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diff --git a/530/CH8/EX8.1/example_8_1.sce b/530/CH8/EX8.1/example_8_1.sce
new file mode 100755
index 000000000..2032008c0
--- /dev/null
+++ b/530/CH8/EX8.1/example_8_1.sce
@@ -0,0 +1,44 @@
+clear;

+clc;

+

+// A Textbook on HEAT TRANSFER by S P SUKHATME

+// Chapter 8

+// Condensation and Boiling

+

+

+// Example 8.1

+// Page 318

+printf("Example 8.1, Page 318 \n \n");

+Ts = 80 ; // [C]

+Tw = 70 ; // [C]

+L = 1 ; // [m]

+g = 9.8 ; // [m/s^2]

+

+// Assuming condensate film is laminar and Re < 30

+Tm = (Ts + Tw)/2 ;

+// From table A.1

+rho = 978.8 ; // [kg/m^3]

+k = 0.672 ; // [W/m K]

+u = 381 *10^-6 ; // [kg/m s]

+v = u/rho ;

+// At 80 C,

+lambda = 2309 ; // [kJ/kg]

+// Substituting in eqn 8.3.9, we get

+h = 0.943*[(lambda*1000*(rho^2)*g*(k^3))/((Ts-Tw)*u*L)]^(1/4); // [W/m^2 K]

+

+rate = h*L*(Ts-Tw)/(lambda*1000); // [kg/m s]

+Re = 4*rate/u;

+printf("Assuming condensate film is laminar and Re < 30 \n");

+printf("h = %f W/m^2 K\n",h);

+printf("Re_L = %f \n",Re);

+printf("Initial assumption was wrong, Now considering the effect of ripples, we get\n");

+

+// Substituting h = Re*(lambda*1000)*u/(4*L*(Ts-Tw)), in eqn 8.3.12

+Re = [[[4*L*(Ts-Tw)*k/(lambda*1000*u)*(g/(v^2))^(1/3)]+5.2]/1.08]^(1/1.22);

+// From eqn 8.3.12

+h = [Re/(1.08*(Re^1.22)-5.2)]*k*((g/v^2)^(1/3)); // [W/m^2 K]

+m = h*L*10/(lambda*1000); // rate of condensation , [kg/m s]

+

+printf("Re = %f \n",Re);

+printf("Heat Transfer Cofficient = %f W/m^2 K \n",h);

+printf("Rate of condensation = %f kg/m s",m);
\ No newline at end of file
diff --git a/530/CH8/EX8.2/example_8_2.sce b/530/CH8/EX8.2/example_8_2.sce
new file mode 100755
index 000000000..77775b641
--- /dev/null
+++ b/530/CH8/EX8.2/example_8_2.sce
@@ -0,0 +1,34 @@
+clear;

+clc;

+

+// A Textbook on HEAT TRANSFER by S P SUKHATME

+// Chapter 8

+// Condensation and Boiling

+

+

+// Example 8.2

+// Page 321

+printf("Example 8.2, Page 321 \n \n");

+

+Ts = 262 ; // [K]

+D = 0.022 ; // [m]

+Tw = 258 ; // [K]

+

+Tm = (Ts+Tw)/2;

+// Properties at Tm

+rho = 1324 ; // [kg/m^3]

+k = 0.1008 ; // [W/m K]

+v = 1.90*10^-7 // [m^2/s];

+lambda = 215.1*10^3 ; // [J/kg]

+g = 9.81 ; // [m/s^2]

+u = v*rho ; // Viscosity

+

+// From eqn 8.4.1

+h = 0.725*[lambda*(rho^2)*g*(k^3)/((Ts-Tw)*u*D)]^(1/4);

+

+rate = h*%pi*D*(Ts-Tw) /lambda ; // [kg/s m]

+Re = 4*rate/u ;

+

+printf("Heat transfer coefficient = %f W/m^2 K\n",h);

+printf("Condensation rate per unit length = %f kg/s m \n",rate);

+printf("Film Reynolds number = %f \n",Re);

diff --git a/530/CH8/EX8.3/example_8_3.sce b/530/CH8/EX8.3/example_8_3.sce
new file mode 100755
index 000000000..3e8594cc8
--- /dev/null
+++ b/530/CH8/EX8.3/example_8_3.sce
@@ -0,0 +1,68 @@
+clear;

+clc;

+

+// A TeTwtbook on HEAT TRANSFER by S P SUKHATME

+// Chapter 8

+// Condensation and Boiling

+

+

+// ETwample 8.3

+// Page 322

+printf("Example 8.3, Page 322 \n \n");

+

+m = 25/60 ; // [kg/sec]

+ID = 0.025 ; // [m]

+OD = 0.029 ; // [m]

+Tci = 30 ; // [C]

+Tce = 70 ; // [C]

+g = 9.8 ; // [m/s^2]

+

+Ts = 100 ; // [C]

+// Assuming 5.3.2 is valid, properties at 50 C 

+// Properties at Tm

+rho = 988.1 ; // [kg/m^3]

+k = 0.648 ; // [W/m K]

+v = 0.556*10^-6 // [m^2/s];

+Pr = 3.54 ;

+Re = 4*m/(%pi*ID*rho*v);

+// From eqn 4.6.4a

+f = 0.005635;

+// From eqn 5.3.2

+Nu = 198.39 ;

+h = Nu*k/ID ;

+

+// Assuming average wall temperature = 90 C

+Tw = 90 ; // [C]

+Tm = (Tw+Ts)/2;

+// Properties at Tm

+// Properties at Tm

+rho = 961.9 ; // [kg/m^3]

+k = 0.682 ; // [W/m K]

+u = 298.6*10^-6 ; // [kg/m s]

+lambda = 2257*10^3 ; // [J/kg]

+

+h = 0.725*[lambda*(rho^2)*g*(k^3)/((Ts-Tw)*u*OD)]^(1/4);

+// Equating the heat flow from the condensing steam to the tube wall, to the heat flow from the tube wall to the flowing water.

+// Solving the simplified equation

+function[f] =temp(Tw)

+    f=(100-Tw)^(3/4)-8.3096/[log((Tw-Tci)/(Tw-Tce))];

+    funcprot(0);

+endfunction

+

+T=fsolve(Tw,temp);

+printf("Temperature obtained from trial and error = %f C \n",T);

+

+// Therefore

+hc = 21338.77/(100-T)^(1/4); // [W/m^2 K]

+printf("h_c = %f W/m^2 K \n",hc);

+

+// Now, equating the heat flowing from the condensing steam to the tube wall to the heat gained by the water, we have

+function[g] =lngth(l)

+    g=hc*(%pi*OD*l)*(100-T)-m*4174*(Tce-Tci);

+    funcprot(0);

+endfunction

+

+l = 0; // (initial guess, assumed value for fsolve function)

+L = fsolve(l,lngth);

+printf("\nLength of the tube = %f m \n",L);

+

diff --git a/530/CH8/EX8.4/example_8_4.sci b/530/CH8/EX8.4/example_8_4.sci
new file mode 100755
index 000000000..4651e6edd
--- /dev/null
+++ b/530/CH8/EX8.4/example_8_4.sci
@@ -0,0 +1,129 @@
+clear;

+clc;

+

+//Properties at (Tw+Ts)/2 = 100.5 degree celsius

+deltaT1 = 1;                  //in degree celsius

+p1 = 7.55e-4;           //[K^(-1) p1 is coefficient of cubical expansion

+v1 = 0.294e-6;                //[m^2/sec]  viscosity at 100.5 degree celsius

+k1 = 0.683;                  //[W/m-k]thermal conductivity

+Pr1 = 1.74;                  //Prandtl number

+g = 9.81;                    //acceleration due to gravity

+L = 0.14e-2;                 //diameter in meters

+//Properties at (Tw+Ts)/2 =102.5

+deltaT2 = 5;                 //in degree celsius

+p2 = 7.66e-4;            //[K^(-1) p1 is coefficient of cubical expansion

+v2 = 0.289e-6;            //[m^2/sec]  viscosity at 102.5 degree celsius 

+k2 = 0.684;                 //[W/m-k]thermal conductivity

+Pr2 = 1.71;                  //Prandtl number 

+//Properties at (Tw+Ts)/2 =105

+deltaT3 = 10;                 //in degree celsius

+p3 = 7.80e-4;            //[K^(-1) p1 is coefficient of cubical expansion

+v3 = 0.284e-6;            //[m^2/sec]  viscosity at 105 degree celsius 

+k3 = 0.684;                 //[W/m-k]thermal conductivity

+Pr3 = 1.68;                  //Prandtl number 

+

+function[Ra]=Rayleigh_no(p,deltaT,v,Pr)

+     Ra = [(p*g*deltaT*L^3)/(v^2)]*Pr;

+     funcprot(0);

+endfunction 

+

+function[q] = flux(k,deltaT,Rai,v)

+    q=(k/L)*(deltaT)*{0.36+(0.518*Rai^(1/4))/[1+(0.559/v)^(9/16)]^(4/9)};

+    funcprot(0);

+endfunction

+

+Ra = Rayleigh_no(p1,deltaT1,v1,Pr1);

+q1 = flux(k1,deltaT1,Ra,Pr1);

+printf("\n q/A = %.1f W/m^2 at (Tw-Ts)=1",q1);

+Ra = Rayleigh_no(p2,deltaT2,v2,Pr2);

+q2 = flux(k2,deltaT2,Ra,Pr2);

+printf("\n q/A = %.1f W/m^2 at (Tw-Ts)=5",q2);

+Ra = Rayleigh_no(p3,deltaT3,v3,Pr3);

+q3 = flux(k3,deltaT3,Ra,Pr3);

+printf("\n q/A = %.1f W/m^2 at (Tw-Ts)=10",q3);

+

+//At 100 degree celsius

+Cpl = 4.220;          //[kJ/kg]

+lamda = 2257;         //[kJ/kg]

+ul = 282.4e-6;        //viscosity is in kg/m-sec

+sigma = 589e-4;       //Surface tension is in N/m

+pl = 958.4;           //density in kg/m^3

+pv =0.598;            //density of vapour in kg/m^3

+deltap = pl-pv;

+Prl = 1.75;           //Prandtl no. of liquid

+Ksf = 0.013;

+function[q1]=heat_flux(deltaT)

+    q1=141.32*deltaT^3;

+    funcprot(0);

+endfunction

+

+printf("\n q/A at deltaT = 5 degree celsius = %.1f W/m^2",heat_flux(5));

+printf("\nq/A at deltaT = 10 degree celsius = %.1f W/m^2",heat_flux(10));

+printf("\n q/A at deltaT =20 degree celsius = %.1f W/m^2",heat_flux(20));

+//qi = [heat_flux(5),heat_flux(10),heat_flux(20)];

+q = [q1 q2 q3];

+i=1;

+while i<=10

+    T(i)=i;

+    ql(i) = heat_flux(i);

+    i=i+1;

+end

+plot2d([1 5 10],q);

+plot2d(T,ql);

+xtitle("Boiling curve","(Tw - Ts)degree celsius","Heat flux,(q/A)W/m^2");

+L1 = (L/2)*[g*(pl-pv)/sigma]^(1/2);

+printf("\n Peak heat flux L = %.3f ",L1);    

+f_L = 0.89+2.27*exp(-3.44*L1^(0.5));

+printf("\n f(l) = %.4f",f_L);

+q2 = f_L*{(%pi/24)*lamda*10^(3)*pv^(0.5)*[sigma*g*(pl-pv)]^(0.25)};

+printf("\n q/A = %.3e W/m^2",q2);

+

+Tn = poly([0],'Tn');

+Tn1 = roots(141.32*Tn^3 - q2);

+printf("\n Tw-Ts = %.1f degree celsius",Tn1(3));

+

+

+

+printf("\n\n Minimum heat flux");

+q3 = 0.09*lamda*10^3*pv*[sigma*g*(pl-pv)/(pl+pv)^(2)]^(0.25);

+printf("\n q/A = %d W/m^2",q3);

+printf("\n\n Stable film boiling");

+Ts1 = 140;          //surface temperature in degree celsius

+Ts2 = 200;          //surface temperature in degree celsius

+Ts3 = 600;          //surface temperature in degree celsius

+Twm1 = (140+100)/2; //Mean film temperature

+//properties of steam at 120 degree celsius and 1.013 bar

+kv = 0.02558;       //thermal conductivity in W/mK

+pv1 = 0.5654;       //vapor density in kg/m^3

+uv=13.185*10^(-6);  //viscosity of vapour in kg/m sec

+lamda1 = (2716.1-419.1)*10^(3);//Latent heat of fusion in J/kg

+hc = 0.62*[(kv^3)*pv*(pl-pv)*g*lamda1/(L*uv*(140-100))]^(0.25);

+printf("\n hc = %.2f W/m^2",hc);

+qrad = 5.67*10^(-8)*(413^4 - 373^4)/[(1/0.9)+1-1];

+printf("\n q/A due to radiation = %.2f W/m^2",qrad);

+hr = qrad/(413-373);

+printf("\n hr = %.2f W/m^2 K ",hr);

+

+printf("\n Since hr<hc ");

+printf("\n The total heat transfer coefficient ");

+h = hc + 0.75*hr;

+printf(" h = %.2f W/m^2 K",h);

+printf("\n Total heat flux = %.3f W/m^2 K",h*(140-100));

+

+hc_200 = 0.62*[(kv^3)*pv*(pl-pv)*g*lamda1/(L*uv*(200-100))]^(0.25);

+qrad1 = 5.67*10^(-8)*(473^4 - 373^4)/[(1/0.9)+1-1];

+hr_200 = qrad1/(200-100);

+printf("\n\n hc = %.2f W/m^2",hc_200);

+printf("\n hr = %.2f W/m^2 K",hr_200);

+printf("\n q/A due to radiation = %.2f W/m^2",qrad1);

+h_200 = hc_200 +0.75*hr_200;

+printf("\n Total heat flux = %d W/m^2",h_200*100);

+hc_600 = 0.62*[(kv^3)*pv*(pl-pv)*g*lamda1/(L*uv*(600-100))]^(0.25);

+qrad2 = 5.67*10^(-8)*(873^4 - 373^4)/[(1/0.9)+1-1];

+hr_600 = qrad1/(600-100)

+printf("\n\n hc = %.2f W/m^2",hc_600);

+printf("\n hr = %.2f W/m^2 K",hr_600);

+printf("\n q/A due to radiation = %.2f W/m^2",qrad2);

+

+

+

diff --git a/530/CH8/EX8.5/example_8_5.sce b/530/CH8/EX8.5/example_8_5.sce
new file mode 100755
index 000000000..0874299a5
--- /dev/null
+++ b/530/CH8/EX8.5/example_8_5.sce
@@ -0,0 +1,45 @@
+clear;

+clc;

+

+// A Textbook on HEAT TRANSFER by S P SUKHATME

+// Chapter 8

+// Condensation and Boiling

+

+

+// Example 8.5

+// Page 337

+printf("Example 8.5, Page 337 \n \n");

+

+D = 0.02 ; // [m]

+l = 0.15 ; // [m]

+T = 500+273 ; // [K]

+Tc = -196+273 ; // [K]

+e = 0.4;

+s = 5.670*10^-8;

+// Film boiling will occur, hence eqn 8.7.9 is applicable

+Tm = (T+Tc)/2;

+

+// Properties

+k = 0.0349 ; // [W/m K]

+rho = 0.80 ; // [kg/m^3]

+u = 23*10^-6 ; // [kg/m s]

+

+Cp_avg = 1.048 ; // [kJ/kg J]

+rho_liq = 800 ; // [kg/m^3]

+latent = 201*10^3 ; // [J/kg]

+

+lambda = [latent + Cp_avg*(Tm-Tc)*1000]; // [J/kg]

+h_c = 0.62*[((k^3)*rho*799.2*9.81*lambda)/(D*u*(T-Tc))]^(1/4); // [W/m^2 K]

+

+// Taking the emissivity of liquid surface to be unity and using equation 3.9.1, the exchange of radiant heat flux

+flux = s*(T^4-Tc^4)/(1/e+1/1-1); // [W/m^2]

+h_r = flux/(T-Tc);

+

+// Since h_r < h_c, total heat transfer coefficient is determined from eqn 8.7.11

+h = h_c+3/4*h_r; // [W/m^2 K]

+

+flux_i = h*(T-Tc);

+Rate = flux_i*%pi*D*l; // [W]

+

+printf("Initial heat flux = %f W/m^2 \n",flux_i);

+printf("Initial heat transfer rate = %f W",Rate);
\ No newline at end of file