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diff --git a/1040/CH6/EX6.1/Chapter6_Ex1_Output.txt b/1040/CH6/EX6.1/Chapter6_Ex1_Output.txt
new file mode 100644
index 000000000..2e421928d
--- /dev/null
+++ b/1040/CH6/EX6.1/Chapter6_Ex1_Output.txt
@@ -0,0 +1,17 @@
+

+ OUTPUT Ex6.1.a

+==========================================================

+ The Power consumption per unit volume at 300rpm = 1.64 HP/1000 gal

+ The Power consumption scaling up sixfold in diameter = 59 HP/1000 gal

+

+

+ OUTPUT Ex6.1.b

+==========================================================

+ The speed of the stirrer  = 2.76 sec-1 or 166 rpm

+ Blending time increases by factor of 1.81 

+

+

+ OUTPUT Ex6.1.c

+==========================================================

+ The new stirrer speed = 1.41 sec-1 or 84 rpm

+ The new blending time  for Da/Dt ratio of 0.5 = 11.4 sec
\ No newline at end of file
diff --git a/1040/CH6/EX6.1/Ex6_1.sce b/1040/CH6/EX6.1/Ex6_1.sce
new file mode 100644
index 000000000..9af0bfd8e
--- /dev/null
+++ b/1040/CH6/EX6.1/Ex6_1.sce
@@ -0,0 +1,72 @@
+//Harriot P., 2003, Chemical Reactor Design (I-Edition), Marcel Dekker, Inc., USA, pp 436.

+//Chapter-6 Ex6.1 Pg No.236

+//Title:Power Consumption at 300 rpm,speed of stirrer and blending time

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

+clear

+clc

+// COMMON INPUT

+D_a=0.1;

+D_t=0.3;

+H=0.3;

+N_P=5.5;

+rho=1000;

+n=5;

+S_f=6;//Scale up factor in diameter

+P_by_V_limit=10;//Pressure per unit volume (HP/1000gal)

+n1=5;

+Da_by_Dt1=D_a/D_t;

+Da_by_Dt2=0.5;

+

+//CALCULATION (Ex6.1.a)

+P_unit_vol=(N_P*n^3*D_a^5)/(%pi*(1/4)*D_t^2*H);

+P_thousand_gal=P_unit_vol*5.067;

+t=(4/n)*(D_t/D_a)^2*(H/D_t);

+P_unit_vol_new=S_f^2*P_thousand_gal;

+

+//CALCULATION (Ex6.1.b)

+n_limit=(P_by_V_limit/P_unit_vol_new)^(1/3) *n1;//Pressure per unit vol propotional to n3

+t_inc_factor=n1/n_limit;//t inversely propotional to n

+rotational_speed=n_limit*60;//Speed in rpm

+

+//CALCULATION (Ex6.1.c)

+n2=(Da_by_Dt1/Da_by_Dt2)^(5/3)*n_limit;

+rotaional_speed=n2*60;

+t1=4*(1/Da_by_Dt1)^2*(H/D_t)*(1/n_limit);

+t2=4*(1/Da_by_Dt2)^2*(H/D_t)*(1/n2);

+

+//OUTPUT (Ex6.1.a)

+mprintf('\n OUTPUT Ex6.1.a');

+mprintf('\n==========================================================');

+mprintf('\n The Power consumption per unit volume at 300rpm = %.2f HP/1000 gal',P_thousand_gal);

+mprintf('\n\ The Power consumption scaling up sixfold in diameter = %.0f HP/1000 gal',P_unit_vol_new); 

+

+

+//OUTPUT (Ex6.1.b)

+mprintf('\n\n\n OUTPUT Ex6.1.b');

+mprintf('\n==========================================================');

+mprintf('\n The speed of the stirrer  = %.2f sec-1 or %.0f rpm',n_limit,rotational_speed);

+mprintf('\n Blending time increases by factor of %.2f ',t_inc_factor); 

+

+//OUTPUT(Ex6.1.c)

+mprintf('\n\n\n OUTPUT Ex6.1.c');

+mprintf('\n==========================================================');

+mprintf('\n The new stirrer speed = %.2f sec-1 or %.0f rpm',n2,rotaional_speed); 

+mprintf('\n The new blending time  for Da/Dt ratio of 0.5 = %.1f sec',t2); 

+

+//FILE OUTPUT

+fid= mopen('.\Chapter6-Ex1-Output.txt','w');

+mfprintf(fid,'\n OUTPUT Ex6.1.a');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\n The Power consumption per unit volume at 300rpm = %.2f HP/1000 gal',P_thousand_gal);

+mfprintf(fid,'\n\ The Power consumption scaling up sixfold in diameter = %.0f HP/1000 gal',P_unit_vol_new);

+mfprintf(fid,'\n\n\n OUTPUT Ex6.1.b');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\n The speed of the stirrer  = %.2f sec-1 or %.0f rpm',n_limit,rotational_speed);

+mfprintf(fid,'\n Blending time increases by factor of %.2f ',t_inc_factor); 

+mfprintf(fid,'\n\n\n OUTPUT Ex6.1.c');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\n The new stirrer speed = %.2f sec-1 or %.0f rpm',n2,rotaional_speed); 

+mfprintf(fid,'\n The new blending time  for Da/Dt ratio of 0.5 = %.1f sec',t2);

+mclose(fid);

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

+//Disclaimer: In Ex6.1.c there is an arithematic error in the value of D_a/D_t. The value of  D_a/D_t should be 11.4 instead of the value reported in the textbook for D_a/D_t=11.1.

diff --git a/1040/CH6/EX6.2/Chapter6_Ex2_Output.txt b/1040/CH6/EX6.2/Chapter6_Ex2_Output.txt
new file mode 100644
index 000000000..170c3b918
--- /dev/null
+++ b/1040/CH6/EX6.2/Chapter6_Ex2_Output.txt
@@ -0,0 +1,2 @@
+

+ The effect of radial diffusion makes conversion almost as same as plug flow as alpha = 4
\ No newline at end of file
diff --git a/1040/CH6/EX6.2/Ex6_2.sce b/1040/CH6/EX6.2/Ex6_2.sce
new file mode 100644
index 000000000..d5e8eaf9d
--- /dev/null
+++ b/1040/CH6/EX6.2/Ex6_2.sce
@@ -0,0 +1,35 @@
+//Harriot P., 2003, Chemical Reactor Design (I-Edition), Marcel Dekker, Inc., USA, pp 436.

+//Chapter-6 Ex6.2 Pg No. 239

+//Title:Effect of diffusion on conversion for laminar flow 

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

+clear

+clc

+//INPUT

+D=1*10^(-2);//Diameter of pipeline (m)

+R=D/2;//Radius (m)

+D_m=10^(-4);//Diffusivity (m2/sec)

+k=1;//Reaction rate constant (sec-1)

+

+

+//CALCULATION

+alpha=D_m/(k*(R^2));//Refer topic ('Diffusion in laminar flow reactors') Pg No.239

+

+

+//OUTPUT

+if (alpha<=0.01) 

+    then

+    mprintf('\n The  effect of radial diffusion  on conversion can be neglected as alpha = %.0f',alpha )

+else

+    mprintf('\n The effect of radial diffusion makes conversion almost as same as plug flow as alpha = %.0f',alpha)

+end

+

+//FILE OUTPUT

+fid= mopen('.\Chapter6-Ex2-Output.txt','w');

+if (alpha<=0.01) 

+    then

+    mfprintf(fid,'\n The  effect of radial diffusion  on conversion can be neglected as alpha = %.0f',alpha )

+else

+    mfprintf(fid,'\n The effect of radial diffusion makes conversion almost as same as plug flow as alpha = %.0f',alpha)

+end

+mclose(fid);

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

diff --git a/1040/CH6/EX6.3/Chapter6_Ex3_Output.txt b/1040/CH6/EX6.3/Chapter6_Ex3_Output.txt
new file mode 100644
index 000000000..8aab34bed
--- /dev/null
+++ b/1040/CH6/EX6.3/Chapter6_Ex3_Output.txt
@@ -0,0 +1,10 @@
+

+ OUTPUT Ex6.3.a

+==========================================================

+ The effect of axial dispersion is significant and the percentage excess of catalyst = 8%

+

+

+ OUTPUT Ex6.3.b

+==========================================================

+ The effect of axial dispersion is less on reducing the bed length 

+ The percentage excess of catalyst = 6%
\ No newline at end of file
diff --git a/1040/CH6/EX6.3/Ex6_3.sce b/1040/CH6/EX6.3/Ex6_3.sce
new file mode 100644
index 000000000..e84f6ca10
--- /dev/null
+++ b/1040/CH6/EX6.3/Ex6_3.sce
@@ -0,0 +1,59 @@
+//Harriot P., 2003, Chemical Reactor Design (I-Edition), Marcel Dekker, Inc., USA, pp 436.

+//Chapter-6 Ex6.3 Pg No. 248

+//Title:Effect of Axial dispersion and length on conversion

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

+clear

+clc

+// COMMON INPUT

+u=1;//Superficial velocity (cm/s)

+D=2*10^(-5)//Molecular Diffusivity(cm2/s)

+Re=30;//Reynolds No.

+Pe_a=0.25;//Peclet No. corresponding Re No. from Fig 6.10

+dp=3*(10^-1);//Particle Size (cm)

+L=48;//Length of the bed (cm)

+X_A=0.93;//Conversion

+L_old=48;// Old bed length (cm)

+L_new=L_old/2;//New bed length (cm)

+

+

+

+//CALCULATION (Ex6.3.a)

+Pe_dash=Pe_a*L/dp;//Refer Pg.No.247

+one_minus_X_A=(1-X_A);

+k_rho_L_by_u1=2.65;//From Fig6.12 for given  Pe_dash

+X_A1=1-exp(-k_rho_L_by_u1);

+//To increase the conversion more catalyst is needed

+k_rho_L_by_u2=2.85;//From Fig6.12

+X_A2=1-exp(-k_rho_L_by_u2);

+Percentage_excess_cat_a=((k_rho_L_by_u2-k_rho_L_by_u1)/k_rho_L_by_u1)*100;

+

+//CALCULATION(Ex6.3.b)

+k_rho_L_by_u_new=k_rho_L_by_u1/2;

+X_A_cal=(1-exp(-k_rho_L_by_u_new));//Calculated conversion

+Pe_dash_new=Pe_dash/2;

+k_rho_L_by_u_graph=1.3992;//Value obtained from Figure6.12 for the calculated conversion

+Percentage_excess_cat_b=((k_rho_L_by_u_graph-k_rho_L_by_u_new)/k_rho_L_by_u_new)*100;

+

+//OUTPUT(Ex6.3.a)

+mprintf('\n OUTPUT Ex6.3.a');

+mprintf('\n==========================================================');

+mprintf('\n The effect of axial dispersion is significant and the percentage excess of catalyst = %.0f%%',Percentage_excess_cat_a );

+

+//OUTPUT (Ex6.3.b)

+mprintf('\n\n\n OUTPUT Ex6.3.b');

+mprintf('\n==========================================================');

+mprintf('\n The effect of axial dispersion is less on reducing the bed length \n The percentage excess of catalyst = %.0f%%',Percentage_excess_cat_b );

+

+//FILE OUTPUT

+fid= mopen('.\Chapter6-Ex3-Output.txt','w');

+mfprintf(fid,'\n OUTPUT Ex6.3.a');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\n The effect of axial dispersion is significant and the percentage excess of catalyst = %.0f%%',Percentage_excess_cat_a );

+mfprintf(fid,'\n\n\n OUTPUT Ex6.3.b');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\n The effect of axial dispersion is less on reducing the bed length \n The percentage excess of catalyst = %.0f%%',Percentage_excess_cat_b );

+mclose(fid);

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

+

+

+

diff --git a/1040/CH6/EX6.4/Chapter6_Ex4_Output.txt b/1040/CH6/EX6.4/Chapter6_Ex4_Output.txt
new file mode 100644
index 000000000..ad8b28f26
--- /dev/null
+++ b/1040/CH6/EX6.4/Chapter6_Ex4_Output.txt
@@ -0,0 +1,9 @@
+

+ OUTPUT Ex6.4.a

+==========================================================

+The average converion when each section has same superficial velocity:94.1%

+

+

+ OUTPUT Ex6.4.b

+==========================================================

+The overall conversion for different velocities:92.7% 
\ No newline at end of file
diff --git a/1040/CH6/EX6.4/Ex6_4.sce b/1040/CH6/EX6.4/Ex6_4.sce
new file mode 100644
index 000000000..86305a9f6
--- /dev/null
+++ b/1040/CH6/EX6.4/Ex6_4.sce
@@ -0,0 +1,61 @@
+// Harriot P., 2003, Chemical Reactor Design (I-Edition), Marcel Dekker, Inc., USA, pp 436.

+//Chapter-6 Ex6.4 Pg No.251

+//Title:Conversion in packed bed for same superficial velocity

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

+clear

+clc

+//COMMON INPUT 

+L=2.5;//Lendth of bed(ft)

+X_A=0.95;//Conversion

+L_a=3;//Length of section a (ft)

+L_b=2;//Length of section b (ft)

+u_oa_by_u0=0.88;//Refer equation 3.64

+u_ob_by_u0=1.12;

+L=2.5;//(ft)

+

+

+//CALCULATION (Ex6.4.a)

+k_rho_L_by_u=log(1/(1-X_A));//First Order reactions

+//For Section a

+k_rho_L_by_u_a=k_rho_L_by_u*(L_a/L);

+X_A_section_a=(1-exp(-k_rho_L_by_u_a));

+//For Section b

+k_rho_L_by_u_b=k_rho_L_by_u*(L_b/L);//Dimensionless Group based on ideal plug flow for first order reaction

+X_A_section_b=(1-exp(-k_rho_L_by_u_b));

+X_A_Ave=(X_A_section_b+X_A_section_a)/2;

+Percent_X_A_Ave=X_A_Ave*100

+

+//CALCULATION (Ex6.4.b)

+k_rho_L_by_u=log(1/(1-X_A));//First Order reaction

+//For Section a

+k_rho_L_by_u_a=k_rho_L_by_u*(L_a/L)*(1/u_oa_by_u0);

+X_A_section_a=(1-exp(-k_rho_L_by_u_a));

+delP_a_by_alpha_u0_pow=L_a*(u_oa_by_u0);//Refer equation 3.64

+

+//For Section b

+k_rho_L_by_u_b=k_rho_L_by_u*(L_b/L)*(1/u_ob_by_u0);//Dimensionless Group based on ideal plug flow for first order reaction

+delP_b_by_alpha_u0_pow=L_b*u_ob_by_u0;

+X_A_section_b=(1-exp(-k_rho_L_by_u_b));

+X_A_avg=(u_oa_by_u0*X_A_section_a+u_ob_by_u0*X_A_section_b)/2;

+Percent_X_A_avg=X_A_avg*100;

+

+//OUTPUT(Ex6.4.a)

+mprintf('\n OUTPUT Ex6.4.a');

+mprintf('\n==========================================================');

+mprintf('\nThe average converion when each section has same superficial velocity:%0.1f%%',Percent_X_A_Ave );

+

+//OUTPUT(Ex6.4.b)

+mprintf('\n\n\n OUTPUT Ex6.4.b');

+mprintf('\n==========================================================');

+mprintf('\nThe overall conversion for different velocities:%0.1f%% ',Percent_X_A_avg );

+

+//FILE OUTPUT

+fid= mopen('.\Chapter6-Ex4-Output.txt','w');

+mfprintf(fid,'\n OUTPUT Ex6.4.a');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\nThe average converion when each section has same superficial velocity:%0.1f%%',Percent_X_A_Ave );

+mfprintf(fid,'\n\n\n OUTPUT Ex6.4.b');

+mfprintf(fid,'\n==========================================================');

+mfprintf(fid,'\nThe overall conversion for different velocities:%0.1f%% ',Percent_X_A_avg );

+mclose(fid);

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