69;//Terminal velocity in cm/s
+g=980;//Acceleration due to gravity in square cm/s^2
+uo=[10;20;30;40;50];//Superficial gas velocity in cm/s
+
+//CALCULATION
+n=length(uo);
+i=1;
+Rept=(dp*ut*rhog)/myu;
+Shstar=2+(0.6*(Rept^0.5)*(Sc^(1/3)));//Sherwood no. from Eqn.(1)
+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)
+ubr=0.711*(g*db)^0.5;//Rise velocity of the bubble
+while i<=n
+    x(i)=(uo(i)-umf)/(ubr*(1-ephsilonmf));//The term delta/(1-epshilonf) after simplification
+    Shbed(i)=x(i)*[(gammab*Shstar*etad)+((phis*dp^2*y)/(6*D))*Kbc];//Sherwood no. from Eqn.(11)
+    Rep(i)=(dp*uo(i)*rhog)/myu;//Reynolds of the particle
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nThe desired result is the relationship between Shbed and Rep  The points gives a straight line of the form y=mx+c');
+printf('\nRep');
+printf('\t\tShbed');
+i=1;
+while i<=n
+    printf('\n%f',Rep(i));
+    printf('\t%f',Shbed(i));
+    i=i+1;
+end
+plot(Rep,Shbed);
+xlabel("Rep");
+ylabel("Shbed");
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH11/EX11.1/Chap11_Ex1_R.jpg b/497/CH11/EX11.1/Chap11_Ex1_R.jpg
new file mode 100755
index 000000000..afda114a3
--- /dev/null
+++ b/497/CH11/EX11.1/Chap11_Ex1_R.jpg
diff --git a/497/CH11/EX11.2/Chap11_Ex2.sce b/497/CH11/EX11.2/Chap11_Ex2.sce
new file mode 100755
index 000000000..a942045dc
--- /dev/null
+++ b/497/CH11/EX11.2/Chap11_Ex2.sce
@@ -0,0 +1,40 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-11, Example 2, Page 267
+//Title: The Effect of m on Bubble-Emulsion Interchange
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+umf=0.12;//Velocity at minimum fluidization condition in cm/s
+uo=40;//Superficial gas velocity in cm/s
+ub=120;//Velocity of the bubble in cm/s
+D=0.7;//Diffusion coefficient of gas in cm^2/s
+abkbe1=1;//Bubble-emuslion interchange coefficient for non absorbing particles(m=0)
+abkbe2=18;//Bubble-emuslion interchange coefficient for highly absorbing particles(m=infinity)
+g=980;//Acceleration due to gravity in square cm/s^2
+
+//CALCULATION
+//For non absorbing particles m=0,etad=0
+Kbc=(ub/uo)*(abkbe1);
+dbguess=2;//Guess value of db
+function[fn]=solver_func(db)//Function defined for solving the system
+    fn=abkbe1-(uo/ub)*(4.5*(umf/db)+5.85*(D^0.5*g^0.25)/(db^(5/4)));//Eqn.(10.27)
+endfunction
+[d]=fsolve(dbguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(10.27) for db
+//For highly absorbing particles m=infinity, etad=1
+M=abkbe2-(uo/ub)*Kbc;
+//For intermediate condition
+alpha=100;
+m=10;
+etad=1/(1+(alpha/m));//Fitted adsorption efficiency factor from Eqn.(23)
+abkbe3=M*etad+(uo/ub)*Kbc;
+
+//OUTPUT
+mprintf('\nFor non absorbing particles:\n\tDiameter of bubble=%fcm\n\tBubble-cloud interchange coefficient=%fs^-1',d,Kbc);
+mprintf('\nFor highly absorbing partilces:\n\tM=%f',M);
+mprintf('\nFor intermediate condition:\n\tFitted adsorption efficiency factor:%f\n\tBubble-emuslion interchange coefficient:%fs^-1',etad,abkbe3);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH11/EX11.3/Chap11_Ex3.sce b/497/CH11/EX11.3/Chap11_Ex3.sce
new file mode 100755
index 000000000..d972b9fd3
--- /dev/null
+++ b/497/CH11/EX11.3/Chap11_Ex3.sce
@@ -0,0 +1,55 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-11, Example 3, Page 273
+//Title: Fitting Reported Heat Transfer Data with the Bubbling Bed Model
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+rhos=1.3;//Density of solids in g/cc
+phis=0.806;//Sphericity of solids
+gammab=0.001;//Ratio of volume of dispersed solids to that of bubble phase
+rhog=1.18E-3;//Density of air in g/cc
+Pr=0.69;//Prandtl number
+myu=1.8E-4;//Viscosity of gas in g/cm s
+Cpg=1.00;//Specific heat capacity of gas in J/g K
+ephsilonmf=0.45;//Void fraction at minimum fluidization condition
+kg=2.61E-4;//Thermal concuctivity of gas in W/cm k
+dp=0.036;//Particle size in cm
+umf=6.5;//Velocity at minimum fluidization condition in cm/s
+ut=150;//Terminal velocity in cm/s
+db=0.4;//Equilibrium bubble size in cm
+etah=1;//Efficiency of heat transfer
+uo=[10;20;30;40;50];//Superficial gas velocity in cm/s
+g=980;//Acceleration due to gravity in square cm/s^2
+
+//CALCULATION
+Nustar=2+[((dp*ut*rhog)/myu)^0.5*Pr^(1/3)];//Nusselt no. from Eqn.(25)
+Hbc=4.5*(umf*rhog*Cpg/db)+5.85*((kg*rhog*Cpg)^0.5*g^0.25/db^(5/4));//Total heat interchange across the bubble-cloud boundary from Eqn.(32)
+ubr=0.711*(g*db)^0.5;//Rise velocity of the bubble from Eqn.(6.7)
+n=length(uo);
+i=1;
+while i<=n
+    x(i)=(uo(i)-umf)/(ubr*(1-ephsilonmf));//The term delta/(1-epshilonf) after simplification
+    Nubed(i)=x(i)*[gammab*Nustar*etah+(phis*dp^2/(6*kg))*Hbc];//Nusselt no. from Eqn.(36)
+    Rep(i)=(dp*uo(i)*rhog)/myu;//Reynolds of the particle
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nThe desired result is the relationship between Nubed and Rep which is in the form of a straight line y=mx+c');
+printf('\nRep');
+printf('\t\tNubed');
+i=1;
+while i<=n
+    printf('\n%f',Rep(i));
+    printf('\t%f',Nubed(i));
+    i=i+1;
+end
+plot(Rep,Nubed);
+xlabel("Rep");
+ylabel("Nubed");
+ 
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH11/EX11.3/Chap11_Ex3_R.jpg b/497/CH11/EX11.3/Chap11_Ex3_R.jpg
new file mode 100755
index 000000000..719ebfecb
--- /dev/null
+++ b/497/CH11/EX11.3/Chap11_Ex3_R.jpg
diff --git a/497/CH11/EX11.4/Chap11_Ex4.sce b/497/CH11/EX11.4/Chap11_Ex4.sce
new file mode 100755
index 000000000..b3f2ff179
--- /dev/null
+++ b/497/CH11/EX11.4/Chap11_Ex4.sce
@@ -0,0 +1,41 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-11, Example 4, Page 274
+//Title: Heating a Particle in a Fluidized Bed
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+rhog=1.2;//Density of air in kg/m^3
+myu=1.8E-5;//Viscosity of gas in kg/m s
+kg=2.6E-2;//Thermal concuctivity of gas in W/m k
+dp=1E-4;//Particle size in m
+rhos=8920;//Density of solids in kg/m^3
+Cps=390;//Specific heat capacity of the solid in J/kg K
+ephsilonf=0.5;//Void fraction of the fluidized bed
+umf=0.1;//Velocity at minimum fluidization condition in m/s
+uo=0.1;//Superficial gas velocity in m/s
+pi=3.14
+
+//CALCULATION
+to=0;//Initial temperature of the bed
+T=100;//Temperature of the bed
+t=0.99*T;//Particle temperature i.e. when it approaches 1% of the bed temperature
+mp=(pi/6)*dp^3*rhos;//Mass of the particle
+A=pi*dp^2;//Surface area of the particle
+Rep=(dp*uo*rhog)/myu;//Reynold's no. of the particle
+Nubed=0.0178;//Nusselt no. from Fig.(6)
+hbed1=(Nubed*kg)/dp;//Heat transfer coefficient of the bed
+t1=(mp*Cps/(hbed1*A))*log((T-to)/(T-t));//Time needed for the particle approach 1 percentage of the bed temperature in case(a)
+hbed2=140*hbed1;//Since from Fig.(6) Nup is 140 times Nubed
+t2=(mp*Cps/(hbed2*A))*log((T-to)/(T-t));//Time needed for the particle approach 1 percentage of the bed temperature in case(b)
+
+//OUTPUT
+printf('\nCase(a):Using the whole bed coefficient from Fig.(6)');
+mprintf('\n\tTime needed for the particle approach 1 percentage of the bed temperature is %fs',t1);
+printf('\nCase(b):Uisng the single-particle coefficient of Eqn.(25),also shown in Fig.(6)');
+mprintf('\n\tTime needed for the particle approach 1 percentage of the bed temperature is %fs',t2);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH12/EX12.1/Chap12_Ex1.sce b/497/CH12/EX12.1/Chap12_Ex1.sce
new file mode 100755
index 000000000..d55dca836
--- /dev/null
+++ b/497/CH12/EX12.1/Chap12_Ex1.sce
@@ -0,0 +1,44 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-12, Example 1, Page 293
+//Title: Fine Particle (Geldart A) Bubbling Bed Reactor
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Kr=10;//rate constant in m^3 gas/m^3 cat s
+D=2E-5;//Diffusion coefficient of gas in m^2/s
+dpbar=68;//Average partilce size in micrometers
+ephsilonm=0.5;//Void fraction of fixed bed
+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase
+ephsilonmf=0.55;//Void fraction at minimum fluidization condition
+umf=0.006;//Velocity at minimum fluidization condition in m/s
+db=0.04;//Equilibrium bubble size in m
+Lm=0.7;//Length of the bed in m
+uo=0.1;//Superficial gas velocity in m/s
+dbed=0.26;//Diameter of the bed in m
+g=9.81;//Acceleration due to gravity in square m/s^2
+
+//CALCULATION
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)
+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)
+delta=uo/ub;//Fraction of bed in bubbles from Eqn.(6.29)
+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)
+ephsilonf=1-(1-delta)*(1-ephsilonmf);//Void fraction of fixed bed from Eqn.(6.20)
+Lf=(1-ephsilonm)*Lm/(1-ephsilonf);//Length of fixed bed from Eqn.(6.19)
+Krtou=Kr*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)
+Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Raction rate for fluidized bed from Eqn.(14)
+XA=1-exp(-1*Kf*Lf/ub);//Conversion from Eqn.(16)
+
+//OUTPUT
+mprintf('\nThe dimnesionless reaction rate group: %f',Krtou);
+mprintf('\nThe reaction rate for fluidized bed: %fs^-1',Kf);
+mprintf('\nConversion: %f',XA);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH12/EX12.2/Chap12_Ex2.sce b/497/CH12/EX12.2/Chap12_Ex2.sce
new file mode 100755
index 000000000..3eb8edbb8
--- /dev/null
+++ b/497/CH12/EX12.2/Chap12_Ex2.sce
@@ -0,0 +1,60 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-12, Example 2, Page 298
+//Title: Commercial-Sized Phthalic Anhydride Reactor
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+umf=0.005;//Velocity at minimum fluidization condition in m/s
+ephsilonm=0.52;//Void fraction of fixed bed
+ephsilonmf=0.57;//Void fraction at minimum fluidization condition
+DA=8.1E-6;//Diffusion coefficient of gas in m^2/s
+DR=8.4E-6;//Diffusion coefficient of gas in m^2/s
+Lm=5;//Length of the bed in m
+dte=1;//Diameter of tube in m
+Kr1=1.5;//rate constant in m^3 gas/m^3 cat s
+Kr3=0.01;//rate constant in m^3 gas/m^3 cat s
+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase
+uo=0.45;//Superficial gas velocity in m/s
+db=0.05;//Equilibrium bubble size in m from Fig.(6.8)
+ub=1.5;//Velocity of bubbles in bubbling bed in m/s from Fig.(6.11(a))
+g=9.81;//Acceleration due to gravity in square m/s^2
+
+//CALCULATION
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+KbcA=4.5*(umf/db)+5.85*((DA^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)
+KceA=6.77*((DA*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)
+KbcR=4.5*(umf/db)+5.85*((DR^0.5*g^0.25)/db^(5/4));//Gas interchange coefficient between bubble and cloud from Eqn.(10.27)
+KceR=6.77*((DR*ephsilonmf*0.711*(g*db)^0.5)/db^3)^0.5;//Gas interchange coefficient between emulsion and cloud from Eqn.(10.34)
+delta=uo/ub;//Fraction of bed in bubbles from Eqn.(6.29)
+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)
+ephsilonf=1-(1-delta)*(1-ephsilonmf);//Void fraction of fixed bed from Eqn.(6.20)
+Lf=(1-ephsilonm)*Lm/(1-ephsilonf);//Length of fixed bed from Eqn.(6.19)
+Krtou=Kr1*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)
+Kr12=Kr1;//Since the reactions are a special case of Denbigh scheme
+Kr34=Kr3;
+Kf1=(gammab*Kr12+1/((1/KbcA)+(1/(gammac*Kr12+1/((1/KceA)+(1/(gammae*Kr12)))))))*(delta/(1-ephsilonf));//Rate of reaction 1 for fluidized bed from Eqn.(14)
+Kf3=(gammab*Kr34+1/((1/KbcR)+(1/(gammac*Kr34+1/((1/KceR)+(1/(gammae*Kr34)))))))*(delta/(1-ephsilonf));//Rate of reaction 2 for fluidized bed from Eqn.(14)
+Kf12=Kf1;
+Kf34=Kf3;
+KfA=[[KbcR*KceA/gammac^2+(Kr12+KceA/gammac+KceA/gammae)*(Kr34+KceR/gammac+KceR/gammae)]*delta*KbcA*Kr12*Kr34/(1-ephsilonf)]/[[(Kr12+KbcA/gammac)*(Kr12+KceA/gammae)+Kr12*KceA/gammac]*[(Kr34+KbcR/gammac)*(Kr34+KceR/gammae)+Kr34*KceR/gammac]];//Rate of raection with respect to A from Eqn.(35)
+KfAR=Kr1/Kr12*Kf12-KfA;//Rate of reaction from Eqn.(34)
+tou=Lf*(1-ephsilonf)/uo;//Residence time from Eqn.(5)
+XA=1-exp(-Kf1*tou);//Conversion of A from Eqn.(26)
+XR=1-((KfAR/(Kf12-Kf34))*[exp(-Kf34*tou)-exp(-Kf12*tou)]);//Conversion of R from Eqn.(27)
+SR=(1-XR)/XA;//Selectivity of R
+
+//OUTPUT
+
+mprintf('\nRate of reaction 1 for fluidized bed:%f',Kf1);
+mprintf('\nRate of reaction 2 for fluidized bed:%f',Kf3);
+mprintf('\nRate of reaction 1 with respect to A:%f',KfA);
+mprintf('\nThe Conversion of Napthalene:%f percentage',XA*100);
+mprintf('\nThe selectivity of Phthalic anhydride:%f percentage',SR*100);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH12/EX12.3/Chap12_Ex3.sce b/497/CH12/EX12.3/Chap12_Ex3.sce
new file mode 100755
index 000000000..8eec09dc6
--- /dev/null
+++ b/497/CH12/EX12.3/Chap12_Ex3.sce
@@ -0,0 +1,42 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-12, Example 3, Page 302
+//Title: Bubbling Bed Reactor for Intermediate Sized Reactor
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Kr=3;//rate constant in m^3 gas/m^3 cat s
+db=0.12;//Equilibrium bubble size in m
+D=9E-5;//Diffusion coefficient of gas in m^2/s
+dpbar=68;//Average partilce size in micrometers
+ephsilonm=0.42;//Void fraction of fixed bed
+uo=0.4;//Superficial gas velocity in m/s
+Lm=0.8;//Length of the bed in m
+ephsilonmf=0.45;//Void fraction at minimum fluidization condition
+umf=0.21;//Velocity at minimum fluidization condition in m/s
+gammab=0;//Ratio of volume of dispersed solids to that of bubble phase
+g=9.81;//Acceleration due to gravity in square m/s^2
+
+//CALCULATION
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)
+ubstar=ub+3*umf;//Rise velocity of the bubble gas from Eqn.(45)
+delta=(uo-umf)/(ub+umf);//Fraction of bed in bubbles from Eqn.(6.46)
+Kbe=4.5*(umf/db);//Interchange coefficient between bubble and emulsion from Eqn.(47)
+Lf=Lm*(1-ephsilonm)/((1-delta)*(1-ephsilonmf));//Length of fixed bed
+phi=[(Kr/Kbe)^2*{(1-ephsilonmf)-gammab*(umf/ubstar)}^2+((delta/(1-delta))+umf/ubstar)^2+2*(Kr/Kbe)*{(1-ephsilonmf)-gammab*(umf/ubstar)}*((delta/(1-delta))-umf/ubstar)]^0.5;//From Eqn.(52)
+q1=0.5*Kr/umf*{(1-ephsilonmf)+gammab*(umf/ubstar)}+0.5*Kbe/umf*{((delta/(1-delta))+umf/ubstar)-phi};//From Eqn.(50)
+q2=0.5*Kr/umf*{(1-ephsilonmf)+gammab*(umf/ubstar)}+0.5*Kbe/umf*{((delta/(1-delta))+umf/ubstar)+phi};//From Eqn.(50)
+si1=0.5-0.5*((1-delta)/delta)*[umf/ubstar-Kr/Kbe*{(1-ephsilonmf)-gammab*(umf/ubstar)}-phi];//From Eqn.(51)
+si2=0.5-0.5*((1-delta)/delta)*[umf/ubstar-Kr/Kbe*{(1-ephsilonmf)-gammab*(umf/ubstar)}+phi];//From Eqn.(51)
+XA=1-(delta/(1-delta))*(1/(uo*phi))*[(1-si2)*{si1*delta*ubstar+(1-delta)*umf}*exp(-q1*Lf)+(si1-1)*{si2*delta*ubstar+(1-delta)*umf}*exp(-q2*Lf)];//Conversion from Eqn.(49)
+Krtou=Kr*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)
+
+//OUTPUT
+mprintf('\nCOmparing the values of 1-XA = %f and Krtou = %f with Fig.(6), we can conlcude that this operating condition is shown as point A in Fig.(3)',1-XA,Krtou);
+printf('\nLine 2 gives the locus of conversions for different values of the reaction rate group for this fluidized contacting');
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH12/EX12.4/Chap12_Ex4.sce b/497/CH12/EX12.4/Chap12_Ex4.sce
new file mode 100755
index 000000000..77c4e6ec6
--- /dev/null
+++ b/497/CH12/EX12.4/Chap12_Ex4.sce
@@ -0,0 +1,31 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-12, Example 4, Page 305
+//Title: Reaction in the Slow Bubble Regime
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+uo=0.25;//Superficial gas velocity in m/s
+db=0.025;//Equilibrium bubble size in m
+Kr=1.5;//rate constant in m^3 gas/m^3 cat s
+umf=0.21;//Velocity at minimum fluidization condition in m/s
+Lm=0.8;//Length of the bed in m
+ephsilonm=0.42;//Void fraction of fixed bed
+g=9.81;//Acceleration due to gravity in square m/s^2
+
+//CALCULATION
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)
+delta=(uo-umf)/(ub+2*umf);//Fraction of bed in bubbles from Eqn.(55) since ub/umf<<1 
+XA=1-exp(-Kr*Lm*((1-ephsilonm)/uo)*(umf/uo)*(1-delta));//Conversion from Eqn.(57)
+Krtou=Kr*Lm*(1-ephsilonm)/uo;//Dimensionless reaction rate group from Eqn.(5)
+
+
+//OUTPUT
+mprintf('\nComparing the values of 1-XA = %f and Krtou = %f with Fig.(6), we can conlcude that this operating condition is shown as point B in Fig.(3)',1-XA,Krtou);
+printf('\nLine 3 gives the locus of conversions for different values of the reaction rate group for this fluidized contacting');
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH12/EX12.5/Chap12_Ex5.sce b/497/CH12/EX12.5/Chap12_Ex5.sce
new file mode 100755
index 000000000..929664bff
--- /dev/null
+++ b/497/CH12/EX12.5/Chap12_Ex5.sce
@@ -0,0 +1,46 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-12, Example 5, Page 307
+//Title: Conversion in the Freeboard of a Reactor
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+uo=0.3;//Superficial gas velocity in m/s
+Lf=1.1;//Length of fixed bed in m
+Hf=1.2;//Length of freeboard in m
+db=0.04;//Equilibrium bubble size in m
+umf=0.006;//Velocity at minimum fluidization condition in m/s
+ephsilonmf=0.55;//Void fraction at minimum fluidization condition
+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase
+Kr=10;//rate constant in m^3 gas/m^3 cat s
+D=2E-5;//Diffusion coefficient of gas in m^2/s
+g=9.81;//Acceleration due to gravity in square m/s^2
+
+//CALCULATION
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+ub=uo-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)
+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)
+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)
+Kf=(gammab*Kr)+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Raction rate for fluidized bed from Eqn.(14)
+XA=1-exp(-1*Kf*Lf/ub);//Conversion at the top of dense bed from Eqn.(16)
+etabed=(Kf*delta)/(Kr*(1-ephsilonf));//Reactor efficiency from Eqn.(22)
+a=0.6/uo//Since uoa = 0.6s^-1 from Fig.(5)
+adash=6.62;//From Fig.(5)
+XA1=1-1/(exp(((1-ephsilonf)*Kr/(uo*a))*[(1-exp(-a*Hf))-((1-etabed)/(1+(adash/a)))*(1-exp(-(a+adash)*Hf))]));//Conversion from Eqn.(64)
+XA2=1-(1-XA1)*(1-XA);//Conversion at the exit from Eqn.(64)
+
+//OUTPUT
+printf('\nThe conversion:');
+mprintf('\n\tAt the top pf the dense bed: %f percentage',XA*100);
+mprintf('\n\tAt the reactor exit: %f percentage',XA2*100);
+
+//Disclaimer: The value of kf deviate from the one given in textbook, where as it is close to the value obtained by manual calculation. 
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH13/EX13.1/Chap13_Ex1.sce b/497/CH13/EX13.1/Chap13_Ex1.sce
new file mode 100755
index 000000000..d27b58919
--- /dev/null
+++ b/497/CH13/EX13.1/Chap13_Ex1.sce
@@ -0,0 +1,50 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-13, Example 1, Page 331
+//Title: h on a Horizontal Tube Bank
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dp=57;//Particle size in micrometer
+rhos=940;//Density of solids in kg/m^3
+Cps=828;//Specific heat capacity of the solid in J/kg K
+ks=0.20;//Thermal conductivity of solids in W/m k
+kg=0.035;//Thermal concuctivity of gas in W/m k
+umf=0.006;//Velocity at minimum fluidization condition in m/s
+ephsilonmf=0.476;//Void fraction at minimum fluidization condition
+do1=0.0254;//Outside diameter of tube in m
+L=1;
+uo=[0.05;0.1;0.2;0.35];//Superficial gas velocity in m/s
+nw=[2;3.1;3.4;3.5];//Bubble frequency in s^-1
+g=9.81;//Acceleration due to gravity in square m/s^2
+
+
+//CALCULATION
+dte=4*do1*L/2*L;//Hydraulic diameter from Eqn.(6.13)
+db=(1+1.5)*0.5*dte;//Rise velocity of the bubble
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+phib=0.19;//From Fig.(15) for ks/kg=5.7
+ke=ephsilonmf*kg+(1-ephsilonmf)*ks*[1/((phib*(ks/kg))+(2/3))];//Effective thermal conductivity of bed from Eqn.(3) 
+n=length(uo);
+i=1;
+while i<=n
+    ub(i)=uo(i)-umf+ubr;//Velocity of bubbles in bubbling beds in Eqn.(6.8)
+    delta(i)=uo(i)/ub(i);//Fraction of bed in bubbles from Eqn.(6.29)
+    h(i)=1.13*[ke*rhos*(1-ephsilonmf)*Cps*nw(i)*(1-delta(i))]^0.5;//Heat transfer coefficinet from Eqn.(18)
+    i=i+1;
+end    
+
+//OUTPUT
+printf('\nSuperficial gas velocity(m/s)');
+printf('\tHeat transfer coefficient(W/m^2 k)');
+i=1;
+while i<=n
+    mprintf('\n%f',uo(i));
+    mprintf('\t\t\t%f',h(i));
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH13/EX13.2/Chap13_Ex2.sce b/497/CH13/EX13.2/Chap13_Ex2.sce
new file mode 100755
index 000000000..c2c02d9be
--- /dev/null
+++ b/497/CH13/EX13.2/Chap13_Ex2.sce
@@ -0,0 +1,45 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-13, Example 2, Page 332
+//Title: Effect of Gas Properties on h
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dp=80;//Particle size in micrometer
+rhos=2550;//Density of solids in kg/m^3
+Cps=756;//Specific heat capacity of the solid in J/kg K
+ks=1.21;//Thermal conductivity of solids in W/m k
+kg=[0.005;0.02;0.2];//Thermal concuctivity of gas in W/m k
+ephsilonmf=0.476;//Void fraction at minimum fluidization condition
+
+//CALCULATION
+delta=0.5*(0.1+0.3);//For a gently fluidized bed
+nw=3;//Bubble frequency in s^-1 from Fig.(5.12) at about 30cm above the distributor
+n=length(kg);
+i=1;
+while i<=n
+    x(i)=ks/kg(i);//To find different values of ks/kg
+    i=i+1;
+end
+phib=[0.08;0.10;0.20];//From Fig.(15) for different values of ks/kg
+i=1;
+while i<=n
+    ke(i)=ephsilonmf*kg(i)+(1-ephsilonmf)*ks*[1/((phib(i)*(ks/kg(i)))+(2/3))];//Effective thermal conductivity of bed from Eqn.(3)
+    h1(i)=1.13*[ke(i)*rhos*(1-ephsilonmf)*Cps*nw*(1-delta)]^0.5;//Heat transfer coefficinet from Eqn.(18)
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nThermal conductivity of Gas(W/m K))');
+printf('\tMax. heat transfer coefficient(W/m^2 k)');
+i=1;
+while i<=n
+    mprintf('\n%f',kg(i));
+    mprintf('\t\t\t\t%f',h1(i));
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH13/EX13.3/Chap13_Ex3.sce b/497/CH13/EX13.3/Chap13_Ex3.sce
new file mode 100755
index 000000000..7fb0be57a
--- /dev/null
+++ b/497/CH13/EX13.3/Chap13_Ex3.sce
@@ -0,0 +1,37 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-13, Example 3, Page 332
+//Title: Effect of Particle Size on h
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+rhos=2700;//Density of solids in kg/m^3
+Cps=755;//Specific heat capacity of the solid in J/kg K
+ks=1.2;//Thermal conductivity of solids in W/m k
+kg=0.028;//Thermal concuctivity of gas in W/m k
+ephsilonmf=0.476;//Void fraction at minimum fluidization condition
+dp1=10E-3;//Particle size for which h=hmax in m
+hmax=250;//Max. heat transfer coefficient in W/m^2 K 
+nw=5;//Bubble frequency in s^-1
+delta=0.1;//Fraction of bed in bubbles
+deltaw=0.1;//Fraction of bed in bubbles in wall region
+dp=2E-3;//Diameter of particle in m
+
+//CALCULATION
+x=ks/kg;
+phib=0.11;
+phiw=0.17;
+ke=ephsilonmf*kg+(1-ephsilonmf)*ks*[1/((phib*(ks/kg))+(2/3))];//Effective thermal conductivity of bed from Eqn.(3)
+hpacket=1.13*[ke*rhos*(1-ephsilonmf)*Cps*nw/(1-deltaw)]^0.5;//Heat transfer coefficient for the packet of emulsion from Eqn.(11)
+ephsilonw=ephsilonmf;//Void fraction in the wall region
+kew=ephsilonw*kg+(1-ephsilonw)*ks*[(phiw*(ks/kg)+(1/3))^-1];//Effective thermal conductivity in the wall region with stagnant gas from Eqn.(4)
+y=(2*kew/dp1)+(hmax*hpacket)/(((1-deltaw)*hpacket)-hmax);//Calculating the term alphaw*Cpg*rhog*uo from Eqn.(16) by rearranging it
+h=(1-deltaw)/((2*kew/dp+y*(dp/dp1)^0.5)^-1+hpacket^-1);//Heat transfer coeeficient from Eqn.(11) by using the value of y 
+
+//OUTPUT
+mprintf('\nThe heat transfer coefficient for paricle size of %fm = %fW/m^2 K',dp,h);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH13/EX13.4/Chap13_Ex4.sce b/497/CH13/EX13.4/Chap13_Ex4.sce
new file mode 100755
index 000000000..cc1eb32b4
--- /dev/null
+++ b/497/CH13/EX13.4/Chap13_Ex4.sce
@@ -0,0 +1,40 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-13, Example 4, Page 334
+//Title: Freeboard Heat Exchange
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Hf=4;//Height of freeboard in m
+uo=2.4;//Superficial gas velocity in m/s
+ho=350;//Heat transfer coefficient at the bottom of freeboard region in W/m^2 K
+hg=20;//Heat transfer coefficient in equivalent gas stream, but free of solids in W/m^2 K
+
+//CALCULATION
+zf=[0;0.5;1;1.5;2;2.5;3;3.5;Hf];//Height above the top of the dense bubbling fluidized bed
+hr=0;//Assuming heat transfer due to radiation is negligible
+a=1.5/uo;//Since decay coefficient from Fig.(7.12), a*uo=1.5s^-1 
+n=length(zf);
+i=1;
+while i<=n
+    h(i)=(hr+hg)+(ho-hr-hg)*exp(-a*zf(i)/2);//Heat transfer coefficient from Eqn.(24) for zf=Hf
+    i=i+1;
+end    
+hbar=(hr+hg)+2*(ho-hr-hg)*(1-exp(-a*Hf/2))/(a*Hf);//Mean heat transfer coefficient for the 4-m high freeboard from Eqn.(26)
+
+//OUTPUT
+printf('\nThe required relationship is h(W/m^2 K) vs. zf(m) as in Fig.(9a)');
+printf('\nHeight above the dense bubbling fluidized bed(m))');
+printf('\tHeat transfer coefficient(W/m^2 k)');
+i=1;
+while i<=n
+    mprintf('\n%f',zf(i));
+    mprintf('\t\t\t\t\t\t%f',h(i));
+    i=i+1;
+end
+mprintf('\n\nThe mean heat transfer coefficient for the 4-m high freeboard =%fW/m^2 K',hbar);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH14/EX14.1/Chap14_Ex1.sce b/497/CH14/EX14.1/Chap14_Ex1.sce
new file mode 100755
index 000000000..8417234c0
--- /dev/null
+++ b/497/CH14/EX14.1/Chap14_Ex1.sce
@@ -0,0 +1,36 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-14, Example 1, Page 343
+//Title: Flow with Elutriation
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Fo=2.7;//Feed rate in kg/min
+Fof=0.9;//Feed rate of fines in feed in kg/min
+Foc=1.8;//Feed rate of coarse in feed in kg/min
+W=17;//Bed weight in kg
+kf=0.8;//Elutriation of fines in min^-1
+kc=0.0125;//Elutriation of coarse in min^-1
+
+//CALCULATION
+F1guess=1;//Guess value of F1
+function[fn]=solver_func(F1)//Function defined for solving the system
+    fn=F1-(Fof/(1+(W/F1)*kf))-(Foc/(1+(W/F1)*kc));//Eqn.(17)
+endfunction
+[F1]=fsolve(F1guess,solver_func,1E-6);//Inbuilt function fsolve to solve for F1
+F1f=Fof/(1+(W/F1)*kf);//Flow rate of fines in entrained streams from Eqn.(16)
+F1c=Foc/(1+(W/F1)*kc);//Flow rate of coarse in entrained streams from Eqn.(16)
+F2f=Fof-F1f;//Flow rate of fines in overflow streams from Eqn.(9)
+F2c=Foc-F1c;//Flow rate of coarse in overflow streams from Eqn.(9)
+tbarf=1/((F1/W)+kf);//Mean residence time of fines from Eqn.(12)
+tbarc=1/((F1/W)+kc);//Mean residence time of coarse from Eqn.(12)
+
+//OUTPUT
+mprintf('\nFlow rate in entrained stream:\n\tFines:%fkg/min\n\tCoarse:%fkg/min',F1f,F1c);
+mprintf('\nFlow rate in overflow stream:\n\tFines:%fkg/min\n\tCoarse:%fkg/min',F2f,F2c);
+mprintf('\nMean residence time:\n\tFines:%fmins\n\tCoarse:%fmins',tbarf,tbarc);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH14/EX14.2/Chap14_Ex2.sce b/497/CH14/EX14.2/Chap14_Ex2.sce
new file mode 100755
index 000000000..a1cf0488c
--- /dev/null
+++ b/497/CH14/EX14.2/Chap14_Ex2.sce
@@ -0,0 +1,72 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-14, Example 2, Page 344
+//Title: Flow with Elutriation and Change in Density of Solids
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dt=4;//Diameter of reactor in m
+ephsilonm=0.4;//Void fraction of static bed
+rhos=2500;//Density of solid in the bed in kg/m^3
+Lm=1.2;//Height of static bed in m
+Fo=3000;//Feed rate in kg/hr
+beta1=1.2;//Increase in density of solids
+dp=[3;4;5;6;7;8;9;10;11;12;3;14;16;18;20;22;24;26;28;30]*10^-2;//Size of particles in mm
+po=[0;0.3;0.8;1.3;1.9;2.6;3.5;4.4;5.7;6.7;7.5;7.8;7.5;6.3;5.0;3.6;2.4;1.3;0.5;0];//Size distribution of solids in mm^-1
+k=[0;10;9.75;9.5;8.75;7.5;6.0;4.38;2.62;1.20;0.325;0;0;0;0;0;0;0;0;0]*10^-4;//Elutriation constant in s^-1
+pi=3.14;
+
+//CALCULATION
+W=(pi/4*dt^2)*Lm*(1-ephsilonm)*rhos;//Weight of solids in bed
+n=length(dp);
+i=1;
+F1guess=1000;//Guess value for F1
+F1c=2510:10:2700;
+while i<=n
+    function[fn]=solver_func(F1)//Function defined for solving the system
+        if k(i)==0  then    x(i)=0; break 
+                    else    x(i)=(po(i)/(W*k(i)/F1))*log(1+(W*k(i)/F1));         
+        end
+    fn=F1/(Lm*Fo)-x(i);
+    endfunction
+    [F1(i)]=fsolve(F1guess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(20) for F1
+    c(i)=F1c(i)/(Lm*Fo);
+    if F1(i)==0 then a(i)=0;
+    else     a(i)=(po(i)/(W*k(i)/F1(i)))*log(1+(W*k(i)/F1(i)));
+    end    
+    i=i+1;
+end
+plot(F1,a,F1,c);
+xtitle('F1 vs a,c','F1','a,c');
+F1n=2500;//The point were both the curves meet
+F2=beta1*Fo-F1n;//Flow rate of the second leaving stream
+j=1;
+m=length(dp);
+while j<=m
+    p1(j)=(1/F1n)*((Fo*po(j))/(1+(W/F1n)*k(j)));//Size distribution of stream 1 in mm^-1 from Eqn.(16)
+    p2(j)=k(j)*W*p1(j)/F2;//Size distribution of stream 2 in mm^-1 from Eqn.(7)
+    if p1(j)==0 & p2(j)==0 then tbar(j)=0;
+    else  if  p1(j)==0 then tbar(j)=(W*p1(j))/(F2*p2(j));
+        else if  p2(j)==0 then tbar(j)=(W*p1(j))/(F1n*p1(j));
+            else tbar(j)=(W*p1(j))/(F1n*p1(j)+F2*p2(j));//Average time in hr from Eqn.(11)
+            end
+        end
+    end
+    j=j+1;
+end
+
+//OUTPUT
+printf('\nFlow rate of stream 1:%fkg/hr',F1n);
+printf('\nFlow rate of stream 2:%fkg/hr',F2);
+j=1;
+mprintf('\ntbar(hr)');
+while j<=m
+    mprintf('\n%f',tbar(j));
+    j=j+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+//DISCLAIMER: The value obtained for tbar is deviating highly form the one given in textbook. However, the value obtained by manual calculation is close to the   ones obtained from the program.
+\ No newline at end of file
diff --git a/497/CH14/EX14.2/Chap14_Ex2_R.jpg b/497/CH14/EX14.2/Chap14_Ex2_R.jpg
new file mode 100755
index 000000000..e38a4223f
--- /dev/null
+++ b/497/CH14/EX14.2/Chap14_Ex2_R.jpg
diff --git a/497/CH14/EX14.3/Chap14_Ex3.sce b/497/CH14/EX14.3/Chap14_Ex3.sce
new file mode 100755
index 000000000..4e1a107a1
--- /dev/null
+++ b/497/CH14/EX14.3/Chap14_Ex3.sce
@@ -0,0 +1,22 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-14, Example 3, Page 351
+//Title: Single-Size Feed of Shrinking Particles
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dp=1;//Particle size in mm
+Fo=10;//Feed rate in kg/min
+k=0.1;//Particle shrinkage rate in mm/min
+
+//CALCULATION
+R=k/2;//Particle shrinkage rate in terms of radius
+W=(Fo*dp/2)/(4*R);//Bed weight from Eqn.(42)
+
+//OUTPUT
+printf('\nWeight of bed:%fkg',W);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH14/EX14.4/Chap14_Ex4.sce b/497/CH14/EX14.4/Chap14_Ex4.sce
new file mode 100755
index 000000000..ccc99bb2f
--- /dev/null
+++ b/497/CH14/EX14.4/Chap14_Ex4.sce
@@ -0,0 +1,30 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-14, Example 4, Page 352
+//Title: Wide Size Distribution of Shrinking Particle
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dpi=[1.05;0.95;0.85;0.75;0.65;0.55;0.45;0.35;0.25;0.15;0.05];//Mean size in mm
+Fo=[0;0.5;3.5;8.8;13.5;17.0;18.2;17.0;13.5;7.3;0]*10^-2;//Feed rate in kg/s
+k=[0;0;0;0;0;0;0;0;2.0;12.5;62.5]*10^-5;//Elutriation constant in s^-1
+R=-1.58*10^-5;//Rate of particle shrinkage in mm/s
+deldpi=0.1;//Size intervals in mm
+
+//CALCULATION
+n=length(dpi);
+m=2;//Starting with the largest value size interval that contains solids
+W(m-1)=0;
+while m<=n
+    W(m)=(Fo(m)-R*W(m-1)/deldpi)/(k(m)-R/deldpi-3*R/dpi(m));//From Eqn.(33)
+    m=m+1;
+end
+Wt=sum(W);//Total sum
+
+//OUTPUT
+printf('\nTotal mass in the bed:%fkg',Wt);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH14/EX14.5/Chap14_Ex5.sce b/497/CH14/EX14.5/Chap14_Ex5.sce
new file mode 100755
index 000000000..74a98ae99
--- /dev/null
+++ b/497/CH14/EX14.5/Chap14_Ex5.sce
@@ -0,0 +1,52 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-14, Example 5, Page 353
+//Title: Elutriation and Attrition of Catalyst
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dpi=[0.17;0.15;0.13;0.11;0.09;0.07;0.05;0.03;0.01];//Mean size of particles in mm
+a=[0;0.95;2.45;5.2;10.1;23.2;35.65;20.0;2.45]*10^-2;//Feed composition Fo(dpi)/Fo
+y=[0;0;0;0;0;0;0.625;10.225;159.25]*10^-6;//Elutriation and cyclone efficiency k(dpi)(1-eta(dpi))
+F=0.01;//Rate at which solids are withdrawn in kg/s
+W=40000;//Weight of bed in kg
+dp1=0.11//Initial size in mm
+dp2=0.085;//Size after shrinking in mm
+dpmin=0.01;//Minimum size in mm
+deldpi=2*10^-2;//Size inerval in mm
+t=20.8;//Time in days
+si=1;
+
+//CALCULATION
+kdash=log((dp1-dpmin)/(dp2-dpmin))/(t*24*3600);//Rate of particle shrinkage from Eqn.(24)
+n=length(dpi);
+m=2;
+Fo=0.05;//Initial value of Fo
+F1(m-1)=0;
+s=0;
+c=0;
+t=1E-6;
+while m<=n
+    R(m)=-kdash*(dpi(m)-dpmin);//Rate of size change
+    x(m)=(a(m)*Fo-W*R(m-1)*F1(m-1)/deldpi)/(F+(W*y(m))-(W*R(m)/deldpi)-3*W*R(m)/dpi(m));//Eqn.(34)
+    F1(m)=x(m)*F;
+    c=c+x(m);
+    m=m+1;
+    if abs(c-1)<t then break
+    end
+    Fo=Fo+0.0001;//Incrementing Fo
+end  
+
+//OUTPUT
+mprintf('\nFeed rate with deldpi=%fmm is %fg/hr',deldpi,Fo);
+i=1;
+mprintf('\nBed composition');
+while i<=n
+    printf('\n%f',x(i)*100);
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH15/EX15.1/Chap15_Ex1.sce b/497/CH15/EX15.1/Chap15_Ex1.sce
new file mode 100755
index 000000000..55c53a315
--- /dev/null
+++ b/497/CH15/EX15.1/Chap15_Ex1.sce
@@ -0,0 +1,25 @@
+//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
new file mode 100755
index 000000000..ea021ba10
--- /dev/null
+++ b/497/CH15/EX15.2/Chap15_Ex2.sce
@@ -0,0 +1,59 @@
+//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
new file mode 100755
index 000000000..4fede05a6
--- /dev/null
+++ b/497/CH15/EX15.3/Chap15_Ex3.sce
@@ -0,0 +1,36 @@
+//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
new file mode 100755
index 000000000..49408ef11
--- /dev/null
+++ b/497/CH15/EX15.4/Chap15_Ex4.sce
@@ -0,0 +1,55 @@
+//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
new file mode 100755
index 000000000..62f3b87b6
--- /dev/null
+++ b/497/CH15/EX15.5/Chap15_Ex5.sce
@@ -0,0 +1,58 @@
+//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
diff --git a/497/CH16/EX16.1/Chap16_Ex1.sce b/497/CH16/EX16.1/Chap16_Ex1.sce
new file mode 100755
index 000000000..95a99c61c
--- /dev/null
+++ b/497/CH16/EX16.1/Chap16_Ex1.sce
@@ -0,0 +1,41 @@
+//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 ======================================================
+\ No newline at end of file
diff --git a/497/CH16/EX16.2/Chap16_Ex2.sce b/497/CH16/EX16.2/Chap16_Ex2.sce
new file mode 100755
index 000000000..c8a5c8864
--- /dev/null
+++ b/497/CH16/EX16.2/Chap16_Ex2.sce
@@ -0,0 +1,78 @@
+//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 ======================================================
+\ No newline at end of file
diff --git a/497/CH16/EX16.3/Chap16_Ex3.sce b/497/CH16/EX16.3/Chap16_Ex3.sce
new file mode 100755
index 000000000..402fe4068
--- /dev/null
+++ b/497/CH16/EX16.3/Chap16_Ex3.sce
@@ -0,0 +1,29 @@
+//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 ======================================================
+\ No newline at end of file
diff --git a/497/CH16/EX16.4/Chap16_Ex4.sce b/497/CH16/EX16.4/Chap16_Ex4.sce
new file mode 100755
index 000000000..ff285781b
--- /dev/null
+++ b/497/CH16/EX16.4/Chap16_Ex4.sce
@@ -0,0 +1,62 @@
+//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 ======================================================
+\ No newline at end of file
diff --git a/497/CH16/EX16.5/Chap16_Ex5.sce b/497/CH16/EX16.5/Chap16_Ex5.sce
new file mode 100755
index 000000000..19b0b730b
--- /dev/null
+++ b/497/CH16/EX16.5/Chap16_Ex5.sce
@@ -0,0 +1,82 @@
+//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 ======================================================
+\ No newline at end of file
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
diff --git a/497/CH18/EX18.1/Chap18_Ex1.sce b/497/CH18/EX18.1/Chap18_Ex1.sce
new file mode 100755
index 000000000..777ab8acc
--- /dev/null
+++ b/497/CH18/EX18.1/Chap18_Ex1.sce
@@ -0,0 +1,41 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-18, Example 1, Page 456
+//Title: Kinetics of Zinc Blende Roasting
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+xA=0.08;//Fraction of oxygen in stream
+dp=[2;0.1];//Particle diameter in mm
+rhos=4130;//Density of catalyst in kg/m^3
+Ds=8E-6;//Diffusion coefficient of solid in m^2/s
+kc=0.02;//Reaction rate constant in m/s
+P=10^5;//Pressure in bar\
+R=8.314;//Universal gas constant
+T=900;//Temperature in degree C
+mB=0.09745;//Molecular weight of ZnS in kg/mol
+
+//CALCULATION
+b=2/3;//Stoichiometric coefficient of ZnS in the reaction equation
+CA=xA*P/(R*(T+273));//Concentration of Oxygen
+rhob=rhos/mB;//Molar density of pure solid
+n=length(dp);
+i=1;
+while i<=n
+    kbar(i)=(kc^-1+(dp(i)*10^-3/(12*Ds)))^-1;//Average reaction rate constant from Eqn.(11)
+    tou(i)=rhob*dp(i)*10^-3/(2*b*kbar(i)*CA);//Time for complete reaction in seconds from Eqn.(9)
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nParticle Size(mm)\tAverage rate constant(m/s)\tTime for complete reaction(min)');
+i=1;
+while i<=n
+    mprintf('\n%f\t\t%f\t\t\t%f',dp(i),kbar(i),tou(i)/60);
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH18/EX18.2/Chap18_Ex2.sce b/497/CH18/EX18.2/Chap18_Ex2.sce
new file mode 100755
index 000000000..8a619e683
--- /dev/null
+++ b/497/CH18/EX18.2/Chap18_Ex2.sce
@@ -0,0 +1,39 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-18, Example 2, Page 457
+//Title: Kinetics of Carbon Burning
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+xA=0.08;//Fraction of oxygen in stream
+dp=1;//Particle diameter in mm
+rhos=2200;//Density of catalyst in kg/m^3
+kc=0.2;//Reaction rate constant in m/s
+mC=0.012;//Molecular weight of carbon in kg/mol
+P=10^5;//Pressure in bar\
+R=8.314;//Universal gas constant
+T=900;//Temperature in degree C
+
+//CALCULATION
+b=1;//Stoichiometric coefficient of C in the reaction equation
+CA=xA*P/(R*(T+273));//Concentration of Oxygen
+rhob=rhos/mC;//Molar density of pure solid reactant
+tou=rhob*10^-3/(2*b*kc*CA);//Time required for complete reaction in seconds
+
+//OUTPUT
+mprintf('\nThe time required for complete combustion:%fmins',tou/60);
+
+//====================================END OF PROGRAM ======================================================
+
+
+
+
+
+
+
+
+
+
diff --git a/497/CH18/EX18.3/Chap18_Ex3.sce b/497/CH18/EX18.3/Chap18_Ex3.sce
new file mode 100755
index 000000000..028edc5fc
--- /dev/null
+++ b/497/CH18/EX18.3/Chap18_Ex3.sce
@@ -0,0 +1,63 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-18, Example 3, Page 462
+//Title: Roasting Kinetics from Flowing Solids Data
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+dp=110;//Particle size in micrometer
+T=900;//Temperature of roaster in degree C
+tbar1=[3;10;30;50];//Reported average time in min
+XBbarr=[0.840;0.940;0.985;0.990];//Reported value of average conversion
+tbar=3;
+XBbar=0.840;//Average conversion for tbar = 3 mins
+
+//CALCULATION
+//Uniform-Reaction Model
+x=(1/tbar)*(1/(1-XBbar)-1);//Term KrCA of Eqn.(20)
+n=length(tbar1);
+i=1;
+while i<=n
+    XBbar1(i)=1-1/(1+x*tbar1(i));//Average conversion using calculated value of KrCA from Eqn.(20)
+    i=i+1;
+end
+
+//Shrinking-Core, Rection Control
+touguess=2;//Guess value of tou
+function[fn]=solver_func(tou)//Function defined for solving the system
+    fn=(1-XBbar)-(0.25*tou/tbar)+(0.05*(tou/tbar)^2)-((1/120)*(tou/tbar)^3);
+endfunction
+[tou]=fsolve(touguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou
+i=1;
+while i<=n
+    XBbar2(i)=1-(0.25*tou/tbar1(i))+(0.05*(tou/tbar1(i))^2)-((1/120)*(tou/tbar1(i))^3);//Average conversion using calculated value of tou from Eqn.(23)
+    i=i+1;
+end
+
+//Shrinking-Core, Diffusion Control
+touguess1=2;//Guess value of tou
+function[fn]=solver_func1(tou)//Function defined for solving the system
+    fn=(1-XBbar)-(1/5*tou/tbar)+(19/420*(tou/tbar)^2)-(41/4620*(tou/tbar)^3)+(0.00149*(tou/tbar)^4);
+endfunction
+[tou1]=fsolve(touguess1,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou
+i=1;
+while i<=n
+    //Average conversion using calculated value of tou from Eqn.(23)
+    XBbar3(i)=1-(1/5*tou1/tbar1(i))+(19/420*(tou1/tbar1(i))^2)-(41/4620*(tou1/tbar1(i))^3)+(0.00149*(tou1/tbar)^4);
+    i=i+1;
+end
+
+//OUTPUT
+printf('\n\t\t\t\tXBbar calculated for Models');
+printf('\nReported Data');
+printf('\ntbar(min)\tXBbar,obs\tUniform Reaction\tShrinking-Core, Rection Control\t\tShrinking-Core, Diffusion Control');
+i=1;
+while i<=n
+    mprintf('\n%f\t%f\t%f\t\t%f\t\t\t\t%f',tbar1(i),XBbarr(i),XBbar1(i),XBbar2(i),XBbar3(i));
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH18/EX18.4/Chap18_Ex4.sce b/497/CH18/EX18.4/Chap18_Ex4.sce
new file mode 100755
index 000000000..ea493c94e
--- /dev/null
+++ b/497/CH18/EX18.4/Chap18_Ex4.sce
@@ -0,0 +1,67 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-18, Example 4, Page 462
+//Title: Scale-up of a Reactor with Flowing Solids
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+W=1;//Bed weight in kg
+F1=0.01;//Solid feed rate in kg/min
+dp=[200;600];//Particle size in micrometer
+XBbar=[0.85;0.64];//Average conversion for corresponding particle sizes
+rhos=2500;//Density of solid in kg/m^3
+ephsilonm=0.4;//Void fracton of fixed bed
+F11=4;//Feed rate of solids in tons/hr
+XBbar1=0.98;
+dp1=600;
+pi=3.14;
+
+//CALCULATION
+//Shrinking-Core, Rection Control
+n=length(dp);
+i=1;
+touguess=2;//Guess value of tou
+while i<=n
+    function[fn]=solver_func2(tou)//Function defined for solving the system
+        fn=(1-XBbar(i))-(0.25*tou/107)+(0.05*(tou/107)^2)-((1/120)*(tou/107)^3);
+    endfunction
+    [tou(i)]=fsolve(touguess,solver_func2,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou
+    i=i+1;
+end
+tou1=tou(2);
+
+//For a single stage fluidized roaster
+tbar1=0.25*(tou1/(1-XBbar1))/60;//Mean residence time of solids in reactor in hr from Eqn.(24)
+W1=F11*tbar1;
+dtguess=2;//Guess value of tou
+function[fn]=solver_func3(dt)//Function defined for solving the system
+    fn=W1*10^3-(pi/4)*dt^2*0.5*dt*rhos*(1-ephsilonm);//Since Lm=0.5dt
+endfunction
+[dt]=fsolve(dtguess,solver_func3,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou
+Lm=dt/2;//Length of bed required
+
+//For a two-stage fluidized roaster
+tbar2=tou1*sqrt(1/(20*(1-XBbar1)))/60;//Mean residence time of solids in reactor in hr from Eqn.(30)
+W2=F11*tbar2;
+dtguess1=2;//Guess value of tou
+function[fn]=solver_func4(dt)//Function defined for solving the system
+    fn=W2*10^3-(pi/4)*dt^2*0.5*dt*rhos*(1-ephsilonm);//Since Lm=0.5dt
+endfunction
+[dt1]=fsolve(dtguess,solver_func4,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou
+Lm1=dt1/2;//Length of bed required
+
+//OUTPUT
+printf('\nSingle stage fluidized roaster');
+printf('\n\tWeight of bed needed:%ftons',W1);
+printf('\n\tDiameter of reactor:%fm',dt);
+printf('\n\tLength of bed:%fm',Lm);
+printf('\nTwo-stage fluidized roaster');
+printf('\n\tWeight of bed needed:%ftons',W2);
+printf('\n\tDiameter of reactor:%fm',dt1);
+printf('\n\tLength of bed:%fm',Lm1);
+printf('\nThese results show that this operation can be accomplished in a single bed of %ftons or in two beds of %f tons each.',W1,W2);
+
+//====================================END OF PROGRAM ======================================================
diff --git a/497/CH18/EX18.5/Chap18_Ex5.sce b/497/CH18/EX18.5/Chap18_Ex5.sce
new file mode 100755
index 000000000..b660d006b
--- /dev/null
+++ b/497/CH18/EX18.5/Chap18_Ex5.sce
@@ -0,0 +1,119 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-18, Example 5, Page 468
+//Title: Design of a Roaster for Finely Ground Ore
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+T=900;//Temperature in roaster in degree C
+P=101325;//Pressure in Pa
+R=8.314;//Universal gas constant
+dpbar=150;//Average particle size in micrometer
+rhosbar=4130;//Average particle density in kg/m^3
+kc=0.015//Rate constant in m/s for reaction which follows shrinking core model
+Ds=8E-6;//Diffusion coefficient of solid in m^2/s
+uo=0.6;//Superficial gas velocity in m/s
+D=2.3E-4;//Diffusion coefficient of gas in m^2/s
+Lm=1;//Length of fixed bed in m
+dte=0.4;//Equivalent diameter of bed
+umf=0.025;//Velocity at minimum fluidization condition in m/s
+ephsilonm=0.45;//Void fraction of fixed bed
+ephsilonmf=0.50;//Void fraction at minimum fluidized condition
+db=0.2;//Estimated bubble size in m
+gammab=0.005;//Ratio of volume of dispersed solids to that of bubble phase
+Fo=2;//Feed rate of solids in kg/s
+XA=0.6677;//Conversion of Oxygen
+xA=0.21;//Mole fraction of oxygen in feed
+mB=0.09744;//Molecular weight of ZnS
+F=0.85;//Fraction of open area
+g=9.81;//Acceleration due to gravity in square m/s^2
+pi=3.14;
+
+//CALCULATION
+//(a)Extreme Calculation
+a=3/2;//Stoichiometric coefficient of Oxygen in the reaction equation
+At=(Fo/mB)*(a)/(uo*(273/(T+273))*(XA*xA)/0.0224);
+dt=sqrt(At/F*4/pi);
+
+//(b)The Three-Step Procedure
+//Step 1. Conversion of gas
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+ub=1.6*{(uo-umf)+1.13*db^0.5}*dte^1.35+ubr;//Bubble rise velocity for Geldart B particle
+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=0.15;//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)
+x=delta*Lm*(1-ephsilonm)/((1-ephsilonf)*uo);//Term Lf/ub of Eqn.(12.16) from Eqn.(6.19)
+CAi=xA*P/(R*(T+273));//Initial concentration of oxygen
+
+//Step 2.Conversion of solids
+rhob=rhosbar/mB;//Density of ZnS
+kbar=(kc^-1+(dpbar*10^-6/(12*Ds))^-1)^-1;//Modified rate constant from Eqn.(11)
+tbar=At*Lm*(1-ephsilonm)*rhosbar/Fo;//Mean residence time of solids
+Krguess=2;//Guess value of Kr
+function[fn]=solver_func(Kr)//Function defined for solving the system
+    Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Reaction rate for fluidized bed from Eqn.(14)
+    XA=1-exp(-x*Kf);//Conversion of oxygen from Eqn.(42)
+    CAbar=(CAi*XA*uo)/(Kr*Lm*(1-ephsilonm));//Average concentration of oxygen from Eqn.(43)
+    tou=rhob*dpbar*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)
+    y=tbar/tou;//Term tbar/tou
+    XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)
+    //Step 3. Material balance of both streams
+    fn=(Fo/mB)*XBbar-(At*uo*CAi*XA/a);//From Eqn.(44b)
+endfunction
+[Kr]=fsolve(Krguess,solver_func,1E-6);//Using inbuilt function fsolve for solving for Kr
+Kf=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Reaction rate for fluidized bed from Eqn.(14)
+XA=1-exp(-x*Kf);//Conversion of oxygen from Eqn.(42)
+CAbar=(CAi*XA*uo)/(Kr*Lm*(1-ephsilonmf));//Average concentration of oxygen from Eqn.(43)
+tou=rhob*dpbar*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)
+y=tbar/tou;//Term tbar/tou
+XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)
+
+
+//(c) For other feed rates of solids
+F1=[2;2.5;3;3.5];//Various feed rates of solids in kg/s
+n=length(F1)
+i=1;
+Krguess1=2;//Guess value of Kr
+while i<=n
+    tbar1(i)=At*Lm*(1-ephsilonm)*rhosbar/F1(i);//Mean residence time of solids
+    function[fn]=solver_func1(Kr)//Function defined for solving the system
+        Kf1=gammab*Kr+1/((1/Kbc)+(1/(gammac*Kr+1/((1/Kce)+(1/(gammae*Kr))))));//Reaction rate for fluidized bed from Eqn.(14)
+        XA1=1-exp(-x*Kf1);//Conversion of oxygen from Eqn.(42)
+        CAbar1=(CAi*XA1*uo)/(Kr*Lm*(1-ephsilonm));//Average concentration of oxygen from Eqn.(43)
+        tou1=rhob*dpbar*10^-6*a/(2*kbar*CAbar1);//Time for complete reaction from Eqn.(9)
+        y1(i)=tbar1(i)/tou1;//Term tbar/tou
+        XBbar1(i)=3*y1(i)-6*y1(i)^2+6*y1(i)^3*(1-exp(-1/y1(i)));//Average conversion of ZnS from Eqn.(22)
+        //Step 3. Material balance of both streams
+        fn=(F1(i)/mB)*XBbar1(i)-(At*uo*CAi*XA1/a);//From Eqn.(44b)
+    endfunction
+    [Kr1(i)]=fsolve(Krguess1,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(23) for tou
+    Kf1(i)=gammab*Kr1(i)+1/((1/Kbc)+(1/(gammac*Kr1(i)+1/((1/Kce)+(1/(gammae*Kr1(i)))))));//Reaction rate for fluidized bed from Eqn.(14)
+    XA1(i)=1-exp(-x*Kf1(i));//Conversion of oxygen from Eqn.(42)
+    CAbar1(i)=(CAi*XA1(i)*uo)/(Kr1(i)*Lm*(1-ephsilonmf));//Average concentration of oxygen from Eqn.(43)
+    tou1(i)=rhob*dpbar*10^-6*a/(2*kbar*CAbar1(i));//Time for complete reaction from Eqn.(9)
+    y1(i)=tbar1(i)/tou1(i);//Term tbar/tou
+    XBbar1(i)=3*y1(i)-6*y1(i)^2+6*y1(i)^3*(1-exp(-1/y1(i)));//Average conversion of ZnS from Eqn.(22)
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nExtreme Calculation');
+printf('\n\tDiameter of tube with all its internals:%fm',dt);
+printf('\nThree step procedure');
+printf('\n\tConversion of ZnS:%f',XBbar);
+printf('\nFor other feed rates of solids');
+printf('\n\tFeed(kg/s)\ttbar(s)\t\tXBbar/XA\tKrbar(s^-1)\tCAbar/CAi\ttou(s)\t\tXA\t\tXB');
+i=1;
+while i<=n
+    mprintf('\n\t%f\t%f\t%f\t%f\t%f\t%f\t%f\t%f',F1(i),tbar1(i),XBbar1(i)/XA1(i),Kr1(i),CAbar1(i)/CAi,tou1(i),XA1(i),XBbar1(i));
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH18/EX18.6/Chap18_Ex6.sce b/497/CH18/EX18.6/Chap18_Ex6.sce
new file mode 100755
index 000000000..b8968e658
--- /dev/null
+++ b/497/CH18/EX18.6/Chap18_Ex6.sce
@@ -0,0 +1,69 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-18, Example 5, Page 471
+//Title: Design of a Roaster for Coarse Ore
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+T=900;//Temperature in roaster in degree C
+P=101325;//Pressure in Pa
+R=8.314;//Universal gas constant
+dp=750;//Particle size in micrometer5
+Fo=2.5;//Feed rate of solids in kg/s
+uo=0.6;//Superficial gas velocity in m/s
+W=80140;//Weight of bed in kg
+ephsilonmf=0.50;//Void fraction at minimum fluidized condition
+umf=0.5;//Velocity at minimum fluidization condition in m/s
+db=0.2;//Estimated bubble size in m
+g=9.81;//Acceleration due to gravity in square m/s^2
+Lm=1;//Length of fixed bed in m
+ephsilonm=0.45;//Void fraction of fixed bed
+xA=0.21;//Mole fraction of oxygen in feed
+kc=0.015//Rate constant in m/s for reaction which follows shrinking core model
+Ds=8E-6;//Diffusion coefficient of solid in m^2/s
+rhosbar=4130;//Average particle density in kg/m^3
+mB=0.09744;//Molecular weight of ZnS
+a=3/2;//Stoichiometric coefficient of Oxygen in the reaction equation
+
+//CALCULATION
+//Selection of models to represent reactor
+ubr=0.711*(g*db)^0.5;//Rise velocity of bubble from Eqn.(6.7)
+f=ubr/(umf/ephsilonmf);
+
+//Step 1.
+ub=uo-umf+ubr;//Rise velocity of bubbles from Eqn.(6.8)
+delta=(uo-umf)/(ub+2*umf);//Fraction of the bed in bubbles from Eqn.(6.26)
+Krguess=2;//Guess value of Kr
+x=Lm*(1-ephsilonm)*umf*(1-delta)/uo^2;
+CAi=xA*P/(R*(T+273));//Initial concentration of oxygen
+
+//Step 2.
+kbar=(kc^-1+(dp*10^-6/(12*Ds))^-1)^-1;//Modified rate constant from Eqn.(11)
+tbar=W/Fo;//Mean residence time of solids from Eqn.(14.2)
+rhob=rhosbar/mB;//Density of ZnS
+function[fn]=solver_func1(Kr)//Function defined for solving the system
+    XA=1-exp(-x*Kr);//Conversion from Eqn.(42)
+    CAbar=(CAi*XA*uo^2)/(Kr*Lm*(1-ephsilonm)*umf*(1-delta));//Average concentration of oxygen from Eqn.(43)
+    tou=rhob*dp*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)
+    y=tbar/tou;//Term tbar/tou
+    XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)
+    //Step 3.
+    fn=XBbar-1.2*XA;//From Table E5, for Fo=2.5kg/s
+endfunction
+[Kr]=fsolve(Krguess,solver_func1,1E-6);//Using inbuilt function fsolve for solving for Kr
+XA=1-exp(-x*Kr);//Conversion from Eqn.(42)
+CAbar=(CAi*XA*uo^2)/(Kr*Lm*(1-ephsilonm)*umf*(1-delta))//Average concentration of oxygen from Eqn.(43)
+tou=rhob*dp*10^-6*a/(2*kbar*CAbar);//Time for complete reaction from Eqn.(9)
+y=tbar/tou;//Term tbar/tou
+XBbar=3*y-6*y^2+6*y^3*(1-exp(-1/y));//Average conversion of ZnS from Eqn.(22)
+
+//OUTPUT
+printf('\nSelection of models to represent reactor');
+printf('\n\tSince ratio ubr/(umf/ephsilonmf)= %f <1, the reactor is operating in slow bubble regime',f);
+printf('\n\tSince particle size =%f micrometer, they react according to shrinking-core model',dp);
+printf('\n\tConversion obtained for %f micrometer particle:%f',dp,XBbar);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH3/EX3.1/Chap3_Ex1.sce b/497/CH3/EX3.1/Chap3_Ex1.sce
new file mode 100755
index 000000000..bf9a1f171
--- /dev/null
+++ b/497/CH3/EX3.1/Chap3_Ex1.sce
@@ -0,0 +1,28 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-3, Example 1, Page 68
+//Title: Size Measure of Nonuniform Solids
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+weight = [0;60;150;270;330;360];// Weight in grams for the oversized particles
+psize = [50;75;100;125;150;175];//PSD in micrometers
+
+//CALCULATION
+len = length(psize); // To obtain the size of input array
+// Computation of sauter mean diameter for the given PSD
+i = 1;
+while i<len
+        dpi(i)=(psize(i,:)+ psize(i+1,:))/2;
+        weightf(i)=(weight(i+1)-weight(i))/weight(6);    
+        dp(i)=weightf(i)/dpi(i);    
+        i=i+1;
+end                     
+dpbar=1/sum(dp);//Calculation of average particle daimeter Eq.(15)
+
+//OUTPUT
+mprintf('\n The Sauter mean diameter of the material with the given particle size distribution = %f micrometer',dpbar);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH3/EX3.2/Chap3_Ex2.sce b/497/CH3/EX3.2/Chap3_Ex2.sce
new file mode 100755
index 000000000..664f0bdd4
--- /dev/null
+++ b/497/CH3/EX3.2/Chap3_Ex2.sce
@@ -0,0 +1,37 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-3, Example 2, Page 76
+//Title: Estimation of Minimum fluidizing velocity
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+ephsilon=0.55;//Void fraction of bed
+rhog=0.0012;//Density of gas in g/cc
+myu=.00018;//Viscosity of gas in g/cm s
+dpbar=0.016;//Mean diameter of solids in centimeter
+phis=0.67;//Sphericity of solids
+rhos=2.6;//Density of solids in g/cc
+g=980;//Acceleration due to gravity in square cm/s^2
+
+//CALCULATION
+//Computation of umf using the simplified equation for small particles
+umf=((dpbar^2)*(rhos-rhog)*g*(ephsilon^3)*(phis^2))/(150*myu*(1-ephsilon));//Simplified equation to calculate minimum fluidizing velocity for small particles Eq.(21)
+Re=(dpbar*umf*rhog)/myu;//To calculate Reynolds number for particle
+
+//Computation of umf if neither void fraction of bed nor sphericity is known
+c1=28.7; c2=0.0494;//Value of constants from Table 4, page 70
+umf1=(myu/(dpbar*rhog))*(((c1^2)+((c2*(dpbar^3)*rhog*(rhos-rhog)*g)/(myu^2)))^0.5-c1);//Equation to calculate minimum fluidizing velocity for coarse particles Eq.(25)
+err=((umf-umf1)/umf)*100;//Calculation of error from experimental value
+
+//OUTPUT
+if Re<20 then 
+    mprintf('\nThe particle Reynolds no = %f',Re)
+    printf('\nThe simplified equation used for calculating minimum fluidizing velocity is valid.');
+end
+mprintf('\nThe minimum fluidizing velocity by simplified equation for small particles = %fcm/s',umf);
+mprintf('\nThe minimum fluidizing velocity by equation for coarse partilces = %fcm/s',umf1);
+mprintf('\nThis value is %f percent below the experimentally reported value.',err);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH3/EX3.3/Chap3_Ex3.sce b/497/CH3/EX3.3/Chap3_Ex3.sce
new file mode 100755
index 000000000..17ddf2f34
--- /dev/null
+++ b/497/CH3/EX3.3/Chap3_Ex3.sce
@@ -0,0 +1,28 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-3, Example 3, Page 82
+//Title: Estimation of terminal velocity of falling particles
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+rhog=1.2e-3;//Density of air in g/cc
+myu=1.8e-4//Viscosity of air in g/cm s
+dpbar=0.016//Mean diameter of solids in centimeter
+phis=0.67;//Sphericity of solids
+rhos=2.6;//Density of solids in g/cc
+g=980//Acceleration due to gravity in square cm/s^2
+
+//CALCULATION
+dpstar=dpbar*((rhog*(rhos-rhog)*g)/myu^2)^(1/3);//Calculation of dimensionless particle size Eq.(31)
+utstar=((18/(dpstar^2))+(2.335-(1.744*phis))/(dpstar^0.5))^-1;//Calculation of dimensionless gas velocity Eq.(33)
+ut=utstar*((myu*(rhos-rhog)*g)/rhog^2)^(1/3);//Calculation of terminal velocity of falling particles Eq.(32)
+
+
+//OUTPUT
+mprintf('\nThe dimensionless particle size = %f', dpstar);
+mprintf('\nThe dimensionless gas velocity = %f', utstar);
+mprintf('\nThe terminal velocity of falling particles = %fcm/s', ut);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH3/EX3.4/Chap3_Ex4.sce b/497/CH3/EX3.4/Chap3_Ex4.sce
new file mode 100755
index 000000000..9a5865a50
--- /dev/null
+++ b/497/CH3/EX3.4/Chap3_Ex4.sce
@@ -0,0 +1,47 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-3, Example 4, Page 91
+//Title: Prediction of flow regime
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+rhos=1.5;//Density of Solid in g/cc
+uo1=40; uo2=80;//Superficial gas velocity in cm/s
+dp1=0.006; dp2=0.045;//Particle size in centimeter
+rhog1=1.5E-3; rhog2=1E-3; //Density of gas in g/cc
+myu1=2E-4; myu2=2.5E-4;//Viscosity of air in g/cm s
+g=980;//Acceleration due to gravity in square cm/s^2
+
+//CALCULATION
+//for smaller particles
+dpstar1=dp1*((rhog1*(rhos-rhog1)*g)/myu1^2)^(1/3);//Calculation of dimensionless particle diamter Eq.(31)
+uostar1=uo1*((rhog1^2)/((myu1)*(rhos-rhog1)*g))^(1/3);
+uostar2=uo2*((rhog1^2)/((myu1)*(rhos-rhog1)*g))^(1/3);//Calculation of dimensionless superficial gas velocity Eq.(32)
+
+//for larger particles 
+dpstar2=dp2*((rhog2*(rhos-rhog2)*g)/myu2^2)^(1/3);//Calculation of dimensionless particle diamter Eq.(31)
+uostar3=uo1*((rhog2^2)/((myu2)*(rhos-rhog2)*g))^(1/3);
+uostar4=uo2*((rhog2^2)/((myu2)*(rhos-rhog2)*g))^(1/3);//Calculation of dimensionless superficial gas velocity Eq.(32)
+
+
+//OUTPUT
+printf('\nFor particle of size %f centimeter',dp1);
+mprintf('\nThe dimensionless particle diameter = %f',dpstar1);
+mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar1,uo1);
+mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar2,uo2);
+mprintf('\n\nFrom Fig.16(page 89)comparing u*=%f vs dp*=%f',uostar1,dpstar1);
+mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Onset of turbulent fluidization in an ordinary bubbling bed',uo1);
+mprintf('\nFrom Fig.16(page 89)comparing u* =%f vs dp* =%f',uostar2,dpstar1);
+mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Fast fluidization(requires a circulating solid system)',uo2);
+printf('\n\nFor particle of size %f centimeter',dp2)
+mprintf('\nThe dimensionless particle diameter = %f',dpstar2);
+mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar3,uo1);
+mprintf('\nThe dimensionless superficial gas velocity = %fcm/s(for superficial gas velocity of %fcm/s)',uostar4,uo2);
+mprintf('\n\nFrom Fig.16(page 89)comparing u*=%f vs dp*=%f',uostar3,dpstar2);
+mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Bublling Fluidization',uo1);
+mprintf('\nFrom Fig.16(page 89)comparing u* =%f vs dp* =%f',uostar4,dpstar2);
+mprintf('\nFor Superficial gas velocity =%f \nMode of Fluidization:Bubbling Fluidization',uo2);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH4/EX4.1/Chap4_Ex1.sce b/497/CH4/EX4.1/Chap4_Ex1.sce
new file mode 100755
index 000000000..ae7ee1021
--- /dev/null
+++ b/497/CH4/EX4.1/Chap4_Ex1.sce
@@ -0,0 +1,72 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-4, Example 1, Page 106
+//Title: Design of a Perforated Plate Distributor
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dt=4;//Vessel diameter in m
+Lmf=2;//Length of the bed in m
+ephsilonmf=0.48;//Void fraction of bed
+rhos=1500;//Density of solid in kg/m^3
+rhog=3.6;//Density of gas in kg/m^3
+myu=2E-5;//Viscosity of gas in kg/m s
+po=3;//Pressure of inlet gas in bar
+uo=0.4;//Superficial velocity of gas in m/s
+uorm=40;//Maximum allowable jet velocity from holes in m/s
+g=9.80;//Acceleration due to gravity in m/s^2
+gc=1;
+pi=3.1428;
+
+//CALCULATION
+//Computation of minimum allowable pressure drop through the distributor
+deltapb={(1-ephsilonmf)*(rhos-rhog)*g*Lmf}/gc;//Calculation of pressure drop in bed using Eqn.(3.17)
+deltapd=0.3*deltapb;//Calculation of pressure drop in distributor using Eqn.(3)
+
+//Computation of orifice coefficient
+Ret=(dt*uo*rhog)/myu;
+if    Ret>=3000 then Cd=0.60;
+elseif    Ret>=2000 then Cd=0.61;
+elseif    Ret>=1000 then Cd=0.64;
+elseif    Ret>=500  then Cd=0.68;
+elseif    Ret>=300  then Cd=0.70;
+elseif    Ret>=100  then Cd=0.68;
+end
+
+//Computation of gas velocity through orifice
+uor=Cd*((2*deltapd)/rhog)^0.5;//Calculation of gas velocity through orifice by using Eqn.(12)
+f=(uo/uor)*100;//Calculation of fraction of open area in the perforated plate 
+
+
+//Computation of number of orifices per unit area of distributor
+dor=[0.001;0.002;0.004];//Different orifice diameters in m
+n=length(dor);
+i=1;
+while i<=n
+    Nor(i)=(uo*4)/(pi*uor*(dor(i))^2);//Calculation of number of orifices by using Eqn.(13)
+    i=i+1;
+end
+    
+//OUTPUT
+mprintf('\nThe pressure drop in bed:%fPa',deltapb);
+mprintf('\nThe minimum allowable pressure drop in distributor:%fPa',deltapd);
+if uor<uorm then mprintf('\nThe gas veleocity of %fm/s is satisfactory',uor);
+    else mprintf('\nThe gas veleocity of %fm/s is not satisfactory',uor);
+end
+if f<10 then mprintf('\nThe fraction of open area of %f percent is allowable',f);
+    else mprintf('\nThe fraction of open area of %f percent is not allowable',f);
+end   
+printf('\nDiameter of orifice(m)');
+printf('\tNumber of orifices per unit area(per sq.m)');
+j=1;
+while j<=n
+    mprintf('\n%f',dor(j));
+    mprintf('\t\t%f',Nor(j));
+    j=j+1;
+end
+printf('\nThis number can be rounded off.');
+printf('\nSince orifices that are too small are liable to clog and those that are too large cause uneven distribution of gas, we choose orifice of diameter %fm',dor(2));
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH4/EX4.2/Chap4_Ex2.sce b/497/CH4/EX4.2/Chap4_Ex2.sce
new file mode 100755
index 000000000..53e00c02a
--- /dev/null
+++ b/497/CH4/EX4.2/Chap4_Ex2.sce
@@ -0,0 +1,50 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-4, Example 2, Page 108
+//Title: Design of a Tuyere Distributor
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+lor=0.1;//Minimum allowable tuyere spacing in m
+uorm=30;//Maximum allowable jet velocity from the tuyere in m/s
+uo=0.4;//Superficial velocity of gas in m/s
+uor=30.2;//Gas velocity through orifice,from Exa 1, in m/s
+Cd=0.6;//Dicharge coefficient from Exa 1
+rhog=3.6//Density of gas in kg/m^3
+pi=3.1428;
+
+//CALCULATION
+Nor=1/(lor^2);//Calculation of number of orifices per unit area by assuming minimum spacing for tuyeres
+dor={(4/pi)*(uo/uor)*(1/Nor)}^0.5;//Calculation of diameter of inlet orifiec by using Eqn.(13)
+
+//Computation of diameter of hole for different number of holes per tuyere
+q=(lor^2)*uo;//Volumetric flow rate in m^3/s
+Nh=[8;6;4];//Different number of holes per tuyere
+n=length(Nh);
+i=1;
+while i<=n
+    dh(i)=((((q/Nh(i))*(4/pi))/uorm)^0.5);//Calculation of diameter of holes
+    i=i+1;
+end
+deltaph=(rhog/2)*((uor/Cd)^2);
+
+//OUTPUT
+printf('\nNumber of holes(number of holes/tuyeres)');
+printf('\tDiameter of hole(m)');
+j=1;
+while j<=n
+    mprintf('\n%f',Nh(j));
+    mprintf('\t\t\t\t\t%f',dh(j));
+    j=j+1;
+end
+printf('\nThe design chosen is as follows');
+printf('\n\tTuyeres are as shown in Fig.2(b),page 97');
+mprintf('\n\tNumber of holes = %f(Since rectangular pitch is chosen for tuyeres)',Nh(2));
+mprintf('\n\tDiameter of hole = %fm',dh(2));
+mprintf('\n\tDiameter of incoming high-pressure-drop orifice = %fm ID',dor);
+printf('\nChecking the pressure drop in tuyeres');
+mprintf('\nSince pressure drop of %fPa gives sufficiently high distributor pressure drop as seen in Exa.1, use of inlet orifice can be dispensed.',deltaph);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH4/EX4.3/Chap4_Ex3.sce b/497/CH4/EX4.3/Chap4_Ex3.sce
new file mode 100755
index 000000000..85ab5bbe9
--- /dev/null
+++ b/497/CH4/EX4.3/Chap4_Ex3.sce
@@ -0,0 +1,59 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-4, Example 3, Page 110
+//Title: Power Requirement for a Fluidized Coal Combustor(FBC)
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+deltapd=[3;10]//Distributor pressure drop in kPa
+deltapd2=10;//Distributor pressure drop in kPa
+po=101;//Entering air pressure in kPa
+To=20;//Entering air temperature in degree C
+y=1.4;//Fugacity of air
+deltapb=10;//Pressure drop in bed in kPa
+p3=103;//Pressure at the bed exit in kPa
+F=8;//Feed rate of coal in tons/hr
+H=25;//Gross heatig value of coal in MJ/kg
+Fa=10;//Air required at standard condition in nm^3/kg
+etac=0.75;//Efficiency of compressor
+etap=36;//Efficiency of plant in %
+
+//CALCULATION
+//Calculation of volumetric flow rate of air
+vo=((F*1000)*Fa*((To+273)/273))/3600;
+
+//Case(a) Distributor Pressure drop = 3kPa and Case(b) Distributor Pressure drop = 10kPa
+n=length(deltapd);
+i=1;
+while i<=n
+    p2(i)=p3+deltapb;//Calculation of pressure at the entrance of the bed
+    p1(i)=p2(i)+deltapd(i);//Calculation of pressure before entering the bed
+    ws(i)=(y/(y-1))*po*vo*((p1(i)/po)^((y-1)/y)-1)*(1/etac);//Calculation of power required for the compressor by Eqn.(18) & Eqn.(20)
+    i=i+1;
+end
+
+//Case(c) 50% of the required bypassed to burn the volatile gases. Distributor Pressure drop = 3kPa
+//No change in pressure drop from case(a)
+v1=vo/2;//New volumetric flow rate of air
+ws1=ws(1)/2;//Power required for blower for primary air
+ws2=(y/(y-1))*po*v1*((p3/po)^((y-1)/y)-1)*(1/etac);//Power required for blower for bypassed air
+wst=ws1+ws2;//Total power required for the two blowers
+p=((ws(1)-wst)/ws(1))*100;//Saving in power when compared to case(a)
+
+//OUTPUT
+printf('\nCase(a)');
+mprintf('\n\tVolumetric flow rate of air = %f m^3/hr',vo);
+mprintf('\n\tPower required for compressor = %f kW',ws(1));
+printf('\nCase(b)');
+mprintf('\n\tVolumetric flow rate of air = %f m^3/hr',vo);
+mprintf('\n\tPower required for compressor = %f kW',ws(2));
+printf('\nCase(c)');
+mprintf('\n\tVolumetric flow rate of air = %f m^3/hr',v1);
+mprintf('\n\tPower required for compressor for primary air = %f kW',ws1);
+mprintf('\n\tPower required for blower for bypassed air = %f kW',ws2);
+mprintf('\n\tTotal power required for the two blowers = %f kW',wst);
+mprintf('\n\tPower saved compared to case(a) = %f percent',p);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH5/EX5.1/Chap5_Ex1.sce b/497/CH5/EX5.1/Chap5_Ex1.sce
new file mode 100755
index 000000000..beb36cfbe
--- /dev/null
+++ b/497/CH5/EX5.1/Chap5_Ex1.sce
@@ -0,0 +1,33 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-5, Example 1, Page 126
+//Title: Charactersitics of a Single Bubble
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dt=60;//ID of tube in cm 
+dp=300;//Size of particles of bed in micrometers
+umf=3;//Velocity at minimum fluidization condition in cm/s
+ephsilonmf=0.5;//Void fraction of bed at minimum fluidization condition
+db=5;//Diameter of bubble in cm
+g=980;//Acceleration due to gravity in cm/s^2
+
+//CALCULATION
+//Computation of rise velocity of bubble
+if (db/dt)<0.125    then ubr=(0.711*((g*db)^0.5));//Rise velocity by Eqn.(3)
+elseif (db/dt)<0.6  then ubr=(0.711*((g*db)^0.5))*1.2*exp(-1.49*(db/dt));//Rise velocity by Eqn.(4)   
+end
+
+//Computation of cloud thickness
+Rb=db/2;//Radius of bubble
+uf=umf/ephsilonmf;//Velocity of emulsion gas
+Rc=Rb*((ubr+(2*uf))/(ubr-uf))^(1/3);//Radius of cloud by Eqn.(6)
+
+//OUTPUT
+mprintf('\nThe rise velocity of the bubble=%fcm/s',ubr);
+mprintf('\nThe cloud thickness=%fcm',Rc-Rb);
+mprintf('\nFrom Fig.8(page 124)comparing fw vs dp, for dp = %f micrometer, wake fraction = 0.24',dp);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH5/EX5.2/Chap5_Ex2.sce b/497/CH5/EX5.2/Chap5_Ex2.sce
new file mode 100755
index 000000000..ee26069eb
--- /dev/null
+++ b/497/CH5/EX5.2/Chap5_Ex2.sce
@@ -0,0 +1,29 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-5, Example 2, Page 132
+//Title: Initial Bubble Size at a Distributor
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+uo=15;//Superificial gas velocity in cm/s
+umf=1;////Velocity at minimum fluidization condition in cm/s
+lor=2;//Pitch of perforated plate in cm
+g=980;//Acceleration due to gravity in cm/s^2
+//CALCULATION
+//Case(a) For porous plate
+dbo1=(2.78/g)*(uo-umf)^2;//Initial bubble size using Eqn.(19)
+
+//Case(b) For Perforated plate
+Nor=(2/sqrt(3))*(1/lor)^2;//Number of orifices in cm^-2
+dbo2=(1.30/(g^0.2))*((uo-umf)/Nor)^0.4;//Initial bubble size using Eqn.(15) assuming inital bubble size is smaller than hole spacing
+
+//OUTPUT
+printf('\nCase(a) For porous plate');
+printf('\n\tInitial bubble size=%fcm',dbo1);
+printf('\nCase(b) For Perforated plate');
+printf('\n\tInitial bubble size=%fcm',dbo2);
+printf('\n\tSince %f<%f, the equation used is correct.',dbo2,lor);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH6/EX6.1/Chap6_Ex1.sce b/497/CH6/EX6.1/Chap6_Ex1.sce
new file mode 100755
index 000000000..99d83c751
--- /dev/null
+++ b/497/CH6/EX6.1/Chap6_Ex1.sce
@@ -0,0 +1,37 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-6, Example 1, Page 150
+//Title: Bubble Size and Rise Velocity in Geldart A Beds
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+z=0.5;//Height of bed in m
+dt=0.5;//ID of tube in m
+rhos=1.6;//Density of catalyst in g/cm^3
+dpbar=60;//Averge catalyst diameter in micrometer
+umf=0.002;//Velocity at minimum fluidization condition in m/s
+uo=0.2;//Superficial velocity in m/s
+dor=2;//Diameter of orifice in mm
+lor=20;//Pitch of perforated plate in mm
+g=9.80;//g=980;//Acceleration due to gravity in m/s^2
+
+//CALCULATION
+//Method 1. Procedure using Eqn.(10) & Eqn.(11)
+db=(0.035+0.040)/2;//Bubble size at z=0.5m from Fig.7(a) & Fig.7(b)
+ub1=1.55*((uo-umf)+14.1*(db+0.005))*(dt^0.32)+0.711*(g*db)^0.5;//Bubble velocity using Eqn.(10) & Eqn.(11)
+
+//Method 2. Werther's procedure
+si=0.8;//From Fig.6 for Geldart A solids 
+ub2=si*(uo-umf)+(3.2*(dt^(1/3)))*(0.711*(g*db)^0.5);//Bubble velocity using Eqn.(9)
+
+//OUTPUT
+printf('\nMethod 1. Procedure using Eqn.(10) & Eqn.(11)');
+mprintf('\n\tDiameter of the bubble=%fm',db);
+mprintf('\n\tRise velocity of the bubble=%fm/s',ub1);
+printf('\nMethod 2. Werthers procedure');
+mprintf('\n\tDiameter of the bubble=%fm',db);
+mprintf('\n\tRise velocity of the bubble=%fm/s',ub2);
+
+//====================================END OF PROGRAM ======================================================
diff --git a/497/CH6/EX6.2/Chap6_Ex2.sce b/497/CH6/EX6.2/Chap6_Ex2.sce
new file mode 100755
index 000000000..84ee3b545
--- /dev/null
+++ b/497/CH6/EX6.2/Chap6_Ex2.sce
@@ -0,0 +1,81 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-6, Example 2, Page 151
+//Title: Bubble Size and Rise Velocity in Geldart B Beds
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+z=0.5;//Height of bed in m
+dt=0.5;//ID of tube in m
+rhos=2.6;//Density of catalyst in g/cm^3
+dpbar=100;//Averge catalyst diameter in micrometer
+umf=0.01;//Velocity at minimum fluidization condition in m/s
+uo=0.45;//Superficial velocity in m/s
+dor=2;//Diameter of orifice in mm
+lor=30;//Pitch of perforated plate in mm
+g=9.80;//Acceleration due to gravity in m/s^2
+pi=3.142857;
+
+//CALCULATION
+//Part(a).Bubble Size
+Nor=(2/sqrt(3))*(1/lor^2);
+dbo=5.5;
+
+//Method 1.Werther's procedure for finding bubble size
+z1=[0;5;10;20;30;50;70];
+n=length(z1);
+i=1; 
+while i<=n
+    db(i)=0.853*((1+0.272*(uo-umf)*100)^(1/3))*(1+0.0684*z1(i))^1.21;
+    i=i+1;    
+end
+db1=0.163;//Since bubble size starts at dbo=5.5cm at z=0, we shift the curve accordingly to z=0.5m
+
+//Method 2.Mori and Wen's procedure for finding bubble size
+dbm=0.65*((pi/4)*((dt*100)^2)*(uo-umf)*100)^0.4;
+db2=dbm-(dbm-dbo)*exp(-0.3^(z/dt));
+
+//Part(b).Bubble Velocity
+//Method 1.Procedure using Eqn.(12)
+ub1=1.6*((uo-umf)+1.13*db1^0.5)*(dt^1.35)+(0.711*(g*db1)^0.5);
+
+//Method 2.Werther's Procedure
+si=0.65;
+ub2=si*(uo-umf)+2*(dt^0.5)*(0.711*(g*db1)^0.5);
+
+//Using Eqn.(7) & Eqn.(8)
+ubr1=0.711*(g*db1)^0.5;
+ubr2=0.711*(g*db2/100)^0.5
+ub3=uo-umf+ubr1;
+ub4=uo-umf+ubr2;
+
+//OUTPUT
+printf('\nBubble Size');
+mprintf('\nInitial bubble size from Fig.5.14 for %fm/s = %fcm',uo-umf,dbo);
+printf('\n\n\tMethod 1.Werthers procedure for finding bubble size');
+printf('\n\t\tHeight of bed(cm)');
+printf('\t\t\tBubble size(cm)');
+m=length(z1);
+j=1;
+while j<=m
+    mprintf('\n\t\t%f',z1(j));
+    mprintf('\t\t\t\t%f',db(j));
+    j=j+1;
+end
+printf('\n\n\tMethod 2.Mori and Wens procedure for finding bubble size');
+mprintf('\n\t\tMaximum expected bubble size=%fcm',dbm);
+mprintf('\n\t\tBubble size=%fcm',db2);
+printf('\nBubble Velocity');
+printf('\n\n\tMethod 1.Procedure using Eqn.(12)');
+mprintf('\n\t\tBubble velocity=%fm/s',ub1);
+printf('\n\n\tMethod 2.Werthers procedure');
+mprintf('\n\t\tBubble velocity=%fm/s',ub2);
+printf('\nComparing the above results with the expressions of the simple two-phase theory');
+printf('\n\tWerthers bubble size');
+mprintf('\tBubble rise velocity=%fm/s\tBubble velocity=%fm/s',ubr1,ub3);
+printf('\n\tMori & Wens bubble size');
+mprintf('\tBubble rise velocity=%fm/s\tBubble velocity=%fm/s',ubr2,ub4);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH6/EX6.3/Chap6_Ex3.sce b/497/CH6/EX6.3/Chap6_Ex3.sce
new file mode 100755
index 000000000..c43313ca3
--- /dev/null
+++ b/497/CH6/EX6.3/Chap6_Ex3.sce
@@ -0,0 +1,36 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-6, Example 3, Page 153
+//Title: Scale-down of a Commercial Chlorinator
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dpbar=53;//Average particle size in micrometer
+s=[1;2];//Size of Bermuda rock in cm 
+rhosbar=3200;//Average solid density of the coke-zircon mixture in kg/m^3
+ephsilonm=0.5;//Void fraction for fixed bed
+ephsilonf=0.75;//Void fraction for bubbling bed
+rhogbar=0.64;//Average density of gas in kg/m^3
+uo=14;//Superficial gas velocity in cm/s
+myu=5E-5;//Viscosity of gas in kg/m s
+T=1000;//Temperature in degree C
+P=1;//Pressure in atm
+dt=91.5;//ID of bed in cm
+sh=150;//Slumped height in cm
+
+//CALCULATION
+rhog2=1.2;//Density of ambient air
+myu2=1.8E-5;//Viscosity of ambient air
+rhos2=rhog2*(rhosbar/rhogbar);//For the requirement of constant density ratio
+m=((rhogbar*myu2)/(rhog2*myu))^(2/3);//Scale factor by usin Eqn.(16)
+u2=(m^0.5)*uo;//Superficial gas velocity by using Eqn.(17)
+//OUTPUT
+printf('\nFor the model use');
+mprintf('\n\tBed of ID %fcm\n\tSlumped bed height of %fcm\n\tPacked bed distributor consisting of %f-%fmm rock',m*dt,m*sh,m*s(1),m*s(2));
+mprintf('\nFluidizing gas: ambient air at %fatm',P);
+mprintf('\nSolids: \tzirconia, Average particle size=%fmicrometers',m*dpbar);
+mprintf('\nEntering gas:\tSuperficial velocity=%fcm/s',u2);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH6/EX6.4/Chap6_Ex4.sce b/497/CH6/EX6.4/Chap6_Ex4.sce
new file mode 100755
index 000000000..4ddea92e2
--- /dev/null
+++ b/497/CH6/EX6.4/Chap6_Ex4.sce
@@ -0,0 +1,116 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-6, Example 4, Page 159
+//Title: Reactor Scale-up for Geldart A Catalyst
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dtb=20;//ID of bench-scale reactor
+dtp=1;//ID of pilot reactor
+dpbar=52;//Average particle size in micrometer
+ephsilonm=0.45;//Void fraction for fixed bed
+ephsilonmf=0.50;//Void fraction at minimum fluidization condition
+ephsilonmb=0.60;//Void fraction 
+uo=30;//Superficial gas velocity in cm/s
+Lmb=2;//Length of fixed bed in m
+umf=0.33;//Velocity at minimum fluidization condition in cm/s
+umb=1;//Velocity at in cm/s
+db=3;//Equilibrium bubble size in cm
+g=9.80;//Acceleration due to gravity in m/s^2
+pi=3.142857;
+
+//CALCULATION
+ubr=0.711*(g*db/100)^0.5;//Rise velocity of bubble using Eqn.(7)
+
+//Bubble velocity for the bench unit
+ubb1=1.55*(((uo-umf)/100)+14.1*((db/100)+0.005))*((dtb/100)^0.32)+ubr;//Bubble velocity using Eqn.(11)
+si=1;
+ubb2=si*((uo-umf)/100)+(3.2*((dtb/100)^(1/3)))*ubr;//Bubble velocity using Eqn.(9)
+ubb=(ubb1+ubb2)/2;//Average bubble velocity
+
+//Bubble velocity for the pilot unit
+ubp1=1.55*(((uo-umf)/100)+14.1*((db/100)+0.005))*(dtp^0.32)+ubr;//Bubble velocity using Eqn.(11)
+si=1;
+ubp2=si*((uo-umf)/100)+(3.2*(dtp^(1/3)))*ubr;//Bubble velocity using Eqn.(9)
+ubp=(ubp1+ubp2)/2;//Average bubble velocity
+
+//Rise velocity of upflowing emulsion
+ueb=ubb-ubr;//For the bench unit
+uep=ubp-ubr;//For the pilot unit
+
+//Scale-Up Alternative 1.
+dteb=20;//Effective bubble diameter
+dib=[5;10;15;20];//Different outside diameters
+n=length(dib);
+i=1;
+while i<=n
+    li(i)=sqrt(((pi*dib(i)*dteb)/4)+((pi/4)*(dib(i))^2));//Pitch using Eqn.(13)
+    i=i+1;
+end    
+
+//Scale-Up Alternative 2.
+Lmp=Lmb*(ubp/ubb);//Static bed height of commercial unit
+dtep=100;//Effective bubble diameter
+dip=[10;15;20;25];//Different outside diameters
+m=length(dip);
+i=1;
+while i<=m
+    lip(i)=sqrt(((pi*dip(i)*dtep)/4)+(pi/4)*dip(i));//Pitch using Eqn.(13)
+    i=i+1;
+end    
+
+//Height of Bubbling beds
+//For bench unit
+deltab=((uo/100)-(umb/100))/(ubb-(umb/100));//Fraction of bed in bubbles using Eqn.(28)
+ephsilonfb=deltab+(1-deltab)*ephsilonmb;//Void fraction of bubbling bed using Eqn.(20)
+Lfb=Lmb*(1-ephsilonm)/(1-ephsilonfb);//Hieght of bubbling bed usnig Eqn.(19)
+//For pilot unit
+deltap=((uo/100)-(umb/100))/(ubp-(umb/100));//Fraction of bed in bubbles using Eqn.(28)
+ephsilonfp=deltap+(1-deltap)*ephsilonmb;//Void fraction of bubbling bed using Eqn.(20)
+Lfp=Lmp*(1-ephsilonm)/(1-ephsilonfp);//Hieght of bubbling bed usnig Eqn.(19)
+
+//OUTPUT
+mprintf('\nRise velocity of bubble=%fm/s',ubr);
+printf('\nFor the bench unit');
+mprintf('\n\tWith Eqn.(11), Rise velocity=%fm/s',ubb1);
+mprintf('\n\tWith Werthers procedure, Rise velocity=%fm/s',ubb2);
+mprintf('\n\tAverage rise velocity=%fm/s',ubb);
+mprintf('\n\tRise velocity of upflowing emulsion=%fm/s',ueb);
+printf('\nFor the pilot unit');
+mprintf('\n\tWith Eqn.(11), Rise velocity=%fm/s',ubp1);
+mprintf('\n\tWith Werthers procedure, Rise velocity=%fm/s',ubp2);
+mprintf('\n\tAverage rise velocity=%fm/s',ubp);
+mprintf('\n\tRise velocity of upflowing emulsion=%fm/s',uep);
+printf('\nScale-Up Alternative 1.');
+printf('\n\tOuter diameter of tube(cm)');
+printf('\tPitch(cm)');
+n=length(dib);
+j=1;
+while j<=n
+    mprintf('\n\t\t%f',dib(j));
+    mprintf('\t\t\t%f',li(j));
+    j=j+1;
+end
+printf('\n\tSuitable arrangement');
+mprintf('\n\t\tOuter Diameter=%fcm\tPitch:Diameter ratio=%f',dib(2),(li(2)/dib(2)));
+printf('\nScale-Up Alternative 2.');
+mprintf('\n\tStatic bed height for commercial unit=%fm',Lmp);
+printf('\n\tOuter diameter of tube(cm)');
+printf('\tPitch(cm)');
+n=length(dip);
+j=1;
+while j<=n
+    mprintf('\n\t\t%f',dip(j));
+    mprintf('\t\t\t%f',lip(j));
+    j=j+1;
+end
+printf('\n\tSuitable arrangement');
+mprintf('\n\t\tOuter Diameter=%fcm\tPitch:Diameter ratio=%f',dip(2),(lip(2)/dip(2)));
+printf('\n\n\t\t\t\tFraction of bed in bubbles\tVoid fraction of bed\tStatic bed height(m)\tHeight of bubbling bed(m)');
+printf('\n\t\t\t\t---------------------------------------------------------------------------------------------------------');
+mprintf('\nBench unit\tID=%fm\t%f\t\t\t%f\t\t%f\t\t%f',dtb/100,deltab,ephsilonfb,Lmb,Lfb);
+mprintf('\nCommercial unit\tID=%fm\t%f\t\t\t%f\t\t%f\t\t%f',dtp,deltap,ephsilonfp,Lmp,Lfp);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH6/EX6.5/Chap6_Ex5.sce b/497/CH6/EX6.5/Chap6_Ex5.sce
new file mode 100755
index 000000000..aea88e31c
--- /dev/null
+++ b/497/CH6/EX6.5/Chap6_Ex5.sce
@@ -0,0 +1,38 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-6, Example 5, Page 161
+//Title: Reactor Scale-up for Geldart B Catalyst
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dtb=20;//ID of bench-scale reactor
+dtp=1;//ID of pilot reactor
+dpbar=200;//Average particle size in micrometer
+ephsilonmf=0.50;//Void fraction at minimum fluidization condition
+ephsilonmb=0.50;//Void fraction 
+uo=30;//Superficial gas velocity in cm/s
+Lmb=2;//Length of fixed bed in m
+umf=3;//Velocity at minimum fluidization condition in cm/s
+umb=3;//Velocity at in cm/s
+g=9.80;//Acceleration due to gravity in m/s^2
+pi=3.142857;
+
+//CALCULATION
+//In the small bench unit
+c=1;
+ubb=c*((uo-umf)/100)+0.35*(g*(dtb/100))^0.5;//Velocity using Eqn.(5.22)
+zsb=60*(dtb)^0.175;//Height using Eqn.(5.24)
+
+//In the large pilot unit
+ubp=c*((uo-umf)/100)+0.35*(g*dtp)^0.5;//Velocity using Eqn.(5.22)
+zsp=60*(dtp*100)^0.175;//Height using Eqn.(5.24)
+
+//OUTPUT
+printf('\nCondition at which bubbles transform into slugs');
+mprintf('\nFor tha small bench unit\n\t\tVelocity=%fm/s\n\t\tHeight above distributor plate=%fm',ubb,zsb/100);
+mprintf('\nFor tha large pilot unit\n\t\tVelocity=%fm/s\n\t\tHeight above distributor plate=%fm',ubp,zsp/100);
+
+//====================================END OF PROGRAM ======================================================
+
diff --git a/497/CH7/EX7.1/Chap7_Ex1.sce b/497/CH7/EX7.1/Chap7_Ex1.sce
new file mode 100755
index 000000000..8b7cc2484
--- /dev/null
+++ b/497/CH7/EX7.1/Chap7_Ex1.sce
@@ -0,0 +1,25 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-7, Example 1, Page 179
+//Title: Entrainment from Fine Particle Beds with High Freeboard
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+rhog=5.51;//Density of gas in kg/m^3
+rhos=1200;//Density of solid in kg/m^3
+dpbar=130;//Average size of particles in micrometer
+uo=0.61;//Superficial gas velocity in m/s
+g=9.80;//Acceleration due to gravity in m/s^2
+
+//CALCULATION
+//Assuming that freeboard in higher than TDH, computation of entrainment rate by Zenz & Weil's method
+x=(uo^2)/(g*(dpbar*10^-6)*rhos^2);//Calculation of value of x-axis for Fig.(6), page 175
+y=1.2;// Value of y-axis from Fig.(6)
+Gsstar=y*rhog*uo;//Computation of rate of entrainment
+
+//OUTPUT
+mprintf('\nRate of entrainment=%fkg/m^2s',Gsstar);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH7/EX7.2/Chap7_Ex2.sce b/497/CH7/EX7.2/Chap7_Ex2.sce
new file mode 100755
index 000000000..a447c8488
--- /dev/null
+++ b/497/CH7/EX7.2/Chap7_Ex2.sce
@@ -0,0 +1,19 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-7, Example 2, Page 180
+//Title: Entrainment from Large Particle Beds with High Freeboard
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+x=0.2;//Fraction of fines in the bed
+Gsstar=4.033320//Rate of entrainment in kg/m^2s(from Exa.1)
+
+//CALCULATION
+Gsstar1=x*Gsstar;//Rate of entrainment by Eqn.(3)
+
+//OUTPUT
+mprintf('\nRate of entrainment=%fkg/m^2s',Gsstar1);
+
+//====================================END OF PROGRAM ====================================================
+\ No newline at end of file
diff --git a/497/CH7/EX7.3/Chap7_Ex3.sce b/497/CH7/EX7.3/Chap7_Ex3.sce
new file mode 100755
index 000000000..8f89cabbe
--- /dev/null
+++ b/497/CH7/EX7.3/Chap7_Ex3.sce
@@ -0,0 +1,42 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-7, Example 3, Page 181
+//Title: Entrainment from Beds with a Wide Size Distribution of Solids
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+rhog=5.51;//Density of gas in kg/m^3
+rhos=1200;//Density of solid in kg/m^3
+uo=0.61;//Superficial gas velocity in m/s
+g=9.80;//Acceleration due to gravity in m/s^2
+dp=[10;30;50;70;90;110;130];//Diameter of particle in micrometer
+p=[0;0.0110;0.0179;0.0130;0.0058;0.0020;0];
+pi=3.142857;
+dt=6;
+
+//CALCULATION
+n=length(dp);
+i=1;
+while i<=n
+    x(i)=(uo^2)/(g*(dp(i)*10^-6)*rhos^2);//Computation of value of x-axis for Fig.(6), page 175)
+    i=i+1;
+end
+y=[40;12;6;3.2;2.;1.3;1];//Value of y-axis corresponding to each value of x-axis
+y1 = y .* p;
+i=1;
+k=0;
+while i<n
+    y1(i)=(y(i)*p(i));
+    k=k+((0.5)*(dp(i+1)-dp(i))*(y1(i+1)+y1(i)));//Integration using Trapezoidal rule
+    i=i+1;
+end
+rhosbar=k*rhog;//Computation of solid loading
+te=(pi/4)*(dt^2)*rhosbar*uo;//Computation of total entrainment
+
+//OUTPUT
+mprintf('\nSolid loading =%fkg/m^3',rhosbar);
+mprintf('\nTotal Entrainment =%fkg/s',te);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH7/EX7.4/Chap7_Ex4.sce b/497/CH7/EX7.4/Chap7_Ex4.sce
new file mode 100755
index 000000000..bba632c15
--- /dev/null
+++ b/497/CH7/EX7.4/Chap7_Ex4.sce
@@ -0,0 +1,38 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-7, Example 4, Page 181
+//Title: k* from Steady State Experiments
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dp=[40;60;80;100;120];//Diameter of particle in micrometer
+uo=0.381;//Superficial gas velocity in m/s
+
+//CALCULATION
+Gs=0.9;//Rate of entrainment in kg/m^2 s from Fig.3(a)
+pb=(1/100)*[0.45;1.00;1.25;1.00;0.60];//Size distribution for bed particles from Fig.3(b)
+pe=(1/100)*[1.20;2.00;1.25;0.45;0.10];//Size distribution for entrained particles from Fig.3(b)
+n=length(dp);
+i=1;
+while i<=n
+    ki(i)=(Gs*pe(i))/pb(i);//Calculation of ki* using Eqn.(13)
+    i=i+1;
+end
+
+//OUTPUT
+printf('\ndpi(micrometer)');
+printf('\t100pb(dpi)(micrometer^-1)');
+printf('\t100pe(dpi)(micrometer^-1)');
+printf('\tki*(kg/m^2 s)');
+j=1;
+while j<=n
+    mprintf('\n%f',dp(j));
+    mprintf('\t%f',100*pb(j));
+    mprintf('\t\t\t%f',100*pe(j));
+    mprintf('\t\t\t%f',ki(j));    
+    j=j+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH7/EX7.5/Chap7_Ex5.sce b/497/CH7/EX7.5/Chap7_Ex5.sce
new file mode 100755
index 000000000..a6fe52db0
--- /dev/null
+++ b/497/CH7/EX7.5/Chap7_Ex5.sce
@@ -0,0 +1,65 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-7, Example 5, Page 181
+//Title: Comparing Predictions for k*
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+rhog=1.217;//Density of gas in kg/m^3
+myu=1.8E-5;//Viscosity of gas in kg/m s
+umf=0.11;//Velocity at minimum fluidization condition in m/s
+rhos=2000;//Density of solid in kg/m^3
+uo=1.0;//Superficial gas velocity in m/s
+g=9.80;//Acceleration due to gravity in m/s^2
+dp=[30;40;50;60;80;100;120];//Diameter of particle in micrometer
+uti=[0.066;0.115;0.175;0.240;0.385;0.555;1.0];//Terminal velocity of particles in m/s
+
+//CALCULATION
+n=length(dp);
+i=1;
+while i<=n
+    //Using Yagi & Aochi's correlation
+    Ret(i)=(rhog*(uti(i))*dp(i)*10^-6)/myu;
+    kistar1(i)=((myu*((uo-uti(i))^2))/(g*(dp(i)*10^-6)^2))*(0.0015*(Ret(i)^0.5)+(0.01*(Ret(i)^1.2)));
+    //Using Wen & Hasinger's correlation
+    kistar2(i)=(((1.52E-5)*((uo-uti(i))^2)*rhog)/(g*dp(i)*10^-6)^0.5)*(Ret(i)^0.725)*((rhos-rhog)/rhog)^1.15;
+    //Using Merrick & Highley's correlation
+    kistar3(i)=uo*rhog*(0.0001+130*exp(-10.4*((uti(i)/uo)^0.5)*((umf/(uo-umf))^0.25)));
+    //Using Geldart's correlation
+    kistar4(i)=23.7*uo*rhog*exp(-5.4*(uti(i)/uo));
+    //Using Zenz & Weil's procedure
+    x1(i)=(uo^2)/(g*(dp(i)*10^-6)*rhos^2);//Computation of value of x-axis for Fig.(6), page 175)
+    y1=[12.2;8.6;6.4;4.9;2.75;1.8;1.2];//Value of y-axis corresponding to each value of x-axis
+    kistar5(i)=y1(i)*rhog*uo;
+    //Using Gugnoni & Zenz's procedure
+    x2(i)=(uo-uti(i))/((g*dp(i)*10^-6)^0.5);//Computation of value of x-axis for Fig.(6), page 175)
+    y=[5.8;5.4;3.2;2.8;1.3;0.6;0];//Value of y-axis corresponding to each value of x-axis
+    kistar6(i)=y(i)*rhog*uo;
+    i=i+1;
+end
+
+i=1;
+printf('dp(micrometer)');
+printf('\tYagi & Aochi');
+printf('\tWen & Hashinger');
+printf('\t\tMerrick & Highley');
+printf('\tGeldart et al.');
+printf('\t\tZenz & Well');
+printf('\t\tGugnoni & Zenz');
+while i<=n
+    mprintf('\n%f',dp(i));
+    mprintf('\t%f',kistar1(i));  
+    mprintf('\t%f',kistar2(i));
+    mprintf('\t\t%f',kistar3(i));
+    mprintf('\t\t%f',kistar4(i));
+    mprintf('\t\t%f',kistar5(i));
+    mprintf('\t\t%f',kistar6(i));
+    i=i+1;
+end    
+
+//Note: There is huge deviation of the calculated answer and the answer given in the textbook for the correlation of Merrick & Highley.  There is a contradiction in the correlation used in the problem and the one given in page 179. 
+//We tried to retrieve the original paper i.e. D.Merrick and J.Highley, AICHE J., 6, 220(1960). But the effort was not fruitful.
+
+//====================================END OF PROGRAM ====================================================
+\ No newline at end of file
diff --git a/497/CH7/EX7.6/Chap7_Ex6.sce b/497/CH7/EX7.6/Chap7_Ex6.sce
new file mode 100755
index 000000000..5d6277894
--- /dev/null
+++ b/497/CH7/EX7.6/Chap7_Ex6.sce
@@ -0,0 +1,31 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-7, Example 6, Page 190
+//Title: Entrainment from a Short Vessel Ht<TDH
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+dpbar=60;//Average size of particles in micrometer
+rhog=1.3;//Density of gas in kg/m^3
+rhos=1500;//Density of solid in kg/m^3
+umf=0.003;//Velocity at minimum fluidization condition in m/s
+uo=0.503;//Superficial gas velocity in m/s
+g=9.80;//Acceleration due to gravity in m/s^2
+Hf=2;//Height at which the cyclone inlet is to be located in m
+
+//CALCULATION
+y=(uo^2)/(g*(dpbar*10^-3)*rhos^2);//Calculation of value of y-axis for Fig.(6), page 175
+x=1;//Value of x-axis from Fig.(6), page 175
+Gsstar=x*rhog*uo;//Computation of rate of entrainment
+Gsuo=5.0;//Ejection rate pf particles in kg/m^2 s from Fig.(11), page 188
+a=0.72/uo;//From Fig.(12), page 189
+Gs=Gsstar+(Gsuo-Gsstar)*exp(-a*Hf);
+p=((Gs-Gsstar)/Gsstar)*100;
+
+//OUTPUT
+mprintf('\nRate of entrainment from short bed=%fkg/m^2s',Gs);
+mprintf('\nThis entrainment is %f percent higher than it would be if the gas exit were at the TDH',p);
+
+//====================================END OF PROGRAM ====================================================
+\ No newline at end of file
diff --git a/497/CH8/EX8.1/Chap8_Ex1.sce b/497/CH8/EX8.1/Chap8_Ex1.sce
new file mode 100755
index 000000000..a783d1e4b
--- /dev/null
+++ b/497/CH8/EX8.1/Chap8_Ex1.sce
@@ -0,0 +1,120 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-8, Example 1, Page 206
+//Title: Performance of a Fast Fluidized Vessel
+//==========================================================================================================
+clear
+clc
+
+//INPUT
+Lmf=2.4;//Length of bed at minimum fluidized condition in m
+uo=[2;4;6];//Superficial gas velocity in m/s
+GsII=100;//Solid circulation rate in kg/m^2 s for Mode II
+uoIII=4;//Superficial gas velocity in m/s for Mode III
+GsIII=[42;50;100;200;400];//Solid circulation rate in kg/m^2 s for Mode III
+GsIV=[70;100;120];//Solid circulation rate in kg/m^2 s for Mode IV
+dt=0.4;//Column diamter in m
+Ht=10;//Height of column in m
+rhos=1000;//Density of solid in kg/m^3
+dpbar=55;//Particle diameter in micrometer
+ephsilonmf=0.5;//Void fraction at minimum fluidization condition
+
+//CALCULATION
+//Mode I
+ephsilonstar=0.01;//Saturation carrying capacity of gas
+ephsilonsd=[0.2;0.16;0.14];//Solid holdup in lower dense region from Fig.8(b) for various uo
+n=length(uo);
+i=1;
+Hfguess=2;//Guess value of height
+while i<=n
+    a(i)=3/uo(i);//Decay constant
+    function[fn]=solver_func(Hf)//Function defined for solving the system
+        fn=Lmf*(1-ephsilonmf)-((ephsilonsd(i)-(ephsilonstar+(ephsilonsd(i)-ephsilonstar)*exp(-a(i)*Hf)))/a(i))-Ht*ephsilonsd(i)+Hf*(ephsilonsd(i)-ephsilonstar);
+    endfunction
+    [Hf(i)]=fsolve(Hfguess,solver_func,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf
+    Hd(i)=Ht-Hf(i);//Height of lower densce region
+    ephsilonse(i)=ephsilonstar+(ephsilonsd(i)-ephsilonstar)*exp(-a(i)*Hf(i));//Solid holdup at exit
+    GsI(i)=rhos*uo(i)*ephsilonse(i);//Solid circulation rate from Eqn.(4)
+    i=i+1;
+end
+
+//Mode II
+i=1;
+Hfguess2=2;//Guess value of height
+while i<=n
+    ephsilonseII(i)=GsII/(rhos*uo(i));//Solid holdup at exit
+    function[fn]=solver_func1(Hf)//Function defined for solving the system
+        fn=ephsilonseII(i)-ephsilonstar-(ephsilonsd(i)-ephsilonstar)*exp(-a(i)*Hf);//From Eqn.(7)
+    endfunction
+    [HfII(i)]=fsolve(Hfguess2,solver_func1,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf
+    HdII(i)=Ht-HfII(i);//Height of lower dense region
+    //Length of bed minimum fluidization condtion
+    LmfII(i)=(1-ephsilonmf)^-1*[((ephsilonsd(i)-ephsilonseII(i))/a(i))+Ht*ephsilonsd(i)-HfII(i)*(ephsilonsd(i)-ephsilonstar)];
+    i=i+1;
+end
+
+//Mode III
+aIII=3/uoIII;//Decay constant
+ephsilonsdIII=0.16;//Solid holdup at lower dense region
+i=1;
+m=length(GsIII);
+Hfguess3=2;//Guess value of height 
+while i<=m
+    ephsilonseIII(i)=GsIII(i)/(rhos*uoIII);//Solid holdup at exit
+    function[fn]=solver_func2(Hf)//Function defined for solving the system
+        fn=ephsilonseIII(i)-ephsilonstar-(ephsilonsdIII-ephsilonstar)*exp(-aIII*Hf);//From Eqn.(7)
+    endfunction
+    [HfIII(i)]=fsolve(Hfguess3,solver_func2,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf
+    HdIII(i)=Ht-HfIII(i);//Height of lower dense region
+    //Length of bed at minimum fluidization condition
+    LmfIII(i)=(1-ephsilonmf)^-1*[((ephsilonsdIII-ephsilonseIII(i))/aIII)+Ht*ephsilonsdIII-HfIII(i)*(ephsilonsdIII-ephsilonstar)];
+    i=i+1;
+end
+
+//Mode IV
+i=1;
+Hfguess4=2;//Guess value of height
+while i<=n
+    aIV(i)=3/uo(i);//Decay constant
+    ephsilonseIV(i)=GsIV(i)/(rhos*uo(i));//Solid holdup at exit
+    function[fn]=solver_func3(Hf)//Function defined for solving the system
+        fn=ephsilonseIV(i)-ephsilonstar-(ephsilonsd(i)-ephsilonstar)*exp(-aIV(i)*Hf);//From Eqn.(7)
+    endfunction
+    [HfIV(i)]=fsolve(Hfguess4,solver_func3,1E-6);//Using inbuilt function fsolve for solving Eqn.(10) for Hf
+    HdIV(i)=Ht-HfIV(i);//Height of lower dense region
+    //Length of bed at minimum fluidization condition
+    LmfIV(i)=(1-ephsilonmf)^-1*[((ephsilonsd(i)-ephsilonseIV(i))/aIV(i))+Ht*ephsilonsd(i)-HfIV(i)*(ephsilonsd(i)-ephsilonstar)];
+    i=i+1;
+end
+
+//OUTPUT
+printf('\nMode I');
+printf('\n\tuo(m/s)\t\tephsilonse(-)\tHf(m)\t\tHd(m)\t\tGs(kg/m^2 s)');
+i=1;
+while i<=n
+    mprintf('\n\t%f\t%f\t%f\t%f\t%f',uo(i),ephsilonse(i),Hf(i),Hd(i),GsI(i));
+    i=i+1;
+end
+printf('\nMode II');
+printf('\n\tuo(m/s)\t\tephsilonse(-)\tHf(m)\t\tHd(m)\t\tLmf(m))');
+i=1;
+while i<=n
+    mprintf('\n\t%f\t%f\t%f\t%f\t%f',uo(i),ephsilonseII(i),HfII(i),HdII(i),LmfII(i));
+    i=i+1;
+end
+printf('\nMode III');
+printf('\n\tGs(kg/m^ s)\tephsilonse(-)\tHf(m)\t\tHd(m)\t\tLmf(m)');
+i=1;
+while i<=m
+    mprintf('\n\t%f\t%f\t%f\t%f\t%f',GsIII(i),ephsilonseIII(i),HfIII(i),HdIII(i),LmfIII(i));
+    i=i+1;
+end
+printf('\nMode IV');
+printf('\n\tuo(m/s)\t\tGs(kg/m^2 s)\tephsilonse(-)\tHf(m)\t\tLmf(m)');
+i=1;
+while i<=n
+    mprintf('\n\t%f\t%f\t%f\t%f\t%f',uo(i),GsIV(i),ephsilonseIV(i),HfIV(i),LmfIV(i));
+    i=i+1;
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH9/EX9.1/Chap9_Ex1.sce b/497/CH9/EX9.1/Chap9_Ex1.sce
new file mode 100755
index 000000000..1f9328035
--- /dev/null
+++ b/497/CH9/EX9.1/Chap9_Ex1.sce
@@ -0,0 +1,47 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-9, Example 1, Page 218
+//Title: Vertical Movement of Solids
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+umf=0.015;//Velocity at minimum fluidization condition in m/s
+ephsilonmf=0.5;//Void fraction at minimum fluidization condition
+uo=0.1;//Superficial gas velocity in m/s
+delta=0.2;//Bed fraction in bubbles
+db=0.06;//Equilibrium bubble size in m
+dt=[0.1;0.3;0.6;1.5];//Various vessel sizes in m
+ub=[0.4;0.75;0.85;1.1];//Bubble velocity in m/s
+Dsv=[0.03;0.11;0.14;0.23];//Reported values of vertical dispersion coefficient
+
+//CALCULATION
+n=length(ub);
+i=1;
+fw1=2;//Wake fraction from Hamilton et al.
+fw2=0.32;//Wake fraction from Fig.(5.8)
+fw=(fw1+fw2)*0.5;//Average value of wake fraction
+while i<=n
+    Dsv1(i)=12*((uo*100)^0.5)*((dt(i)*100)^0.9);//Vertical distribution coefficient from Eqn.(3)
+    Dsv2(i)=(fw^2*ephsilonmf*delta*db*ub(i)^2)/(3*umf);//Vertical distribution coefficient from Eqn.(12)
+    i=i+1;
+end
+
+//OUTPUT
+printf('\n\t\tVertical dispersion coefficient(m^2/s)');
+printf('\nVessel Size(m)');
+printf('\tFrom Experiment');
+printf('\tFrom Eqn.(3)');
+printf('\tFrom Eqn.(12)');
+i=1;
+while i<=n
+    mprintf('\n%f',dt(i));
+    mprintf('\t%f',Dsv(i));
+    mprintf('\t%f',Dsv1(i)/10^4);
+    mprintf('\t%f',Dsv2(i));
+    i=i+1;   
+end
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH9/EX9.2/Chap9_Ex2.sce b/497/CH9/EX9.2/Chap9_Ex2.sce
new file mode 100755
index 000000000..f8eb9da3b
--- /dev/null
+++ b/497/CH9/EX9.2/Chap9_Ex2.sce
@@ -0,0 +1,68 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-9, Example 2, Page 222
+//Title: Horizontal Drift Of Solids
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Lmf=0.83;//Length of bed at minimum fluidization condition in m
+dp=450;//Average particle size in micrometer
+ephsilonmf=0.42;//Void fraction at minimum fluidization condition
+umf=0.17;//Velocity at minimum fluidization condition in m/s
+uo=[0.37;0.47;0.57;0.67];//Superficial gas velocity in m/s
+Dsh=[0.0012;0.0018;0.0021;0.0025];//Horizontal Drift Coefficient from Experiment in m^2/s
+db=[0.10;0.14];//Equilibrium bubble size in m
+g=9.81;//Acceleration due to gravity in m/s^2
+
+
+//CALCULATION
+n=length(uo);
+m=length(db);
+j=1;
+i=1;
+k=1;
+alpha=0.77;//Since we are not dealing with Geldart A or AB solids
+uf=umf/ephsilonmf;
+for j = 1:m
+        for i = 1:n
+            ubr(k)=0.711*(db(j)*g)^0.5;//Rise velocity of a single bubble in m/s
+            ub(k)=uo(i)-umf+ubr(k);//Rise velocity of bubbles in a bubbling bed
+            delta(k)=(uo(i)-umf)/(ub(k)+umf);//Bed fraction in bubbles
+            if ubr(i)>uf then Dshc(k)=(3/16)*(delta(k)/(1-delta(k)))*((alpha^2*db(j)*ubr(k)*[(((ubr(k)+2*uf)/(ubr(k)-uf))^(1/3))-1]));//Horizontal Distribution coeff. from Eqn.(14)
+            else Dsh(k)=(3/16)*(delta/(1-delta))*(alpha^2*umf*db/ephsilonmf);//Horizontal Distribution coeff. from Eqn.(15)
+            end
+            Dshc(k)=(3/16)*(delta(k)/(1-delta(k)))*((alpha^2*db(j)*ubr(k)*[(((ubr(k)+2*uf)/(ubr(k)-uf))^(1/3))-1]));//Horizontal Distribution coeff. from Eqn.(14)
+            i=i+1;
+            k=k+1;
+        end
+    i=1;
+    j=j+1;
+end
+
+//OUTPUT
+i=1;
+j=1;
+k=1;
+while k<=m*n
+    mprintf('\nSnce we do not have ub=%fm/s>>uf=%fm/s we use Eqn.(14).',ub(k),uf)
+    printf('\nGas Velocity(m/s)');
+    printf('\tHorizontal Drift Coefficient Calculated(m^2/s)');
+    printf('\tHorizontal Drift Coefficient from Experiment(m^2/s)');
+    while j<=m
+        mprintf('\ndb=%fm',db(j));
+        while i<=n
+            mprintf('\n%f',uo(i));
+            mprintf('\t\t%f',Dshc(k));
+            mprintf('\t\t\t\t\t%f',Dsh(i));
+            i=i+1;   
+            k=k+1;
+        end
+    i=1;
+    j=j+1;
+    end
+end    
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
diff --git a/497/CH9/EX9.3/Chap9_Ex3.sce b/497/CH9/EX9.3/Chap9_Ex3.sce
new file mode 100755
index 000000000..0cceb0c04
--- /dev/null
+++ b/497/CH9/EX9.3/Chap9_Ex3.sce
@@ -0,0 +1,45 @@
+//Kunii D., Levenspiel O., 1991. Fluidization Engineering(II Edition). Butterworth-Heinemann, MA, pp 491
+
+//Chapter-9, Example 3, Page 232
+//Title: Design of Baffle Plates
+//==========================================================================================================
+
+clear
+clc
+
+//INPUT
+Gsup=1.5;//Solid interchange rate in kg/m^2plate s
+dor=19.1;//Orifice diameter in mm
+dp=210;//Particle size in micrometer
+uo=0.4;//Superficial gas velocity in m/s
+fopen=[0.12;0.17;0.26];//Open area fraction 
+pi=3.14;
+
+//CALCULATION
+n=length(fopen);
+i=1;
+while i<=n
+    uor(i)=uo/fopen(i);//Gas velocity through the orifice
+    ls1(i)=Gsup/fopen(i);//Flux of solids through the holes
+    i=i+1;
+end
+ls2=[12;20;25];//Flux of solids through holes from Fig.13(c) for different uor values
+fopen1=0.12;//Open area fraction which gives reasonable fit
+lor=sqrt(((pi/4)*dor^2)/fopen1);//Orifice spacing
+
+//OUTPUT
+printf('\nfopen');
+printf('\t\tuor(m/s)');
+printf('\tls from Eqn.(18)');
+printf('\tls from Fig.13(c)');
+i=1;
+while i<=n
+    mprintf('\n%f',fopen(i));
+    mprintf('\t%f',uor(i));
+    mprintf('\t%f',ls1(i));
+    mprintf('\t\t%f',ls2(i));
+    i=i+1;   
+end
+mprintf('\n\nFor square pitch, the orifice spacing should be %fmm',lor);
+
+//====================================END OF PROGRAM ======================================================
+\ No newline at end of file
author	priyanka	2015-06-24 15:03:17 +0530
committer	priyanka	2015-06-24 15:03:17 +0530
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