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diff --git a/1040/CH5/EX5.1/Chapter5_Ex1_Plot_1.pdf b/1040/CH5/EX5.1/Chapter5_Ex1_Plot_1.pdf
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+++ b/1040/CH5/EX5.1/Chapter5_Ex1_Plot_1.pdf
diff --git a/1040/CH5/EX5.1/Chapter5_Ex1_Plot_2.pdf b/1040/CH5/EX5.1/Chapter5_Ex1_Plot_2.pdf
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index 000000000..0eeb75fb8
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+++ b/1040/CH5/EX5.1/Chapter5_Ex1_Plot_2.pdf
diff --git a/1040/CH5/EX5.1/Ex5_1.sce b/1040/CH5/EX5.1/Ex5_1.sce
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+//Harriot P.,2003,Chemical Reactor Design (I-Edition) Marcel Dekker,Inc. USA,pp 436

+//Chapter-5 Ex5.1 Pg No. 185

+//Title: Temperature Profiles for tubular reactor

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

+clear

+clc

+clf

+//INPUT

+delta_H=-25000;//(kcal/mol) Enthalpy

+D=2;//(cm)Diameter of Tubular Reactor 

+C_A0=0.002;//(mol/cm3) Initial concentration of feed

+k=0.00142;//(s-1) Rate Constant

+E_by_R=15000;//(K-1)

+rho=0.8;//(g/cm3)

+c_p= 0.5;// (cal/g°C)

+U=0.025;//(cal/sec cm2°C )

+u=60;//(cm/s)

+

+

+//CALCULATION

+function diffeqn = Simul_diff_eqn(l,y,T_j)

+    diffeqn(1) =(k*exp(E_by_R*((1/T_initial)-(1/y(2)))))*(1-y(1))/u;// Derivative for the first variable  

+    diffeqn(2) =(C_A0*(k*exp(E_by_R*((1/T_initial)-(1/y(2)))))*(1-y(1))*(-1*delta_H)-U*(4/D)*(y(2)-T_j))/(u*rho*c_p) ; // Derivative for the second variable 

+endfunction

+

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

+

+T_j_data = [ 348 349 350 351];

+m = length(T_j_data);

+n = 1;

+while n <= m 

+T_j = T_j_data(n)

+T_initial=340;// for rate constant

+x0=0;

+T0=344;

+l0=0;

+l=0:0.1E2:70E2; 

+y = ode([x0;T0],l0,l,list(Simul_diff_eqn,T_j));

+x_data(n,:) = y(1,:);

+T_data(n,:) = y(2,:);

+n = n + 1;

+end

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

+scf(0)

+plot(l,T_data(1,:),'r-',l,T_data(2,:),'b-',l,T_data(3,:),'k-',l,T_data(4,:),'g-')

+xtitle('Temperature Profiles for a jacketed  tubular  reactor')

+xlabel("Length (cm)")

+ylabel("Temperature (K)")

+legend(['348';'349';'350';'351']);

+

+scf(1)

+plot(l,x_data(1,:),'r-',l,x_data(2,:),'b-',l,x_data(3,:),'k-',l,x_data(4,:),'g-')

+xtitle('Conversion for a jacketed  tubular  reactor');

+xlabel("Length (cm)")

+ylabel("Conversion")

+legend(['348';'349';'350';'351']);

+

+//OUTPUT

+mprintf('\n The Temperature profiles for four feed temperatures are plotted');

+mprintf('\n For T0:348 K  attains its maximum temperature at conversion of about 25%%-30%%');

+mprintf('\n At T0:351 K the temperature increases by 6.5°C high senstivity that the reactor is nearing unstable');

+

+//FILE OUTPUT

+fid= mopen('.\Chapter5-Ex1-Output.txt','w');

+mfprintf(fid,'\n The Temperature profiles for four feed temperatures are plotted.');

+mfprintf(fid,'\n For T0:348 K  attains its maximum temperature at conversion of about 25%%-30%%');

+mfprintf(fid,'\n At T0:351 K the temperature increases by 6.5°C high senstivity that the reactor is nearing unstable');

+mclose(fid);

+

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

+

+

+

+

diff --git a/1040/CH5/EX5.2/Chapter5_Ex2_Output.txt b/1040/CH5/EX5.2/Chapter5_Ex2_Output.txt
new file mode 100644
index 000000000..f8756898e
--- /dev/null
+++ b/1040/CH5/EX5.2/Chapter5_Ex2_Output.txt
@@ -0,0 +1,2 @@
+

+	The maximum internal temperature difference 1.264 °C
\ No newline at end of file
diff --git a/1040/CH5/EX5.2/Ex5_2.sce b/1040/CH5/EX5.2/Ex5_2.sce
new file mode 100644
index 000000000..48486f8b9
--- /dev/null
+++ b/1040/CH5/EX5.2/Ex5_2.sce
@@ -0,0 +1,32 @@
+//Harriot P.,2003,Chemical Reactor Design (I-Edition) Marcel Dekker,Inc.,USA,pp 436.

+//Chapter-5 Ex5.2 Pg No. 194

+//Title: Maximum internal temperature difference

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

+clear

+format(16)

+clc

+//INPUT

+T_C=200;//Temperature(°C)

+P=1.2;//Pressure (atm)

+f_ethylene=0.05;//fraction of ethylene

+k_s=8*10^(-4);//Solid conductivity (cal/sec cm°C)

+D_e=0.02;//Diffusivity for ethylene (cm2/s)

+del_H= -32.7*10^(3);//Heat of reaction (cal)

+V_ref=22400;// reference volume(cm3)

+T_ref=273;//Reference Temperature (K)

+P_ref=1;//Reference Pressure (atm)

+T_K=T_C+273;//Reaction Temperature (K)

+

+//CALCULATION

+C_s=f_ethylene*P*T_ref/(V_ref*T_K*P_ref);

+Tc_minus_Ts=D_e*C_s*(-del_H)/k_s;//Refer equation 5.51 Pg No. 194

+

+//OUTPUT

+mprintf('\n\tThe maximum internal temperature difference %0.3f °C',Tc_minus_Ts);

+

+//FILE OUTPUT

+fid= mopen('.\Chapter5-Ex2-Output.txt','w');

+mfprintf(fid,'\n\tThe maximum internal temperature difference %0.3f °C',Tc_minus_Ts);

+mclose(fid);

+

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

diff --git a/1040/CH5/EX5.3/Chapter5_Ex3_Output.txt b/1040/CH5/EX5.3/Chapter5_Ex3_Output.txt
new file mode 100644
index 000000000..cc13ed577
--- /dev/null
+++ b/1040/CH5/EX5.3/Chapter5_Ex3_Output.txt
@@ -0,0 +1,21 @@
+

+ OUTPUT Ex5.3.a

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

+The Overall Heat transfer coefficient for given Velocities

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

+  u(velocity)     U

+  (ft/s)     (cal/cm2 sec K)

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

+ 1.5     2.704991E-03

+ 3.0     4.240314E-03

+

+

+ OUTPUT Ex5.3.b

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

+The Peak Radial average bed temperature for given Velocities

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

+  u(velocity)     delta_T

+  (ft/s)           (°C)

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

+  1.5 	  	  25

+  3.0 	  	  16
\ No newline at end of file
diff --git a/1040/CH5/EX5.3/Ex5_3.sce b/1040/CH5/EX5.3/Ex5_3.sce
new file mode 100644
index 000000000..8e94e72a7
--- /dev/null
+++ b/1040/CH5/EX5.3/Ex5_3.sce
@@ -0,0 +1,123 @@
+//Harriot P.,2003,Chemical Reactor Design (I-Edition) Marcel Dekker,Inc.,USA,pp 436.

+//Chapter-5 Ex5.3 Pg No. 209

+//Title:Overall heat transfer coefficients and radial average bed temperature for packed bed reactor

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

+clear

+clc

+

+// COMMON INPUT

+k_s= 8*10^(-4);//(cal/sec cm°C)

+M_air_avg=29.24;// Average Molecular weight of air

+Cp_air_mol=7.91;// cal/mol°C;

+Cp_air_g=Cp_air_mol/M_air_avg;//cal/g°C

+dp=0.4;//Size of the catalyst pellet (cm)

+D=3.8;//Diameter of tube (cm)

+R_pellet=D/2;//Radius

+f_EO=0.7;//Fraction  of ethylene forming ethylene oxide 

+f_CO2_H2O=1-f_EO;//Fraction  of ethylene forming CO2 and H2O

+rho_p=2.5;//Density of catalyst particle (g/cm3)

+V_ref=22400;//Reference volume(cm3)

+T_ref=273;// Reference Temperature (K)

+P_ref=1;//Reference  Pressure (atm)

+P=5;//System Pressure (atm)

+T_C=230;//System Temperature (°C)

+T=T_C+273;//System Temperature (K)

+u_ft=[1.5 3];//Velocity (ft/s)

+myu=0.026*(10^(-2));//Viscosity of air (Poise)

+M_wt=[28 32 44 28];//Molecular weight

+M_fraction=[0.04 0.07 0.06 0.83];

+Cp=[15.3 7.4 10.7 7.4];//(cal/mol°C)

+k_g=9.27*10^(-5);//(cal/sec cm°C)

+del_H_rxn=[-29.9 -317];//(kcal/mol)

+E=18*1000;//Activation Energy (cal)

+R=1.987;//Gas Constant (cal/K.mol)

+

+//CALCULATION (Ex5.3.a)

+rho=M_air_avg*P*T_ref/(V_ref*P_ref*T);

+u=30.533.*u_ft;//Velocity in (cm/s)

+Re_p=(rho*dp/myu).*u;

+Pr=Cp_air_g*myu/k_g;

+ks_by_kg=k_s/k_g;

+k0e_by_kg=3.5;//From figure 5.16 Pg. No. 203

+kr_by_kg=2.5;//From equation 5.68 and 5.69  Pg. No. 204

+for i=1:2

+    ktd_by_k_air(i)=(0.1*Pr)*Re_p(i);

+ke_by_kg(i)=(k0e_by_kg+kr_by_kg)+ktd_by_k_air(i);

+k_e(i)=ke_by_kg(i)*k_g;

+h_bed(i)=4*k_e(i)/R_pellet;

+Nu_w(i)=(1.94*Pr^(0.33))*Re_p(i)^(0.5);//Refer equation 5.83  Pg. No. 208

+h_w(i)=(k_g/dp)*Nu_w(i);//(cal/sec cm2 K)

+h_j=100*10^(-3);//Assumed

+      U(i)=1/((1/h_j)+(1/h_w(i))+(1/h_bed(i)));

+end

+

+//CALCULATION (Ex5.3.b)

+minus_delH=f_EO*(-del_H_rxn(1))+f_CO2_H2O*(-del_H_rxn(2));

+T_max=T+20;

+del_Tc= R*(T_max)^2/E;

+T_new=250 +273;

+X_E=0.1;

+k250_by_k230=exp((E/R)*((1/T)-(1/T_new)));

+P_E=P*(1-X_E)*M_fraction(1);

+P_O2=P*(1-f_EO*X_E)*M_fraction(2);

+P_CO2=P*(1+f_CO2_H2O*X_E)*M_fraction(3);

+r=k250_by_k230*((0.076*P_E*P_O2)/(1+2*P_E+15*P_CO2));

+Q_dash=r*minus_delH*10^3/3600;

+epsilon=0.4;

+rho_bed=rho_p*(1-0.4);

+A_percm3=4/D;

+Q=(Q_dash*rho_bed)

+for i=1:2

+    delta_T(i)=(Q/A_percm3)*(1/U(i));

+end

+

+//OUTPUT ((Ex5.3.a))

+mprintf('\n OUTPUT Ex5.3.a');

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

+mprintf('\nThe Overall Heat transfer coefficient for given Velocities' )

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

+mprintf('\n  u(velocity)     U')

+mprintf('\n  (ft/s)     (cal/cm2 sec K)')

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

+for i=1:2

+    mprintf('\n %0.1f     %3E',u_ft(i),U(i))

+end

+

+//OUTPUT ((Ex5.3.b)

+mprintf('\n\n\n OUTPUT Ex5.3.b');

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

+mprintf('\nThe Peak Radial average bed temperature for given Velocities' )

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

+mprintf('\n  u(velocity)     delta_T')

+mprintf('\n  (ft/s)           (°C)')

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

+for i=1:2

+    mprintf('\n  %0.1f \t  \t  %0.0f',u_ft(i),delta_T(i))

+end

+

+//FILE OUTPUT

+fid= mopen('.\Chapter5-Ex3-Output.txt','w');

+mfprintf(fid,'\n OUTPUT Ex5.3.a');

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

+mfprintf(fid,'\nThe Overall Heat transfer coefficient for given Velocities' )

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

+mfprintf(fid,'\n  u(velocity)     U')

+mfprintf(fid,'\n  (ft/s)     (cal/cm2 sec K)')

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

+for i=1:2

+    mfprintf(fid,'\n %0.1f     %3E',u_ft(i),U(i))

+end

+mfprintf(fid,'\n\n\n OUTPUT Ex5.3.b');

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

+mfprintf(fid,'\nThe Peak Radial average bed temperature for given Velocities' )

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

+mfprintf(fid,'\n  u(velocity)     delta_T')

+mfprintf(fid,'\n  (ft/s)           (°C)')

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

+for i=1:2

+    mfprintf(fid,'\n  %0.1f \t  \t  %0.0f',u_ft(i),delta_T(i))

+end

+mclose(fid);

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

+

+