diff options
Diffstat (limited to '534')
99 files changed, 3323 insertions, 0 deletions
diff --git a/534/CH1/EX1.1/1_1_Wall_Heat_Loss.sce b/534/CH1/EX1.1/1_1_Wall_Heat_Loss.sce new file mode 100644 index 000000000..e92a71d6a --- /dev/null +++ b/534/CH1/EX1.1/1_1_Wall_Heat_Loss.sce @@ -0,0 +1,20 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.1 Page 5 ')//Example 1.1
+// Find Wall Heat Loss - Problem of Pure Conduction Unidimensional Heat
+
+L=.15; //[m] - Thickness of conducting wall
+delT = 1400 - 1150; //[K] - Temperature Difference across the Wall
+A=.5*1.2; //[m^2] - Cross sectional Area of wall = H*W
+k=1.7; //[W/m.k] - Thermal Conductivity of Wall Material
+
+//Using Fourier's Law eq 1.2
+Q = k*delT/L; //[W/m^2] - Heat Flux
+
+q = A*Q; //[W] - Rate of Heat Transfer
+
+printf("\n \n Heat Loss through the Wall = %.2f W",q);
+//END
+
+
+
diff --git a/534/CH1/EX1.2/1_2_Emissive_Power_Irradiation.sce b/534/CH1/EX1.2/1_2_Emissive_Power_Irradiation.sce new file mode 100644 index 000000000..20610d7e4 --- /dev/null +++ b/534/CH1/EX1.2/1_2_Emissive_Power_Irradiation.sce @@ -0,0 +1,26 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.2 Page 11 \n')// Example 1.2
+// Find a) Emissive Power & Irradiation b)Total Heat Loss per unit length
+
+d=.07; //[m] - Outside Diameter of Pipe
+Ts = 200+273.15; //[K] - Surface Temperature of Steam
+Tsurr = 25+273.15; //[K] - Temperature outside the pipe
+e=.8; // Emissivity of Surface
+h=15; //[W/m^2.k] - Thermal Convectivity from surface to air
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+//Using Eq 1.5
+E = e*stfncnstt*Ts^4; //[W/m^2] - Emissive Power
+G = stfncnstt*Tsurr^4; //[W/m^2] - Irradiation falling on surface
+
+printf("\n (a) Surface Emissive Power = %.2f W/m^2",E);
+printf("\n Irradiation Falling on Surface = %.2f W/m^2",G);
+
+//Using Eq 1.10 Total Rate of Heat Transfer Q = Q by convection + Q by radiation
+q = h*(%pi*d)*(Ts-Tsurr)+e*(%pi*d)*stfncnstt*(Ts^4-Tsurr^4); //[W]
+
+printf("\n\n (b) Total Heat Loss per unit Length of Pipe= %.2f W",q);
+//END
+
+
+
diff --git a/534/CH1/EX1.3/1_3_Theoretical_Problem.sce b/534/CH1/EX1.3/1_3_Theoretical_Problem.sce new file mode 100644 index 000000000..64bc95f58 --- /dev/null +++ b/534/CH1/EX1.3/1_3_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.3 Page 18 \n')// Example 1.3
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH1/EX1.4/1_4_Coolant_Fuid_Velocity.sce b/534/CH1/EX1.4/1_4_Coolant_Fuid_Velocity.sce new file mode 100644 index 000000000..814df67ef --- /dev/null +++ b/534/CH1/EX1.4/1_4_Coolant_Fuid_Velocity.sce @@ -0,0 +1,30 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.4 Page 20 \n')// Example 1.4
+// Find Velocity of Coolant Fluid
+
+Ts = 56.4+273.15; //[K] - Surface Temperature of Steam
+Tsurr = 25+273.15; //[K] - Temperature of Surroundings
+e=.88; // Emissivity of Surface
+
+//As h=(10.9*V^.8)[W/m^2.k] - Thermal Convectivity from surface to air
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+
+A=2*.05*.05; // [m^2] Area for Heat transfer i.e. both surfaces
+
+E = 11.25; //[W] Net heat to be removed by cooling air
+
+Qrad = e*stfncnstt*A*(Ts^4-Tsurr^4);
+
+//Using Eq 1.10 Total Rate of Heat Transfer Q = Q by convection + Q by radiation
+Qconv = E - Qrad;//[W]
+
+//As Qconv = h*A*(Ts-Tsurr) & h=10.9 Ws^(.8)/m^(-.8)K.V^(.8)
+
+V = [Qconv/(10.9*A*(Ts-Tsurr))]^(1/0.8);
+
+printf("\n\n Velocity of Cooling Air flowing= %.2f m/s",V);
+//END
+
+
+
diff --git a/534/CH1/EX1.5/1_5_Theoretical_Problem.sce b/534/CH1/EX1.5/1_5_Theoretical_Problem.sce new file mode 100644 index 000000000..e7156c2eb --- /dev/null +++ b/534/CH1/EX1.5/1_5_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.5 Page 23 \n')// Example 1.5
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH1/EX1.6/1_6_Human_Body_Heat_Loss.sce b/534/CH1/EX1.6/1_6_Human_Body_Heat_Loss.sce new file mode 100644 index 000000000..9c8c40257 --- /dev/null +++ b/534/CH1/EX1.6/1_6_Human_Body_Heat_Loss.sce @@ -0,0 +1,48 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.6 Page 26 ')// Example 1.6
+// Find Skin Temperature & Heat loss rate
+
+A=1.8; // [m^2] Area for Heat transfer i.e. both surfaces
+Ti = 35+273; //[K] - Inside Surface Temperature of Body
+Tsurr = 297; //[K] - Temperature of surrounding
+Tf = 297; //[K] - Temperature of Fluid Flow
+e=.95; // Emissivity of Surface
+L=.003; //[m] - Thickness of Skin
+k=.3; // Effective Thermal Conductivity
+h=2; //[W/m^2.k] - Natural Thermal Convectivity from body to air
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+//Using Eq 1.5
+
+Tsa=305; //[K] Body Temperature Assumed
+
+i=-1;
+while(i==-1)
+ hr = e*stfncnstt*(Tsa+Tsurr)*(Tsa^2+Tsurr^2); //[W/m^2.K] - Radiative Heat transfer Coeff on assumption
+
+ //Using Eq 1.8 & Eq 1.9 k(Ti-Ts)/L = h(Ts - Tf) + hr(Ts - Tsurr)
+Ts = (k*Ti/L + (h+hr)*Tf)/(k/L +(h+hr));
+ c=abs(Ts-Tsa);
+ if(c<=0.0001)
+ i=1;
+ break;
+ end
+ Tsa=Ts;
+end
+
+q = k*A*(Ti-Ts)/L; //[W]
+
+printf("\n\n (I) In presence of Air")
+printf("\n (a) Temperature of Skin = %.2f K",Ts);
+printf("\n (b) Total Heat Loss = %.2f W",q);
+
+//When person is in Water
+h = 200; //[W/m^2.k] - Thermal Convectivity from body to water
+hr = 0; // As Water is Opaque for Thermal Radiation
+Ts = (k*Ti/L + (h+hr)*Tf)/(k/L +(h+hr)); //[K] Body Temperature
+q = k*A*(Ti-Ts)/L; //[W]
+printf("\n\n (II) In presence of Water")
+printf("\n (a) Temperature of Skin = %.2f K",Ts);
+printf("\n (b) Total Heat Loss = %.2f W",q);
+
+//END
\ No newline at end of file diff --git a/534/CH1/EX1.7/1_7_Cure_Temperature.sce b/534/CH1/EX1.7/1_7_Cure_Temperature.sce new file mode 100644 index 000000000..83187249c --- /dev/null +++ b/534/CH1/EX1.7/1_7_Cure_Temperature.sce @@ -0,0 +1,58 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.7 Page 30 \n')//Example 1.7
+// (a) Cure Temperature for h = 15 W/m^2
+// (b) Value of h for cure temp = 50 deg C
+
+Tsurr = 30+273; //[K] - Temperature of surrounding
+Tf = 20+273; //[K] - Temperature of Fluid Flow
+e=.5; // Emissivity of Surface
+a = .8; // Absorptivity of Surface
+G = 2000; //[W/m^2] - Irradiation falling on surface
+h=15; //[W/m^2.k] - Thermal Convectivity from plate to air
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+T=375; //[K] Value initially assumed for trial-error approach
+//Using Eq 1.3a & 1.7 and trial-and error approach of Newton Raphson
+while(1>0)
+f=((a*G)-(h*(T-Tf)+e*stfncnstt*(T^4 - Tsurr^4)));
+fd=(-h*T-4*e*stfncnstt*T^3);
+Tn=T-f/fd;
+if(((a*G)-(h*(Tn-Tf)+e*stfncnstt*(Tn^4 - Tsurr^4)))<=.01)
+ break;
+end;
+T=Tn;
+end
+
+printf("\n (a) Cure Temperature of Plate = %i degC\n",T-273);
+//solution (b)
+Treq=50+273;
+function[T]=Tvalue(h)
+ T=240;
+ while(1>0)
+ f=((a*G)-(h*(T-Tf)+e*stfncnstt*(T^4 - Tsurr^4)));
+ fd=(-h*T-4*e*stfncnstt*T^3);
+ Tn=T-f/fd;
+ if(((a*G)-(h*(Tn-Tf)+e*stfncnstt*(Tn^4 - Tsurr^4)))<=.01)
+ break;
+ end;
+ T=Tn;
+ end
+ funcprot(0)
+endfunction
+
+h = [2:.5:100];
+Tm = [1:1:197];
+for i=1:1:197;
+ Tm(i)=Tvalue(h(i));
+end
+
+T=Treq;
+hnew=((a*G)-(e*stfncnstt*(T^4 - Tsurr^4)))/(T-Tf);
+clf()
+xtitle("Graph Temp vs Convection Coeff", "h (W/m^2/K)", "T (degC)");
+x=[0 hnew hnew];
+y=[Treq-273 Treq-273 0];
+plot(h,Tm-273,x,y);
+legend("Plot","h at T = 50 degC");
+printf("\n (b) Air flow must provide a convection of = %i W/m^2.K", hnew);
+//END
\ No newline at end of file diff --git a/534/CH1/EX1.8/1_8_Theoretical_Problem.sce b/534/CH1/EX1.8/1_8_Theoretical_Problem.sce new file mode 100644 index 000000000..2d458cad6 --- /dev/null +++ b/534/CH1/EX1.8/1_8_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 1.8 Page 40 \n')// Example 1.8
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH10/EX10.1/10_1_Boiling_Water_pan.sce b/534/CH10/EX10.1/10_1_Boiling_Water_pan.sce new file mode 100644 index 000000000..93db94d87 --- /dev/null +++ b/534/CH10/EX10.1/10_1_Boiling_Water_pan.sce @@ -0,0 +1,35 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 10.1 Page 632 \n'); //Example 10.1
+// Power Required by electruc heater to cause boiling
+// Rate of water evaporation due to boiling
+// Critical Heat flux corresponding to the burnout point
+
+//Operating Conditions
+Ts = 118+273 ;//[K] Surface Temperature
+Tsat = 100+273 ;//[K] Saturated Temperature
+D = .3 ;//[m] Diameter of pan
+g = 9.81 ;//[m^2/s] gravitaional constant
+//Table A.6 Saturated water Liquid Properties T = 373 K
+rhol = 957.9 ;//[kg/m^3] Density
+cp = 4.217*10^3 ;//[J/kg] Specific Heat
+u = 279*10^-6 ;//[N.s/m^2] Viscosity
+Pr = 1.76 ;// Prandtl Number
+hfg = 2257*10^3 ;//[J/kg] Specific Heat
+si = 58.9*10^-3 ;//[N/m]
+//Table A.6 Saturated water Vapor Properties T = 373 K
+rhov = .5956 ;//[kg/m^3] Density
+
+Te = Ts-Tsat;
+//From Table 10.1
+C = .0128;
+n = 1;
+q = u*hfg*[g*(rhol-rhov)/si]^.5*(cp*Te/(C*hfg*Pr^n))^3;
+qs = q*%pi*D^2/4;
+
+m = qs/hfg;
+
+qmax = .149*hfg*rhov*[si*g*(rhol-rhov)/rhov^2]^.25;
+
+printf("\n Boiling Heat transfer rate = %.1f kW \n Rate of water evaporation due to boiling = %i kg/h \n Critical Heat flux corresponding to the burnout point = %.2f MW/m^2",qs/1000,m*3600,qmax/10^6);
+//END
\ No newline at end of file diff --git a/534/CH10/EX10.2/10_2_Horizontal_cylinder.sce b/534/CH10/EX10.2/10_2_Horizontal_cylinder.sce new file mode 100644 index 000000000..97bf09ef6 --- /dev/null +++ b/534/CH10/EX10.2/10_2_Horizontal_cylinder.sce @@ -0,0 +1,43 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 10.2 Page 635 \n'); //Example 10.2
+// Power Dissipation per unith length for the cylinder, qs
+
+//Operating Conditions
+Ts = 255+273 ;//[K] Surface Temperature
+Tsat = 100+273 ;//[K] Saturated Temperature
+D = 6*10^-3 ;//[m] Diameter of pan
+e = 1 ;// eimssivity
+stfncnstt=5.67*10^(-8) ;// [W/m^2.K^4] - Stefan Boltzmann Constant
+g = 9.81 ;//[m^2/s] gravitaional constant
+//Table A.6 Saturated water Liquid Properties T = 373 K
+rhol = 957.9 ;//[kg/m^3] Density
+hfg = 2257*10^3 ;//[J/kg] Specific Heat
+//Table A.4 Water Vapor Properties T = 450 K
+rhov = .4902 ;//[kg/m^3] Density
+cpv = 1.98*10^3 ;//[J/kg.K] Specific Heat
+kv = 0.0299 ;//[W/m.K] Conductivity
+uv = 15.25*10^-6 ;//[N.s/m^2] Viscosity
+
+Te = Ts-Tsat;
+
+hconv = .62*[kv^3*rhov*(rhol-rhov)*g*(hfg+.8*cpv*Te)/(uv*D*Te)]^.25;
+hrad = e*stfncnstt*(Ts^4-Tsat^4)/(Ts-Tsat);
+
+//From eqn 10.9 h^(4/3) = hconv^(4/3) + hrad*h^(1/3)
+//Newton Raphson
+h=250; //Initial Assumption
+while(1>0)
+f = h^(4/3) - [hconv^(4/3) + hrad*h^(1/3)];
+fd = (4/3)*h^(1/3) - [(1/3)*hrad*h^(-2/3)];
+hn=h-f/fd;
+if((hn^(4/3) - [hconv^(4/3) + hrad*hn^(1/3)])<=.01)
+ break;
+end;
+h=hn;
+end
+
+q = h*%pi*D*Te;
+
+printf("\n Power Dissipation per unith length for the cylinder, qs= %i W/m",q);
+//END
\ No newline at end of file diff --git a/534/CH10/EX10.3/10_3_Condensation_Chimney.sce b/534/CH10/EX10.3/10_3_Condensation_Chimney.sce new file mode 100644 index 000000000..1153e9ae8 --- /dev/null +++ b/534/CH10/EX10.3/10_3_Condensation_Chimney.sce @@ -0,0 +1,36 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 10.3 Page 648 \n'); //Example 10.3
+// Heat Transfer and Condensation Rates
+
+//Operating Conditions
+Ts = 50+273 ;//[K] Surface Temperature
+Tsat = 100+273 ;//[K] Saturated Temperature
+D = .08 ;//[m] Diameter of pan
+g = 9.81 ;//[m^2/s] gravitaional constant
+L = 1 //[m] Length
+//Table A.6 Saturated Vapor Properties p = 1.0133 bars
+rhov = .596 ;//[kg/m^3] Density
+hfg = 2257*10^3 ;//[J/kg] Specific Heat
+//Table A.6 Saturated water Liquid Properties T = 348 K
+rhol = 975 ;//[kg/m^3] Density
+cpl = 4193 ; //[J/kg.K] Specific Heat
+kl = 0.668 ;//[W/m.K] Conductivity
+ul = 375*10^-6 ;//[N.s/m^2] Viscosity
+uvl = ul/rhol; ;//[N.s.m/Kg] Kinematic viscosity
+Ja = cpl*(Tsat-Ts)/hfg;
+hfg2 = hfg*(1+.68*Ja);
+//Equation 10.43
+Re = [3.70*kl*L*(Tsat-Ts)/(ul*hfg2*(uvl^2/g)^.33334)+4.8]^.82;
+
+//From equation 10.41
+hL = Re*ul*hfg2/(4*L*(Tsat-Ts));
+q = hL*(%pi*D*L)*(Tsat-Ts);
+
+m = q/hfg;
+//Using Equation 10.26
+del = [4*kl*ul*(Tsat-Ts)*L/(g*rhol*(rhol-rhov)*hfg2)]^.25;
+
+
+printf("\n Heat Transfer Rate = %.1f kW and Condensation Rates= %.4f kg/s \n And as del(L) %.3f mm << (D/2) %.2f m use of vertical cylinder correlation is justified",q/1000,m,del*1000,D/2);
+//END
\ No newline at end of file diff --git a/534/CH10/EX10.4/10_4_Steam_Condenser.sce b/534/CH10/EX10.4/10_4_Steam_Condenser.sce new file mode 100644 index 000000000..cb6a4ca11 --- /dev/null +++ b/534/CH10/EX10.4/10_4_Steam_Condenser.sce @@ -0,0 +1,32 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 10.4 Page 652 \n'); //Example 10.4
+// Condensation rate per unit length of tubes
+
+//Operating Conditions
+Ts = 25+273 ;//[K] Surface Temperature
+Tsat = 54+273 ;//[K] Saturated Temperature
+D = .006 ; //[m] Diameter of pan
+g = 9.81 ;//[m^2/s] gravitaional constant
+N = 20 // No of tubes
+
+//Table A.6 Saturated Vapor Properties p = 1.015 bar
+rhov = .098 ;//[kg/m^3] Density
+hfg = 2373*10^3 ;//[J/kg] Specific Heat
+//Table A.6 Saturated water Liquid Properties Tf = 312.5 K
+rhol = 992 ;//[kg/m^3] Density
+cpl = 4178 ;//[J/kg.K] Specific Heat
+kl = 0.631 ; //[W/m.K] Conductivity
+ul = 663*10^-6 ; //[N.s/m^2] Viscosity
+
+Ja = cpl*(Tsat-Ts)/hfg;
+hfg2 = hfg*(1+.68*Ja);
+//Equation 10.46
+h = .729*[g*rhol*(rhol-rhov)*kl^3*hfg2/(N*ul*(Tsat-Ts)*D)]^.25;
+//Equation 10.34
+m1 = h*(%pi*D)*(Tsat-Ts)/hfg2;
+
+m = N^2*m1;
+
+printf("\n For the complete array of tubes, the condensation per unit length is %.3f kg/s.m",m);
+//END
\ No newline at end of file diff --git a/534/CH11/EX11.1/11_1_Counterflow_tube_HeatX.sce b/534/CH11/EX11.1/11_1_Counterflow_tube_HeatX.sce new file mode 100644 index 000000000..15c8fd824 --- /dev/null +++ b/534/CH11/EX11.1/11_1_Counterflow_tube_HeatX.sce @@ -0,0 +1,51 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 11.1 Page 680 \n'); //Example 11.1
+// Tube Length to achieve a desired hot fluid temperature
+
+//Operating Conditions
+Tho = 60+273 ;//[K] Hot Fluid outlet Temperature
+Thi = 100+273 ; //[K] Hot Fluid intlet Temperature
+Tci = 30+273 ;//[K] Cold Fluid intlet Temperature
+mh = .1 ;//[kg/s] Hot Fluid flow rate
+mc = .2 ;//[kg/s] Cold Fluid flow rate
+Do = .045 ;//[m] Outer annulus
+Di = .025 ;//[m] Inner tube
+
+//Table A.5 Engine Oil Properties T = 353 K
+cph = 2131 ;//[J/kg.K] Specific Heat
+kh = .138 ; //[W/m.K] Conductivity
+uh = 3.25*10^-2 ; //[N.s/m^2] Viscosity
+//Table A.6 Saturated water Liquid Properties Tc = 308 K
+cpc = 4178 ;//[J/kg.K] Specific Heat
+kc = 0.625 ; //[W/m.K] Conductivity
+uc = 725*10^-6 ; //[N.s/m^2] Viscosity
+Pr = 4.85 ;//Prandtl Number
+
+q = mh*cph*(Thi-Tho);
+
+Tco = q/(mc*cpc)+Tci;
+
+T1 = Thi-Tco;
+T2 = Tho-Tci;
+Tlm = (T1-T2)/(2.30*log10(T1/T2));
+
+//Through Tube
+Ret = 4*mc/(%pi*Di*uc);
+printf("\n Flow through Tube has Reynolds Number as %i. Thus the flow is Turbulent", Ret);
+//Equation 8.60
+Nut = .023*Ret^.8*Pr^.4;
+hi = Nut*kc/Di;
+
+//Through Shell
+Reo = 4*mh*(Do-Di)/(%pi*uh*(Do^2-Di^2));
+printf("\n Flow through Tube has Reynolds Number as %i. Thus the flow is Laminar", Reo);
+//Table 8.2
+Nuo = 5.63;
+ho = Nuo*kh/(Do-Di);
+
+U = 1/[1/hi+1/ho];
+L = q/(U*%pi*Di*Tlm);
+
+printf("\n Tube Length to achieve a desired hot fluid temperature is %.1f m",L);
+//END
\ No newline at end of file diff --git a/534/CH11/EX11.2/11_2_Counterflow_plate_HeatX.sce b/534/CH11/EX11.2/11_2_Counterflow_plate_HeatX.sce new file mode 100644 index 000000000..79317e1c3 --- /dev/null +++ b/534/CH11/EX11.2/11_2_Counterflow_plate_HeatX.sce @@ -0,0 +1,71 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 11.2 Page 683 \n'); //Example 11.2
+// Exterior Dimensions of heat Exchanger
+// Pressure drops within the plate-type Heat exchanger with N=60 gaps
+
+//Operating Conditions
+Tho = 60+273 ;//[K] Hot Fluid outlet Temperature
+Thi = 100+273 ;//[K] Hot Fluid intlet Temperature
+Tci = 30+273 ;//[K] Cold Fluid intlet Temperature
+mh = .1 ;//[kg/s] Hot Fluid flow rate
+mc = .2 ;//[kg/s] Cold Fluid flow rate
+Do = .045 ;//[m] Outer annulus
+Di = .025 ;//[m] Inner tube
+
+//Table A.5 Engine Oil Properties T = 353 K
+cph = 2131 ;//[J/kg.K] Specific Heat
+kh = .138 ;//[W/m.K] Conductivity
+uh = 3.25*10^-2 ; //[N.s/m^2] Viscosity
+rhoh = 852.1 ;//[kg/m^3] Density
+//Table A.6 Saturated water Liquid Properties Tc = 308 K
+cpc = 4178 ;//[J/kg.K] Specific Heat
+kc = 0.625 ;//[W/m.K] Conductivity
+uc = 725*10^-6 ;//[N.s/m^2] Viscosity
+Pr = 4.85 ;//Prandtl Number
+rhoc = 994 ;//[kg/m^3] Density
+
+q = mh*cph*(Thi-Tho);
+
+Tco = q/(mc*cpc)+Tci;
+
+T1 = Thi-Tco;
+T2 = Tho-Tci;
+Tlm = (T1-T2)/(2.30*log10(T1/T2));
+
+N = linspace(20,80,100);
+L = q/Tlm*[1/(7.54*kc/2)+1/(7.54*kh/2)]*(N^2-N)^-1;
+clf();
+plot(N,L);
+xtitle("Size of Heat Xchanger vs Number of gaps", "Number of Gaps (N)", "L (m)");
+
+N2 = 60;
+L = q/((N2-1)*N2*Tlm)*[1/(7.54*kc/2)+1/(7.54*kh/2)];
+a = L/N2;
+Dh = 2*a ;//Hydraulic Diameter [m]
+//For water filled gaps
+umc = mc/(rhoc*L^2/2);
+Rec = rhoc*umc*Dh/uc;
+//For oil filled gaps
+umh = mh/(rhoh*L^2/2);
+Reh = rhoh*umh*Dh/uh;
+printf("\n Flow of the fluids has Reynolds Number as %.2f & %i. Thus the flow is Laminar for both", Reh,Rec);
+
+//Equations 8.19 and 8.22a
+delpc = 64/Rec*rhoc/2*umc^2/Dh*L ;//For water
+delph = 64/Reh*rhoh/2*umh^2/Dh*L ;//For oil
+
+//For example 11.1
+L1 = 65.9;
+Dh1c = .025;
+Dh1h = .02;
+Ret = 4*mc/(%pi*Di*uc);
+f = (.790*2.30*log10(Ret)-1.64)^-2 ;//friction factor through tube Eqn 8.21
+umc1 = 4*mc/(rhoc*%pi*Di^2);
+delpc1 = f*rhoc/2*umc1^2/Dh1c*L1;
+Reo = 4*mh*(Do-Di)/(%pi*uh*(Do^2-Di^2));
+umh1 = 4*mh/(rhoh*%pi*(Do^2-Di^2));
+delph1 = 64/Reo*rhoh/2*umh1^2/Dh1h*L1;
+
+printf("\n Exterior Dimensions of heat Exchanger L = %.3f m \n Pressure drops within the plate-type Heat exchanger with N=60 gaps\n For water = %.2f N/m^2 For oil = %.2f N/m^2\n Pressure drops tube Heat exchanger of example 11.1\n For water = %.1f kN/m^2 For oil = %.1f kN/m^2",L,delpc,delph,delpc1/1000,delph1/1000);
+//END
\ No newline at end of file diff --git a/534/CH11/EX11.3/11_3_Crossflow_finned_tube_HeatX.sce b/534/CH11/EX11.3/11_3_Crossflow_finned_tube_HeatX.sce new file mode 100644 index 000000000..ef5e9baa6 --- /dev/null +++ b/534/CH11/EX11.3/11_3_Crossflow_finned_tube_HeatX.sce @@ -0,0 +1,34 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 11.3 Page 692 \n'); //Example 11.3
+// Required gas side surface area
+
+//Operating Conditions
+Tho = 100+273 ;//[K] Hot Fluid outlet Temperature
+Thi = 300+273 ;//[K] Hot Fluid intlet Temperature
+Tci = 35+273 ;//[K] Cold Fluid intlet Temperature
+Tco = 125+273 ; //[K] Cold Fluid outlet Temperature
+mc = 1 ;//[kg/s] Cold Fluid flow rate
+Uh = 100 ;//[W/m^2.K] Coefficient of heat transfer
+//Table A.5 Water Properties T = 353 K
+cph = 1000 ; //[J/kg.K] Specific Heat
+//Table A.6 Saturated water Liquid Properties Tc = 308 K
+cpc = 4197 ; //[J/kg.K] Specific Heat
+
+Cc = mc*cpc;
+//Equation 11.6b and 11.7b
+Ch = Cc*(Tco-Tci)/(Thi-Tho);
+// Equation 11.18
+qmax = Ch*(Thi-Tci);
+//Equation 11.7b
+q = mc*cpc*(Tco-Tci);
+
+e = q/qmax;
+ratio = Ch/Cc;
+
+printf("\n As effectiveness is %.2f with Ratio Cmin/Cmax = %.2f, It follows from figure 11.14 that NTU = 2.1",e,ratio);
+NTU = 2.1;
+A = 2.1*Ch/Uh;
+
+printf("\n Required gas side surface area = %.1f m^2",A);
+//END
\ No newline at end of file diff --git a/534/CH11/EX11.4/11_4_Crossflow_finned_HeatX2.sce b/534/CH11/EX11.4/11_4_Crossflow_finned_HeatX2.sce new file mode 100644 index 000000000..b9730f03d --- /dev/null +++ b/534/CH11/EX11.4/11_4_Crossflow_finned_HeatX2.sce @@ -0,0 +1,36 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 11.4 Page 695 \n'); //Example 11.4
+// Heat Transfer Rate and Fluid Outlet Temperatures
+
+//Operating Conditions
+Thi = 250+273 ;//[K] Hot Fluid intlet Temperature
+Tci = 35+273 ;//[K] Cold Fluid intlet Temperature
+mc = 1 ;//[kg/s] Cold Fluid flow rate
+mh = 1.5 ; //[kg/s] Hot Fluid flow rate
+Uh = 100 ;//[W/m^2.K] Coefficient of heat transfer
+Ah = 40 ; //[m^2] Area
+//Table A.5 Water Properties T = 353 K
+cph = 1000 ; //[J/kg.K] Specific Heat
+//Table A.6 Saturated water Liquid Properties Tc = 308 K
+cpc = 4197 ; //[J/kg.K] Specific Heat
+
+Cc = mc*cpc;
+Ch = mh*cph;
+Cmin = Ch;
+Cmax = Cc;
+
+NTU = Uh*Ah/Cmin;
+ratio = Cmin/Cmax;
+
+printf("\n As Ratio Cmin/Cmax = %.2f and Number of transfer units NTU = %.2f, It follows from figure 11.14 that e = .82",ratio,NTU);
+e = 0.82;
+qmax = Cmin*(Thi-Tci);
+q = e*qmax;
+
+//Equation 11.6b
+Tco = q/(mc*cpc) + Tci;
+//Equation 11.7b
+Tho = -q/(mh*cph) + Thi;
+printf("\n Heat Transfer Rate = %.2e W \n Fluid Outlet Temperatures Hot Fluid (Tho) = %.1f degC Cold Fluid (Tco) = %.1f degC",q,Tho-273,Tco-273);
+//END
\ No newline at end of file diff --git a/534/CH11/EX11.5/11_5_Shell_n_Tube_HeatX.sce b/534/CH11/EX11.5/11_5_Shell_n_Tube_HeatX.sce new file mode 100644 index 000000000..3faf9cf71 --- /dev/null +++ b/534/CH11/EX11.5/11_5_Shell_n_Tube_HeatX.sce @@ -0,0 +1,39 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 11.5 Page 696 \n'); //Example 11.5
+// Outlet Temperature of cooling Water
+// Tube length per pass to achieve required heat transfer
+
+//Operating Conditions
+q = 2*10^9 ;//[W] Heat transfer Rate
+ho = 11000 ;//[W/m^2.K] Coefficient of heat transfer for outer surface
+Thi = 50+273 ;//[K] Hot Fluid Condensing Temperature
+Tho = Thi ;//[K] Hot Fluid Condensing Temperature
+Tci = 20+273 ;//[K] Cold Fluid intlet Temperature
+mc = 3*10^4 ; //[kg/s] Cold Fluid flow rate
+m = 1 ;//[kg/s] Cold Fluid flow rate per tube
+D = .025 ;//[m] diameter of tube
+//Table A.6 Saturated water Liquid Properties Tf = 300 K
+rho = 997 ; //[kg/m^3] Density
+cp = 4179 ; //[J/kg.K] Specific Heat
+k = 0.613 ; //[W/m.K] Conductivity
+u = 855*10^-6 ; //[N.s/m^2] Viscosity
+Pr = 5.83 ; // Prandtl number
+
+//Equation 11.6b
+Tco = q/(mc*cp) + Tci;
+
+Re = 4*m/(%pi*D*u);
+printf("\n As the Reynolds number of tube fluid is %i. Hence the flow is turbulent. Hence using Diettus-Boetllor Equation 8.60", Re);
+Nu = .023*Re^.8*Pr^.4;
+hi = Nu*k/D;
+U = 1/[1/ho + 1/hi];
+N = 30000 ;//No of tubes
+T1 = Thi-Tco;
+T2 = Tho-Tci;
+Tlm = (T1-T2)/(2.30*log10(T1/T2));
+L2 = q/(U*N*2*%pi*D*Tlm);
+
+
+printf("\n Outlet Temperature of cooling Water = %.1f degC\n Tube length per pass to achieve required heat transfer = %.2f m",Tco-273,L2);
+//END
\ No newline at end of file diff --git a/534/CH11/EX11.6/11_6_Finned_Compact_HeatX.sce b/534/CH11/EX11.6/11_6_Finned_Compact_HeatX.sce new file mode 100644 index 000000000..d6c7ba472 --- /dev/null +++ b/534/CH11/EX11.6/11_6_Finned_Compact_HeatX.sce @@ -0,0 +1,59 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 11.6 Page 702 \n'); //Example 11.6
+// Gas-side overall heat transfer coefficient. Heat exchanger Volume
+
+//Operating Conditions
+hc = 1500 ;//[W/m^2.K] Coefficient of heat transfer for outer surface
+hi = hc;
+Th = 825 ;//[K] Hot Fluid Temperature
+Tci = 290 ;//[K] Cold Fluid intlet Temperature
+Tco = 370 ;//[K] Cold Fluid outlet Temperature
+mc = 1 ;//[kg/s] Cold Fluid flow rate
+mh = 1.25 ;//[kg/s] Hot Fluid flow rate
+Ah = .20 ;//[m^2] Area of tubes
+Di = .0138 ;//[m] diameter of tube
+Do = .0164 ;//[m] Diameter
+//Table A.6 Saturated water Liquid Properties Tf = 330 K
+cpw = 4184 ; //[J/kg.K] Specific Heat
+//Table A.1 Aluminium Properties T = 300 K
+k = 237 ; //[W/m.K] Conductivity
+//Table A.4 Air Properties Tf = 700 K
+cpa = 1075 ; //[J/kg.K] Specific Heat
+u = 33.88*10^-6 ; //[N.s/m^2] Viscosity
+Pr = .695 ; // Prandtl number
+
+//Geometric Considerations
+si = .449;
+Dh = 6.68*10^-3 ;//[m] hydraulic diameter
+G = mh/si/Ah;
+Re = G*Dh/u;
+//From Figure 11.16
+jh = .01;
+hh = jh*G*cpa/Pr^.66667;
+
+AR = Di*2.303*log10(Do/Di)/(2*k*(.143));
+//Figure 11.16
+AcAh = Di/Do*(1-.830);
+//From figure 3.19
+nf = .89;
+noh = 1-(1-.89)*.83;
+
+U = [1/(hc*AcAh) + AR + 1/(noh*hh)]^-1;
+
+Cc = mc*cpw;
+q = Cc*(Tco-Tci);
+Ch = mh*cpa;
+qmax = Ch*(Th-Tci);
+e = q/qmax;
+ratio = Ch/Cc;
+
+printf("\n As effectiveness is %.2f with Ratio Cmin/Cmax = %.2f, It follows from figure 11.14 that NTU = .65",e,ratio);
+NTU = .65;
+A = NTU*Ch/U;
+//From Fig 11.16
+al = 269; //[m^-1] gas side area per unit heat wxchanger volume
+V = A/al;
+
+printf("\n Gas-side overall heat transfer coefficient.r = %i W/m^2.K\n Heat exchanger Volume = %.3f m^3",U,V);
+//END;
\ No newline at end of file diff --git a/534/CH12/EX12.1/12_1_Plate_surface.sce b/534/CH12/EX12.1/12_1_Plate_surface.sce new file mode 100644 index 000000000..953567f5f --- /dev/null +++ b/534/CH12/EX12.1/12_1_Plate_surface.sce @@ -0,0 +1,34 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.1 Page 731 \n')// Example 12.1
+
+// a) Intensity of emission in each of the three directions
+// b) Solid angles subtended by the three surfaces
+// c) Rate at which radiation is intercepted by the three surfaces
+
+A1 = .001 ;//[m^2] Area of emitter
+In = 7000 ;//[W/m^2.Sr] Intensity of radiation in normal direction
+A2 = .001 ;//[m^2] Area of other intercepting plates
+A3 = A2 ;//[m^2] Area of other intercepting plates
+A4 = A2 ;//[m^2] Area of other intercepting plates
+r = .5 ;//[m] Distance of each plate from emitter
+theta1 = 60 ;//[deg] Angle between surface 1 normal & direction of radiation to surface 2
+theta2 = 30 ;//[deg] Angle between surface 2 normal & direction of radiation to surface 1
+theta3 = 45 ;//[deg] Angle between surface 1 normal & direction of radiation to surface 4
+
+//From equation 12.2
+w31 = A3/r^2;
+w41 = w31;
+w21 = A2*cos(theta2*0.0174532925)/r^2;
+
+
+//From equation 12.6
+q12 = In*A1*cos(theta1*0.0174532925)*w21;
+q13 = In*A1*cos(0)*w31;
+q14 = In*A1*cos(theta3*0.0174532925)*w41;
+
+printf("\n (a) As Intensity of emitted radiation is independent of direction, for each of the three directions I = %i W/m^2.sr \n\n (b) By the Three Surfaces\n Solid angles subtended Rate at which radiation is intercepted \n w4-1 = %.2e sr q1-4 = %.1e W \n w3-1 = %.2e sr q1-3 = %.1e W\n w2-1 = %.2e sr q1-2 = %.1e W ",In,w41,q14,w31,q13,w21,q12);
+//END
+
+
+
diff --git a/534/CH12/EX12.10/12_10_Metallic_Sphere.sce b/534/CH12/EX12.10/12_10_Metallic_Sphere.sce new file mode 100644 index 000000000..101f8e4a5 --- /dev/null +++ b/534/CH12/EX12.10/12_10_Metallic_Sphere.sce @@ -0,0 +1,26 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.10 Page 768 \n')// Example 12.10
+
+// Total hemispherical absorptivity and emissivity of sphere for initial condition
+// values of absoprtivity and emissivity after sphere has been in furnace a long time
+
+Ts = 300; //[K] temperature of surface
+Tf = 1200; //[K] Temperature of Furnace
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+// From the given graph of absorptivities
+a1 = .8; //between wavelength 0 micro-m- 5 micro-m
+a2 = .1; //greater than wavelength 5 micro-m
+
+//From Table 12.1
+//For wl1 = 5 micro-m and T = 1200 K, At wl1*T = 6000 micro-m.K
+F0wl1 = 0.738;
+//From equation 12.44
+a = a1*F0wl1 + a2*(1-F0wl1);
+//From Table 12.1
+//For wl1 = 5 micro-m and T = 300 K, At wl1*T = 1500 micro-m.K
+F0wl1s = 0.014;
+//From equation 12.36
+e = a1*F0wl1s + a2*(1-F0wl1s);
+
+printf('\n For Initial Condition \n Total hemispherical absorptivity = %.2f Emissivity of sphere = %.2f \n\n Beacuase the spectral characteristics of the coating and the furnace temeprature remain fixed, there is no change in the value of absorptivity with increasing time. \n Hence, After a sufficiently long time, Ts = Tf = %i K and emissivity equals absorptivity e = a = %.2f',a,e,Tf,a);
\ No newline at end of file diff --git a/534/CH12/EX12.11/12_11_Solar_Collector.sce b/534/CH12/EX12.11/12_11_Solar_Collector.sce new file mode 100644 index 000000000..645ac0b7b --- /dev/null +++ b/534/CH12/EX12.11/12_11_Solar_Collector.sce @@ -0,0 +1,28 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.11 Page 774 \n')// Example 12.11
+
+// Useful heat removal rate per unit area
+// Efficiency of the collector
+
+Ts = 120+273; //[K] temperature of surface
+Gs = 750; //[W/m^2] Solar irradiation
+Tsky = -10+273; //[K] Temperature of Sky
+Tsurr = 30+273; //[K] Temperature os surrounding Air
+e = .1 ;// emissivity
+as = .95 ;// Absorptivity of Surface
+asky = e ;// Absorptivity of Sky
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+h = 0.22*(Ts - Tsurr)^.3334 ;//[W/m^2.K] Convective Heat transfer Coeff
+//From equation 12.67
+Gsky = stfncnstt*Tsky^4; //[W/m^2] Irradiadtion from sky
+qconv = h*(Ts-Tsurr); //[W/m^2] Convective Heat transfer
+E = e*stfncnstt*Ts^4; //[W/m^2] Irradiadtion from Surface
+
+//From energy Balance
+q = as*Gs + asky*Gsky - qconv - E;
+
+//Collector efficiency
+eff = q/Gs;
+
+printf('\n Useful heat removal rate per unit area by Energy Conservation = %i W/m^2 \n Collector efficiency defined as the fraction of solar irradiation extracted as useful energy is %.2f',q,eff);
\ No newline at end of file diff --git a/534/CH12/EX12.2/12_2_Spectral_Distribution.sce b/534/CH12/EX12.2/12_2_Spectral_Distribution.sce new file mode 100644 index 000000000..c39690689 --- /dev/null +++ b/534/CH12/EX12.2/12_2_Spectral_Distribution.sce @@ -0,0 +1,19 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.2 Page 734\n')// Example 12.2
+
+// Total Irradiation
+x=[0 5 20 25];
+y=[0 1000 1000 0];
+clf();
+plot2d(x,y,style=5,rect=[0,0,30,1100]);
+xtitle("Spectral Distribution", "wavelength (micro-m)", "G (W/m^2.micro-m)");
+
+//By Equation 12.4
+G = 1000*(5-0)/2+1000*(20-5)+1000*(25-20)/2;
+
+printf("\n G = %i W/m^2",G);
+//END
+
+
+
diff --git a/534/CH12/EX12.3/12_3_Blackbody_Radiation.sce b/534/CH12/EX12.3/12_3_Blackbody_Radiation.sce new file mode 100644 index 000000000..7c8c97943 --- /dev/null +++ b/534/CH12/EX12.3/12_3_Blackbody_Radiation.sce @@ -0,0 +1,34 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.3 Page 741 \n')// Example 12.3
+
+// Spectral Emissive Power of a small aperture on the enclosure
+// wavelengths below which and above which 10% of the radiation is concentrated
+// Spectral emissive power and wavelength associated with maximum emission
+// Irradiation on a small object inside the enclosure
+
+T = 2000 ;//[K] temperature of surface
+stfncnstt = 5.67*10^-8 ;//[W/m^2.K^4] Stefan-Boltzmann constant
+E = stfncnstt*T^4; //[W/m^2]
+
+//From Table 12.1
+constt1 = 2195 ; //[micro-m.K]
+wl1 = constt1/T;
+//From Table 12.1
+constt2 = 9382 ; //[micro-m.K]
+wl2 = constt2/T;
+
+//From Weins Law, wlmax*T = consttmax = 2898 micro-m.K
+consttmax = 2898 ;//micro-m.K
+wlmax = consttmax/T;
+//from Table 12.1 at wlmax = 1.45 micro-m.K and T = 2000 K
+I = .722*10^-4*stfncnstt*T^5;
+Eb = %pi*I;
+
+G = E; //[W/m^2] Irradiation of any small object inside the enclosure is equal to emission from blackbody at enclosure temperature
+
+printf("\n (a) Spectral Emissive Power of a small aperture on the enclosure = %.2e W/m^2.Sr for each of the three directions \n (b) Wavelength below which 10percent of the radiation is concentrated = %.1f micro-m \n Wavelength above which 10percent of the radiation is concentrated = %.2f micro-m \n (c) Spectral emissive power and wavelength associated with maximum emission is %.2e micro-m and %.2e W/m^2.micro-m respectively \n (d) Irradiation on a small object inside the enclosure = %.2e W/m^2",E,wl1,wl2,Eb,wlmax,G);
+//END
+
+
+
diff --git a/534/CH12/EX12.4/12_4_Blackbody_Angular_Radiation.sce b/534/CH12/EX12.4/12_4_Blackbody_Angular_Radiation.sce new file mode 100644 index 000000000..6015f17bc --- /dev/null +++ b/534/CH12/EX12.4/12_4_Blackbody_Angular_Radiation.sce @@ -0,0 +1,26 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.4 Page 743 \n')// Example 12.4
+
+// Rate of emission per unit area over all directions between 0 degC and 60 degC and over all wavelengths between wavelengths 2 and 4 micro-m
+
+T = 1500 ;//[K] temperature of surface
+stfncnstt = 5.67*10^-8 ;//[W/m^2.K^4] Stefan-Boltzmann constant
+
+//From Equation 12.26 Black Body Radiation
+Eb = stfncnstt*T^4; //[W/m^2]
+
+//From Table 12.1 as wl1*T = 2*1500 (micro-m.K)
+F02 = .273;
+//From Table 12.1 as wl2*T = 4*1500 (micro-m.K)
+F04 = .738;
+
+//From equation 12.10 and 12.11
+i1 = integrate('2*cos(x)*sin(x)','x',0,%pi/3);
+delE = i1*(F04-F02)*Eb;
+
+printf("\n Rate of emission per unit area over all directions between 0 degC and 60 degC and over all wavelengths between wavelengths 2 micro-m and 4 micro-m = %.1e W/m^2",delE);
+//END
+
+
+
diff --git a/534/CH12/EX12.5/12_5_Diffuse_emitter.sce b/534/CH12/EX12.5/12_5_Diffuse_emitter.sce new file mode 100644 index 000000000..8d2f40319 --- /dev/null +++ b/534/CH12/EX12.5/12_5_Diffuse_emitter.sce @@ -0,0 +1,45 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.5 Page 748 \n')// Example 12.5
+
+// Total hemispherical emissivity
+// Total emissive Power
+// Wavelength at which spectral emissive power will be maximum
+
+T = 1600 ;//[K] temperature of surface
+wl1 = 2 ;//[micro-m] wavelength 1
+wl2 = 5 ;//[micro-m] wavelength 2
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+// From the given graph of emissivities
+e1 = .4;
+e2 = .8;
+//From Equation 12.26 Black Body Radiation
+Eb = stfncnstt*T^4; //[W/m^2]
+
+//Solution (A)
+//From Table 12.1 as wl1*T = 2*1600 (micro-m.K)
+F02 = .318;
+//From Table 12.1 as wl2*T = 5*1600 (micro-m.K)
+F05 = .856;
+//From Equation 12.36
+e = e1*F02 + e2*[F05 - F02];
+
+//Solution (B)
+//From equation 12.35
+E = e*Eb;
+
+//Solution (C)
+//For maximum condition Using Weins Law
+consttmax = 2898 ;//[micro-m.K]
+wlmax = consttmax/T;
+
+//equation 12.32 with Table 12.1
+E1 = %pi*e1*.722*10^-4*stfncnstt*T^5;
+
+E2 = %pi*e2*.706*10^-4*stfncnstt*T^5;
+
+printf("\n (a) Total hemispherical emissivity = %.3f \n (b) Total emissive Power = %i kW/m^2 \n (c) Emissive Power at wavelength 2micro-m is greater than Emissive power at maximum wavelength \n i.e. %.1f kW/m^2 > %.1f kW/m^2 \n Thus, Peak emission occurs at %i micro-m",e,E/1000,E2/1000,E1/1000,wl1);
+//END
+
+
+
diff --git a/534/CH12/EX12.6/12_6_Metallic_surface.sce b/534/CH12/EX12.6/12_6_Metallic_surface.sce new file mode 100644 index 000000000..2a4c4b7f7 --- /dev/null +++ b/534/CH12/EX12.6/12_6_Metallic_surface.sce @@ -0,0 +1,32 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.6 Page 751 \n')// Example 12.6
+
+// Spectral , Normal emissivity en and spectral hemispherical emissivity e
+// Spectral normal intensity In and Spectral emissive power
+
+T = 2000 ;//[K] temperature of surface
+wl = 1 ;//[micro-m] wavelength
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+
+// From the given graph of emissivities
+e1 = .3;
+e2 = .6;
+//From Equation 12.26 Black Body Radiation
+Eb = stfncnstt*T^4; //[W/m^2]
+
+//Equation 12.34
+i1 = integrate('e1*cos(x)*sin(x)','x',0,%pi/3);
+i2 = integrate('e2*cos(x)*sin(x)','x',%pi/3,4*%pi/9);
+e = 2*[i1+i2];
+
+// From Table 12.1 at wl = 1 micro-m and T = 2000 K.
+
+I = .493*10^-4 * stfncnstt*T^5 ;//[W/m^2.micro-m.sr]
+
+In = e1*I;
+
+//Using Equation 12.32 for wl = 1 micro-m and T = 2000 K
+E = e*%pi*I;
+
+printf('\n Spectral Normal emissivity en = %.1f and spectral hemispherical emissivity e = %.2f \n Spectral normal intensity In = %.2e W/m^2.micro-m.sr and Spectral emissive power = %.1e W/m^2.micro-m.sr ', e1, e,In,E);
\ No newline at end of file diff --git a/534/CH12/EX12.7/12_7_Opaque_surface.sce b/534/CH12/EX12.7/12_7_Opaque_surface.sce new file mode 100644 index 000000000..941a2e172 --- /dev/null +++ b/534/CH12/EX12.7/12_7_Opaque_surface.sce @@ -0,0 +1,29 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.7 Page 759 \n')// Example 12.7
+
+// Spectral distribution of reflectivity
+// Total, hemispherical absorptivity
+// Nature of surface temperature change
+
+T = 500 ;//[K] temperature of surface
+e = .8;
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+
+x=[0 6 8 16];
+y=[.8 .8 0 0];
+clf();
+plot2d(x,y,style=5,rect=[0,0,20,1]);
+
+
+xtitle("Spectral Distribution of reflectivity", "wavelength (micro-m)", "reflectivity");
+
+//From equation 12.43 and 12.44
+Gabs = {.2*500/2*(6-2)+500*[.2*(8-6)+(1-.2)*(8-6)/2]+1*500*(12-8)+500*(16-12)/2} ;//[w/m^2]
+G = {500*(6-2)/2+500*(12-6)+500*(16-12)/2} ;//[w/m^2]
+a = Gabs/G;
+
+//Neglecting convection effects net het flux to the surface
+qnet = a*G - e*stfncnstt*T^4;
+
+printf('\n Total, hemispherical absorptivity %.2f \n Nature of surface temperature change = %i W/m^2 \n Since qnet > 0, the sirface temperature will increase with the time', a,qnet);
\ No newline at end of file diff --git a/534/CH12/EX12.8/12_8_Glass_Cover.sce b/534/CH12/EX12.8/12_8_Glass_Cover.sce new file mode 100644 index 000000000..c723347b9 --- /dev/null +++ b/534/CH12/EX12.8/12_8_Glass_Cover.sce @@ -0,0 +1,20 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.8 Page 761 \n')// Example 12.8
+
+// Total emissivity of cover glass to solar radiation
+
+T = 5800 ;//[K] temperature of surface
+e = .8;
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+
+//From Table 12.1
+//For wl1 = .3 micro-m and T = 5800 K, At wl1*T = 1740 micro-m.K
+F0wl1 = .0335;
+//For wl1 = .3 micro-m and T = 5800 K, At wl2*T = 14500 micro-m.K
+F0wl2 = .9664;
+
+//Hence from equation 12.29
+t = .90*[F0wl2 - F0wl1];
+
+printf('\n Total emissivity of cover glass to solar radiation = %.2f',t);
\ No newline at end of file diff --git a/534/CH12/EX12.9/12_9_Brick_Wall.sce b/534/CH12/EX12.9/12_9_Brick_Wall.sce new file mode 100644 index 000000000..55c598a70 --- /dev/null +++ b/534/CH12/EX12.9/12_9_Brick_Wall.sce @@ -0,0 +1,35 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 12.9 Page 766 \n')// Example 12.9
+
+// Total hemispherical emissivity of fire brick wall
+// Total emissive power of brick wall
+// Absorptivity of the wall to irradiation from coals
+
+Ts = 500 ;//[K] temperature of brick surface
+Tc = 2000 ;//[K] Temperature of coal exposed
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+// From the given graph of emissivities
+e1 = .1; //between wavelength 0 micro-m- 1.5 micro-m
+e2 = .5; //between wavelength 1.5 micro-m- 10 micro-m
+e3 = .8; //greater than wavelength 10 micro-m
+
+//From Table 12.1
+//For wl1 = 1.5 micro-m and T = 500 K, At wl1*T = 750 micro-m.K
+F0wl1 = 0;
+//For wl2 = 10 micro-m and T = 500 K, At wl2*T = 5000 micro-m.K
+F0wl2 = .634;
+//From equation 12.36
+e = e1*F0wl1 + e2*F0wl2 + e3*(1-F0wl1-F0wl2);
+
+//Equation 12.26 and 12.35
+E = e*stfncnstt*Ts^4;
+
+//From Table 12.1
+//For wl1 = 1.5 micro-m and T = 2000 K, At wl1*T = 3000 micro-m.K
+F0wl1c = 0.273;
+//For wl2 = 10 micro-m and T = 2000 K, At wl2*T = 20000 micro-m.K
+F0wl2c = .986;
+ac = e1*F0wl1c + e2*[F0wl2c-F0wl1c] + e3*(1-F0wl2c);
+
+printf('\n Total hemispherical emissivity of fire brick wall = %.3f \n Total emissive power of brick wall = %i W/m^2.\n Absorptivity of the wall to irradiation from coals = %.3f',e,E,ac);
\ No newline at end of file diff --git a/534/CH13/EX13.1/13_1_Theoretical_Problem.sce b/534/CH13/EX13.1/13_1_Theoretical_Problem.sce new file mode 100644 index 000000000..e39b18582 --- /dev/null +++ b/534/CH13/EX13.1/13_1_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.1 Page 820 \n')// Example 13.1
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH13/EX13.2/13_2_View_Factor_Geometries.sce b/534/CH13/EX13.2/13_2_View_Factor_Geometries.sce new file mode 100644 index 000000000..dcc25225a --- /dev/null +++ b/534/CH13/EX13.2/13_2_View_Factor_Geometries.sce @@ -0,0 +1,24 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.2 Page 821 \n')// Example 13.2
+
+// View Factors of known surface Geometries
+
+// (1) Sphere within Cube
+F12a = 1 ;//By Inspection
+F21a = (%pi/6)*F12a ; //By Reciprocity
+
+// (2) Partition within a Square Duct
+F11b = 0 ;//By Inspection
+//By Symmetry F12 = F13
+F12b = (1-F11b)/2 ; //By Summation Rule
+F21b = sqrt(2)*F12b ; //By Reciprocity
+
+// (3) Circular Tube
+//From Table 13.2 or 13.5, with r3/L = 0.5 and L/r1 = 2
+F13c = .172;
+F11c = 0; //By Inspection
+F12c = 1 - F11c - F13c ;//By Summation Rule
+F21c = F12c/4 ;//By Reciprocity
+
+printf('\n Desired View Factors may be obtained from inspection, the reciprocity rule, the summation rule and/or use of charts \n (1) Sphere within Cube F21 = %.3f \n (2) Partition within a Square Duct F21 = %.3f \n (3) Circular Tube F21 = %.3f',F21a,F21b,F21c);
\ No newline at end of file diff --git a/534/CH13/EX13.3/13_3_Curved_Surface.sce b/534/CH13/EX13.3/13_3_Curved_Surface.sce new file mode 100644 index 000000000..aa34769e3 --- /dev/null +++ b/534/CH13/EX13.3/13_3_Curved_Surface.sce @@ -0,0 +1,43 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.3 Page 826 \n')// Example 13.3
+
+// Net rate of Heat transfer to the absorber surface
+
+L = 10 ;//[m] Collector length = Heater Length
+T2 = 600 ;//[K] Temperature of curved surface
+A2 = 15 ;//[m^2] Area of curved surface
+e2 = .5 ;// emissivity of curved surface
+stfncnstt = 5.67*10^-8; //[W/m^2.K^4] Stefan-Boltzmann constant
+T1 = 1000 ;//[K] Temperature of heater
+A1 = 10 ;//[m^2] area of heater
+e1 = .9 ;// emissivity of heater
+W = 1 ;//[m] Width of heater
+H = 1 ;//[m] Height
+T3 = 300 ;//[K] Temperature of surrounding
+e3 = 1 ;// emissivity of surrounding
+
+J3 = stfncnstt*T3^4; //[W/m^2]
+//From Figure 13.4 or Table 13.2, with Y/L = 10 and X/L =1
+F12 = .39;
+F13 = 1 - F12; //By Summation Rule
+//For a hypothetical surface A2h
+A2h = L*W;
+F2h3 = F13; //By Symmetry
+F23 = A2h/A2*F13; //By reciprocity
+Eb1 = stfncnstt*T1^4; //[W/m^2]
+Eb2 = stfncnstt*T2^4; //[W/m^2]
+//Radiation network analysis at Node corresponding 1
+//-10J1 + 0.39J2 = -510582
+//.26J1 - 1.67J2 = -7536
+//Solving above equations
+A = [-10 .39;
+ .26 -1.67];
+B = [-510582;
+ -7536];
+
+X = inv(A)*B;
+
+q2 = (Eb2 - X(2))/(1-e2)*(e2*A2);
+
+printf('\n Net Heat transfer rate to the absorber is = %.1f kW',q2/1000);
\ No newline at end of file diff --git a/534/CH13/EX13.4/13_4_Cylindrical_Furnace.sce b/534/CH13/EX13.4/13_4_Cylindrical_Furnace.sce new file mode 100644 index 000000000..a30032052 --- /dev/null +++ b/534/CH13/EX13.4/13_4_Cylindrical_Furnace.sce @@ -0,0 +1,23 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.4 Page 830 \n')// Example 13.4
+
+// Power required to maintain prescribed temperatures
+
+T3 = 300 ;//[K] Temperature of surrounding
+L = .15 ;//[m] Furnace Length
+T2 = 1650+273 ;//[K] Temperature of bottom surface
+T1 = 1350+273 ;//[K] Temperature of sides of furnace
+D = .075 ;//[m] Diameter of furnace
+stfncnstt = 5.670*10^-8; //[W/m^2.K^4] Stefan Boltzman Constant
+A2 = %pi*D^2/4 ;//[m] Area of bottom surface
+A1 = %pi*D*L ;//[m] Area of curved sides
+//From Figure 13.5 or Table 13.2, with ri/L = .25
+F23 = .056;
+F21 = 1 - F23; //By Summation Rule
+F12 = A2/A1*F21; //By reciprocity
+F13 = F12 ;//By Symmetry
+//From Equation 13.17 Heat balance
+q = A1*F13*stfncnstt*(T1^4 - T3^4) + A2*F23*stfncnstt*(T2^4 - T3^4);
+
+printf('\n Power required to maintain prescribed temperatures is = %i W',q);
\ No newline at end of file diff --git a/534/CH13/EX13.5/13_5_Concentric_Tube_Arrangement.sce b/534/CH13/EX13.5/13_5_Concentric_Tube_Arrangement.sce new file mode 100644 index 000000000..c198ebab9 --- /dev/null +++ b/534/CH13/EX13.5/13_5_Concentric_Tube_Arrangement.sce @@ -0,0 +1,24 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.5 Page 834 \n')// Example 13.5
+
+// Heat gain by the fluid passing through the inner tube
+// Percentage change in heat gain with radiation shield inserted midway between inner and outer tubes
+
+T2 = 300 ;//[K] Temperature of inner surface
+D2 = .05 ;//[m] Diameter of Inner Surface
+e2 = .05 ;// emissivity of Inner Surface
+T1 = 77 ;//[K] Temperature of Outer Surface
+D1 = .02 ;//[m] Diameter of Inner Surface
+e1 = .02 ;// emissivity of Outer Surface
+D3 = .035 ;//[m] Diameter of Shield
+e3 = .02 ;// emissivity of Shield
+stfncnstt = 5.670*10^-8 ;//[W/m^2.K^4] Stefan Boltzman Constant
+
+//From Equation 13.20 Heat balance
+q = stfncnstt*(%pi*D1)*(T1^4-T2^4)/(1/e1 + (1-e2)/e2*D1/D2) ;//[W/m]
+
+RtotL = (1-e1)/(e1*%pi*D1) + 1/(%pi*D1*1) + 2*[(1-e3)/(e3*%pi*D3)] + 1/(%pi*D3*1) + (1-e2)/(e2*%pi*D2) ;//[m^-2]
+q2 = stfncnstt*(T1^4 - T2^4)/RtotL; //[W/m]
+
+printf('\n Heat gain by the fluid passing through the inner tube = %.2f W/m \n Percentage change in heat gain with radiation shield inserted midway between inner and outer tubes is = %.2f percent',q,(q2-q)*100/q);
\ No newline at end of file diff --git a/534/CH13/EX13.6/13_6_Triangular_Baking_Duct.sce b/534/CH13/EX13.6/13_6_Triangular_Baking_Duct.sce new file mode 100644 index 000000000..6f6aafc18 --- /dev/null +++ b/534/CH13/EX13.6/13_6_Triangular_Baking_Duct.sce @@ -0,0 +1,31 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.6 Page 836 \n')// Example 13.6
+
+// Rate at which heat must be supplied per unit length of duct
+// Temperature of the insulated surface
+
+T2 = 500 ;//[K] Temperature of Painted surface
+e2 = .4 ;// emissivity of Painted Surface
+T1 = 1200 ;//[K] Temperature of Heated Surface
+W = 1 ; //[m] Width of Painted Surface
+e1 = .8 ;// emissivity of Heated Surface
+er = .8 ;// emissivity of Insulated Surface
+stfncnstt = 5.670*10^-8 ;//[W/m^2.K^4] Stefan Boltzman Constant
+
+//By Symmetry Rule
+F2R = .5;
+F12 = .5;
+F1R = .5;
+
+//From Equation 13.20 Heat balance
+q = stfncnstt*(T1^4-T2^4)/((1-e1)/e1*W+ 1/(W*F12+[(1/W/F1R) + (1/W/F2R)]^-1) + (1-e2)/e2*W) ;//[W/m]
+
+//Surface Energy Balance 13.13
+J1 = stfncnstt*T1^4 - (1-e1)*q/(e1*W) ;// [W/m^2] Surface 1
+J2 = stfncnstt*T2^4 - (1-e2)*(-q)/(e2*W) ;// [W/m^2] Surface 2
+//From Equation 13.26 Heat balance
+JR = (J1+J2)/2;
+TR = (JR/stfncnstt)^.25;
+
+printf('\n Rate at which heat must be supplied per unit length of duct = %.2f kW/m \n Temperature of the insulated surface = %i K',q/1000,TR);
\ No newline at end of file diff --git a/534/CH13/EX13.7/13_7_Semicircular_Tube.sce b/534/CH13/EX13.7/13_7_Semicircular_Tube.sce new file mode 100644 index 000000000..1270d9011 --- /dev/null +++ b/534/CH13/EX13.7/13_7_Semicircular_Tube.sce @@ -0,0 +1,51 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 13.7 Page 841 \n')// Example 13.7
+
+// Rate at which heat must be supplied
+// Temperature of the insulated surface
+
+T1 = 1000 ;//[K] Temperature of Heated Surface
+e1 = .8 ;// emissivity of Heated Surface
+e2 = .8 ; // emissivity of Insulated Surface
+r = .02 ;//[m] Radius of surface
+Tm = 400 ;//[K] Temperature of surrounding air
+m = .01 ;//[kg/s] Flow rate of surrounding air
+p = 101325 ;//[Pa] Pressure of surrounding air
+stfncnstt = 5.670*10^-8 ;//[W/m^2.K^4] Stefan Boltzman Constant
+//Table A.4 Air Properties at 1 atm, 400 K
+k = .0338 ;//[W/m.K] conductivity
+u = 230*10^-7 ;//[kg/s.m] Viscosity
+cp = 1014 ;//[J/kg] Specific heat
+Pr = .69 ;// Prandtl Number
+
+//Hydraulic Diameter
+Dh = 2*%pi*r/(%pi+2) ;//[m]
+//Reynolds number
+Re = m*Dh/(%pi*r^2/2)/u;
+//View Factor
+F12 = 1 ;
+
+printf("\n As Reynolds Number is %i, Hence it is Turbulent flow inside a cylinder. Hence we will use Dittus-Boelter Equation",Re);
+
+//From Dittus-Boelter Equation
+Nu = .023*Re^.8*Pr^.4;
+h = Nu*k/Dh; //[W/m^2.K]
+
+//From Equation 13.18 Heat Energy balance
+//Newton Raphson
+T2=600; //Initial Assumption
+while(1>0)
+f=(stfncnstt*(T1^4 - T2^4)/((1-e1)/(e1*2*r)+1/(2*r*F12)+(1-e2)/(e2*%pi*r)) - h*%pi*r*(T2-Tm));
+fd=(4*stfncnstt*( - T2^3)/((1-e1)/(e1*2*r)+1/(2*r*F12)+(1-e2)/(e2*%pi*r)) - h*%pi*r*(T2));
+T2n=T2-f/fd;
+if(stfncnstt*(T1^4 - T2n^4)/((1-e1)/(e1*2*r)+1/(2*r*F12)+(1-e2)/(e2*%pi*r)) - h*%pi*r*(T2n-Tm))<=.01
+ break;
+end;
+T2=T2n;
+end
+
+//From energy Balance
+q = h*%pi*r*(T2-Tm) + h*2*r*(T1-Tm) ;//[W/m]
+
+printf('\n Rate at which heat must be supplied per unit length of duct = %.2f W/m & Temperature of the insulated surface = %i K',q,T2);
\ No newline at end of file diff --git a/534/CH14/EX14.1/14_1_Diffusion_mass_transfer_Hydrogen.sce b/534/CH14/EX14.1/14_1_Diffusion_mass_transfer_Hydrogen.sce new file mode 100644 index 000000000..00496de66 --- /dev/null +++ b/534/CH14/EX14.1/14_1_Diffusion_mass_transfer_Hydrogen.sce @@ -0,0 +1,44 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.1 Page 884 \n')// Example 14.1
+
+// Molar and mass fluxes of hydrogen and the relative values of the mass and thermal diffusivities for the three cases
+
+T = 293 ;//[K] Temperature
+Ma = 2 ;//[kg/kmol] Molecular Mass
+//Table A.8 Hydrogen-Air Properties at 298 K
+Dab1 = .41*10^-4; //[m^2/s] diffusion coefficient
+//Table A.8 Hydrogen-Water Properties at 298 K
+Dab2 = .63*10^-8; //[m^2/s] diffusion coefficient
+//Table A.8 Hydrogen-iron Properties at 293 K
+Dab3 = .26*10^-12; //[m^2/s] diffusion coefficient
+//Table A.4 Air properties at 293 K
+a1 = 21.6*10^-6; //[m^2/s] Thermal Diffusivity
+//Table A.6 Water properties at 293 K
+k = .603 ;//[W/m.K] conductivity
+rho = 998 ;//[kg/m^3] Density
+cp = 4182 ;//[J/kg] specific Heat
+//Table A.1 Iron Properties at 300 K
+a3 = 23.1 * 10^-6; //[m^2/s]
+
+//Equation 14.14
+//Hydrogen-air Mixture
+DabT1 = Dab1*(T/298)^1.5; // [m^2/s] mass diffusivity
+J1 = -DabT1*1; //[kmol/s.m^2] Total molar concentration
+j1 = Ma*J1; //[kg/s.m^2] mass Flux of Hydrogen
+Le1 = a1/DabT1; // Lewis Number Equation 6.50
+
+//Hydrogen-water Mixture
+DabT2 = Dab2*(T/298)^1.5; // [m^2/s] mass diffusivity
+a2 = k/(rho*cp) ;//[m^2/s] thermal diffusivity
+J2 = -DabT2*1 ;//[kmol/s.m^2] Total molar concentration
+j2 = Ma*J2 ;//[kg/s.m^2] mass Flux of Hydrogen
+Le2 = a2/DabT2 ;// Lewis Number Equation 6.50
+
+//Hydrogen-iron Mixture
+DabT3 = Dab3*(T/298)^1.5; // [m^2/s] mass diffusivity
+J3 = -DabT3*1; //[kmol/s.m^2] Total molar concentration
+j3 = Ma*J3; //[kg/s.m^2] mass Flux of Hydrogen
+Le3 = a3/DabT3 ;// Lewis Number Equation 6.50
+
+printf('\n Species a (m^2/s) Dab (m^2/s) Le ja (kg/s.m^2) \n Air %.1e %.1e %.2f %.1e \n Water %.1e %.1e %i %.1e \n Iron %.1e %.1e %.1e %.1e',a1,DabT1,Le1,j1,a2,DabT2,Le2,j2,a3,DabT3,Le3,j3);
\ No newline at end of file diff --git a/534/CH14/EX14.2/14_2_Diffusion_mass_transfer_Water_droplet.sce b/534/CH14/EX14.2/14_2_Diffusion_mass_transfer_Water_droplet.sce new file mode 100644 index 000000000..8d01d3d77 --- /dev/null +++ b/534/CH14/EX14.2/14_2_Diffusion_mass_transfer_Water_droplet.sce @@ -0,0 +1,38 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.2 Page 898 \n')// Example 14.2
+
+// Evaporation rate through a single pore
+
+T = 298 ;//[K] Temperature
+D = 10*10^-6 ;//[m]
+L = 100*10^-6; //[m]
+H = .5 ;// Moist Air Humidity
+p = 1.01325 ;//[bar]
+//Table A.6 Saturated Water vapor Properties at 298 K
+psat = .03165; //[bar] saturated Pressure
+//Table A.8 Water vapor-air Properties at 298 K
+Dab = .26*10^-4; //[m^2/s] diffusion coefficient
+
+C = p/(8.314*10^-2*298) ;//Total Concentration
+//From section 6.7.2, the mole fraction at x = 0 is
+xa0 = psat/p;
+//the mole fraction at x = L is
+xaL = H*psat/p;
+
+//Evaporation rate per pore Using Equation 14.41 with advection
+N = (%pi*D^2)*C*Dab/(4*L)*2.303*log10((1-xaL)/(1-xa0)) ;//[kmol/s]
+
+//Neglecting effects of molar averaged velocity Equation 14.32
+//Species transfer rate per pore
+Nh = (%pi*D^2)*C*Dab/(4*L)*(xa0-xaL) ;//[kmol/s]
+
+printf('\n Evaporation rate per pore Without advection effects %.2e kmol/s and With Advection effects %.2e kmol/s',Nh,N)
+
+clf();
+x = linspace(300,800,100);
+y1 = N*x^1.5/298^1.5*10^15;
+y2 = Nh*x^1.5/298^1.5*10^15;
+plot(x,y1,x,y2);
+xtitle("Evaporation Temp vs Temp", "T (K)", "Na *10^15(kmol/s)");
+legend ("Without Advection", "With Advection");
\ No newline at end of file diff --git a/534/CH14/EX14.3/14_3_Polymer_Sheet_and_Trough_geometry.sce b/534/CH14/EX14.3/14_3_Polymer_Sheet_and_Trough_geometry.sce new file mode 100644 index 000000000..5e1161a41 --- /dev/null +++ b/534/CH14/EX14.3/14_3_Polymer_Sheet_and_Trough_geometry.sce @@ -0,0 +1,18 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.3 Page 898 \n')// Example 14.3
+
+// Rate of water vapor molar diffusive ttansfer through the trough wall
+
+D = .005 ;//[m] Diameter
+L = 50*10^-6; //[m] Length
+h = .003 ;//[m] Depth
+Dab = 6*10^-14 ;//[m^2/s] Diffusion coefficient
+Cas1 = 4.5*10^-3 ;//[kmol/m^3] Molar concentrations of water vapor at outer surface
+Cas2 = 0.5*10^-3 ;//[kmol/m^3] Molar concentrations of water vapor at inner surface
+
+//Transfer Rate through cylindrical wall Equation 14.54
+Na = Dab/L*(%pi*D^2/4 + %pi*D*h)*(Cas1-Cas2); //[kmol/s]
+
+printf('\n Rate of water vapor molar diffusive ttansfer through the trough wall %.2e kmol/s',Na);
+//END
\ No newline at end of file diff --git a/534/CH14/EX14.4/14_4_Helium_Gas_spherical_container.sce b/534/CH14/EX14.4/14_4_Helium_Gas_spherical_container.sce new file mode 100644 index 000000000..46db4f06d --- /dev/null +++ b/534/CH14/EX14.4/14_4_Helium_Gas_spherical_container.sce @@ -0,0 +1,20 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.4 Page 902 \n')// Example 14.4
+
+// The rate of change of the helium pressure dp/dt
+
+D = .2 ;//[m] Diameter
+L = 2*10^-3 ;//[m] Thickness
+p = 4 ;//[bars] Helium Pressure
+T = 20+273 ;//[K] Temperature
+//Table A.8 helium-fused silica (293K) Page 952
+Dab = .4*10^-13 ;//[m^2/s] Diffusion coefficient
+//Table A.10 helium-fused silica (293K)
+S = .45*10^-3 ;//[kmol/m^3.bar] Solubility
+
+// By applying the species conservation Equation 14.43 and 14.62
+dpt = -6*(.08314)*T*(Dab)*S*p/(L*D);
+
+printf('\n The rate of change of the helium pressure dp/dt %.2e bar/s',dpt);
+//END
\ No newline at end of file diff --git a/534/CH14/EX14.5/14_5_Hydrogen_plastic_diffusion.sce b/534/CH14/EX14.5/14_5_Hydrogen_plastic_diffusion.sce new file mode 100644 index 000000000..620f6325c --- /dev/null +++ b/534/CH14/EX14.5/14_5_Hydrogen_plastic_diffusion.sce @@ -0,0 +1,23 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.5 Page 904 \n')// Example 14.5
+
+// The Hydrogen mass diffusive flux nA (kg/s.m^2)
+//A -> Hydrogen
+//B -> Plastic
+
+Dab = 8.7*10^-8 ;//[m^2/s] Diffusion coefficient
+Sab = 1.5*10^-3 ;//[kmol/m^3.bar] Solubility
+L = .0003 ;//[m] thickness of bar
+p1 = 3 ;//[bar] pressure on one side
+p2 = 1 ;//[bar] pressure on other side
+Ma = 2 ;//[kg/mol] molecular mass of Hydrogen
+//Surface molar concentrations of hydrogen from Equation 14.62
+Ca1 = Sab*p1 ; //[kmol/m^3]
+Ca2 = Sab*p2 ; //[kmol/m^3]
+//From equation 14.42 to 14.53 for obtaining mass flux
+N = Dab/L*(Ca1-Ca2) ; //[kmol/s.m^2]
+n = Ma*N ; //[kg/s.m^2] on Mass basis
+
+printf('\n The Hydrogen mass diffusive flux n = %.2e (kg/s.m^2)',n);
+//END
\ No newline at end of file diff --git a/534/CH14/EX14.6/14_6_Bacteria_Biofilm.sce b/534/CH14/EX14.6/14_6_Bacteria_Biofilm.sce new file mode 100644 index 000000000..92b514f05 --- /dev/null +++ b/534/CH14/EX14.6/14_6_Bacteria_Biofilm.sce @@ -0,0 +1,17 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.6 Page 909 \n')// Example 14.6
+
+// Maximum Thickness of a bacteria laden biofilm, that may be siccessfully treated
+
+Dab = 2*10^-12 ;//[m^2/s] Diffusion coefficient
+Ca0 = 4*10^-3 ;//[kmol/m^3] Fixed Concentration of medication
+Na = -.2*10^-3 ;//[kmol/m^3.s] Minimum consumption rate of antibiotic
+k1 = .1 ;//[s^-1] Reaction Coefficient
+
+//For firsst order kinetic reaction Equation 14.74
+m = (k1/Dab)^.5;
+L = m^-1*acosh(-k1*Ca0/Na);
+
+printf('\n Maximum Thickness of a bacteria laden biofilm, that may be siccessfully treated is %.1f pico-m',L*10^6);
+//END
\ No newline at end of file diff --git a/534/CH14/EX14.7/14_7_Drug_Medication.sce b/534/CH14/EX14.7/14_7_Drug_Medication.sce new file mode 100644 index 000000000..150f3e3d5 --- /dev/null +++ b/534/CH14/EX14.7/14_7_Drug_Medication.sce @@ -0,0 +1,46 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 14.7 Page 913 \n')// Example 14.7
+
+// Total dosage of medicine delivered to the patient over a one-week time period, sensivity of the dosage to the mass duffusivity of the patch and skin
+
+Dap = .1*10^-12 ;//[m^2/s] Diffusion coefficient of medication with patch
+Das = .2*10^-12 ;//[m^2/s] Diffusion coefficient of medication with skin
+L = .05 ;//[m] patch Length
+rhop = 100 ;//[kg/m^3] Density of medication on patch
+rho2 = 0 ;//[kg/m^3] Density of medication on skin
+K = .5 ;//Partition Coefficient
+t = 3600*24*7 ;//[s] Treatment time
+
+//Applying Conservation of species equation 14.47b
+//By analogy to equation 5.62, 5.26 and 5.58
+D = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das*Dap*t)/(sqrt(Das)+sqrt(Dap)/K);
+
+printf('\n Total dosage of medicine delivered to the patient over a one-week time period is %.1f mg',D*10^6);
+
+//Senstivity of dosage to the patch and skin
+clf();
+//Subplot 1
+Dap1 = .1*10^-12 ;//[m^2/s]
+Das1 = .1*10^-12 ;//[m^2/s]
+Das2 = .2*10^-12 ;//[m^2/s]
+Das3 = .4*10^-12 ;//[m^2/s]
+x = linspace(0,7,50);
+y1 = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das1*Dap1*3600*24*x)/(sqrt(Das1)+sqrt(Dap1)/K)*10^6;
+y2 = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das2*Dap1*3600*24*x)/(sqrt(Das2)+sqrt(Dap1)/K)*10^6;
+y3 = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das3*Dap1*3600*24*x)/(sqrt(Das3)+sqrt(Dap1)/K)*10^6;
+subplot(1,2,1);
+plot(x,y1,x,y2,x,y3);
+xtitle("Dosage vs Time-period at Dap = .1*10^ -12 (m^2/s)", "Day", "Dosage (mg)");
+legend (".1*10^12", ".2*10^12", ".4*10^12");
+
+//Subplot 2
+Dap2 = .01*10^-12 ;//[m^2/s]
+yn1 = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das1*Dap2*3600*24*x)/(sqrt(Das1)+sqrt(Dap2)/K)*10^6;
+yn2 = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das2*Dap2*3600*24*x)/(sqrt(Das2)+sqrt(Dap2)/K)*10^6;
+yn3 = 2*rhop*L^2/(sqrt(%pi))*sqrt(Das3*Dap2*3600*24*x)/(sqrt(Das3)+sqrt(Dap2)/K)*10^6;
+subplot(1,2,2);
+plot(x,yn1,x,yn2,x,yn3);
+xtitle("Dosage vs Time-period at Dap = .01*10^ -12 (m^2/s)", "Day", "Dosage (mg)");
+legend (".1*10^12", ".2*10^12", ".4*10^12");
+//END
\ No newline at end of file diff --git a/534/CH2/EX2.1/2_1_Thermal_Diffusivity.sce b/534/CH2/EX2.1/2_1_Thermal_Diffusivity.sce new file mode 100644 index 000000000..dd10dc0c1 --- /dev/null +++ b/534/CH2/EX2.1/2_1_Thermal_Diffusivity.sce @@ -0,0 +1,46 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 2.1 Page 68 \n')//Example 2.1
+// Find Value for Thermal Diffusivity
+
+function a=alpha(p, Cp, k)
+ a=k/(p*Cp); //[m^2/s]
+ funcprot(0);
+endfunction
+
+//(a) Pure Aluminium at 300K
+// From Appendix A, Table A.1
+
+p = 2702; //[Kg/m^3] - Density Of Material
+Cp = 903; //[J/kg.K] - Specific heat of Material
+k = 237; //[W/m.k] - Thermal Conductivity of Material
+
+printf("\n (a) Thermal Diffuisivity of Pure Aluminium at 300K = %.2e m^2/s\n",alpha(p, Cp, k));
+
+//(b) Pure Aluminium at 700K
+// From Appendix A, Table A.1
+
+p = 2702; //[Kg/m^3] - Density Of Material
+Cp = 1090; //[J/kg.K] - Specific heat of Material
+k = 225; //[W/m.k] - Thermal Conductivity of Material
+
+printf("\n (b) Thermal Diffuisivity of Pure Aluminium at 700K = %.2e m^2/s\n",alpha(p, Cp, k));
+
+//(c) Silicon Carbide at 1000K
+// From Appendix A, Table A.2
+
+p = 3160; //[Kg/m^3] - Density Of Material
+Cp = 1195; //[J/kg.K] - Specific heat of Material
+k = 87; //[W/m.k] - Thermal Conductivity of Material
+
+printf("\n (c) Thermal Diffuisivity of Silicon Carbide at 1000K = %.2e m^2/s\n",alpha(p, Cp, k));
+
+//(d) Paraffin at 300K
+// From Appendix A, Table A.3
+
+p = 900; //[Kg/m^3] - Density Of Material
+Cp = 2890; //[J/kg.K] - Specific heat of Material
+k = .24; //[W/m.k] - Thermal Conductivity of Material
+
+printf("\n (d) Thermal Diffuisivity of Paraffin at 300K = %.2e m^2/s",alpha(p, Cp, k));
+//END
diff --git a/534/CH2/EX2.2/2_2_Non_Uniform_Temp_Distribution.sce b/534/CH2/EX2.2/2_2_Non_Uniform_Temp_Distribution.sce new file mode 100644 index 000000000..cc8bae725 --- /dev/null +++ b/534/CH2/EX2.2/2_2_Non_Uniform_Temp_Distribution.sce @@ -0,0 +1,46 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 2.2 Page 75 \n')//Example 2.2
+// Analyze a Situation of Non-Uniform Temperature Distribution
+//T(x) = a + bx +cx^2 T-degC & x-meter
+
+a = 900; //[degC]
+b = -300; //[degC/m]
+c = -50; //[degC/m^2]
+
+q = 1000; //[W/m^2.K] - Unifrom heat Generation
+A = 10 ; //[m^2] - Wall Area
+//Properties of Wall
+p = 1600; //[kg/m^3] - Density
+k = 40; //[W/m] - Thermal Conductivity
+Cp = 4000; //[J/kg.K] - Specific Heat
+L = 1; //[m] - Length of wall
+
+//(i) Rate of Heat Transfer entering the wall and leaving the wall
+// From Eqn 2.1
+// qin = -kA(dT/dx)|x=0 = -kA(b)
+
+qin= - b*k*A;
+
+// Similarly
+// qout = -kA(dT/dx)|x=L = -kA(b+2cx)|x=L
+
+qout= - k*A*(b+2*c*L);
+
+printf("\n (i) Rate of Heat Transfer entering the wall = %i W \n And leaving the wall = %i W \n", qin, qout);
+
+//(ii) Rate of change Of Energy Storage in Wall E`st
+// Applying Overall Energy Balance across the Wall
+//E`st = E`in + E`g + E`out = qin + q`AL - qout
+Est = qin + q*A*L - qout;
+
+printf("\n (ii) Rate of change Of Energy Storage in Wall = %i W\n",Est);
+
+//(iii) Time rate of Temperature change at x= 0, 0.25 and .5m
+//Using Eqn 2.19
+// T`= dT/dt = (k/p*Cp)*d(dT/dx)/dx + q`/p*Cp
+//As d(dT/dx)/dx = d(b + 2cx)/dx = 2c - Independent of x
+T = (k/(p*Cp))*(2*c)+ q/(p*Cp);
+printf("\n (iii) Time rate of Temperature change independent of x = %f degC/s\n",T);
+
+//END
diff --git a/534/CH2/EX2.3/2_3_Theoretical_Problem.sce b/534/CH2/EX2.3/2_3_Theoretical_Problem.sce new file mode 100644 index 000000000..f00d529d2 --- /dev/null +++ b/534/CH2/EX2.3/2_3_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 2.3 Page 79 \n')// Example 2.3
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH3/EX3.1/3_1_Human_Heat_Loss_part2.sce b/534/CH3/EX3.1/3_1_Human_Heat_Loss_part2.sce new file mode 100644 index 000000000..7043393fc --- /dev/null +++ b/534/CH3/EX3.1/3_1_Human_Heat_Loss_part2.sce @@ -0,0 +1,44 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.1 Page 104 \n') //Example 3.1
+// Find Skin Temperature & Aerogel Insulation Thickness
+
+A=1.8; // [m^2] Area for Heat transfer i.e. both surfaces
+Ti = 35+273; //[K] - Inside Surface Temperature of Body
+Tsurr = 10+273; //[K] - Temperature of surrounding
+Tf = 283; //[K] - Temperature of Fluid Flow
+e=.95; // Emissivity of Surface
+Lst=.003; //[m] - Thickness of Skin
+kst=.3; // [W/m.K] Effective Thermal Conductivity of Body
+kins = .014; // [W/m.K] Effective Thermal Conductivity of Aerogel Insulation
+hr = 5.9; //[W/m^2.k] - Natural Thermal Convectivity from body to air
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+q = 100; //[W] Given Heat rate
+
+//Using Conducion Basic Eq 3.19
+Rtot = (Ti-Tsurr)/q;
+//Also
+//Rtot=Lst/(kst*A) + Lins/(kins*A)+(h*A + hr*A)^-1
+//Rtot = 1/A*(Lst/kst + Lins/kins +(1/(h+hr)))
+
+//Thus
+//For Air,
+h=2; //[W/m^2.k] - Natural Thermal Convectivity from body to air
+Lins1 = kins * (A*Rtot - Lst/kst - 1/(h+hr));
+
+//For Water,
+h=200; //[W/m^2.k] - Natural Thermal Convectivity from body to air
+Lins2 = kins * (A*Rtot - Lst/kst - 1/(h+hr));
+
+Tsa=305; //[K] Body Temperature Assumed
+
+//Temperature of Skin is same in both cases as Heat Rate is same
+//q=(kst*A*(Ti-Ts))/Lst
+Ts = Ti - q*Lst/(kst*A);
+
+//Also from eqn of effective resistance Rtot F
+printf("\n\n (I) In presence of Air, Insulation Thickness = %.1f mm",Lins1*1000)
+
+printf("\n (II) In presence of Water, Insulation Thickness = %.1f mm",Lins2*1000);
+printf("\n\n Temperature of Skin = %.2f degC",Ts-273);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.10/3_10_Finned_Cylinder.sce b/534/CH3/EX3.10/3_10_Finned_Cylinder.sce new file mode 100644 index 000000000..772e9dd20 --- /dev/null +++ b/534/CH3/EX3.10/3_10_Finned_Cylinder.sce @@ -0,0 +1,29 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.10 Page 156 \n'); //Example 3.10
+// Study of motorcycle finned cylinder
+
+H = .15; //[m] height
+k = 186; //[W/m.K] alumunium at 400K
+h = 50; //[W/m^2.K] Heat convection coefficient
+Tsurr = 300; //[K] Temperature of surrounding air
+To = 500; //[K] Temp inside
+
+//Dimensions of Fin
+N = 5;
+t = .006; //[m] Thickness
+L = .020; //[m] Length
+r2c = .048; //[m]
+r1 = .025; //[m]
+
+Af = 2*%pi*(r2c^2-r1^2);
+At = N*Af + 2*%pi*r1*(H-N*t);
+
+//Using fig 3.19
+nf = .95;
+
+qt = h*At*[1-N*Af*(1-nf)/At]*(To-Tsurr);
+qwo = h*(2*%pi*r1*H)*(To-Tsurr);
+
+printf("\n\n Heat Transfer Rate with the fins =%i W \n Heat Transfer Rate without the fins =%i W \n Thus Increase in Heat transfer rate of %i W is observed with fins",qt,qwo,qt-qwo);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.11/3_11_Fuel_cell.sce b/534/CH3/EX3.11/3_11_Fuel_cell.sce new file mode 100644 index 000000000..e98810a0b --- /dev/null +++ b/534/CH3/EX3.11/3_11_Fuel_cell.sce @@ -0,0 +1,45 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.11 Page 158 \n'); //Example 3.11
+// Study of Fuel-cell fan system
+
+Wc =.05; //[m] width
+H = .026; //[m] height
+tc = .006; //[m] thickness of cell
+V = 9.4; //[m/sec] vel of cooling air
+P = 9; //[W] Power generated
+C = 1000; //[W/(m^3/s)] Ratio of fan power consumption to vol flow rate
+k = 200; //[W/m.K] alumunium
+Tsurr = 25+273.15; //[K] Temperature of surrounding air
+Tc = 56.4+273.15; //[K] Temp of fuel cell
+Rtcy = 10^-3; //[K/W] Contact thermal resistance
+tb = .002; //[m] thickness of base of heat sink
+Lc = .05; //[m] length of fuel cell
+//Dimensions of Fin
+tf = .001; //[m] Thickness
+Lf = .008; //[m] Length
+
+Vf = V*[Wc*(H-tc)]; //[m^3/sec] Volumetric flow rate
+Pnet = P - C*Vf;
+
+
+P = 2*(Lc+tf);
+Ac = Lc*tf;
+N = 22;
+a=(2*Wc - N*tf)/N;
+h = 19.1; ///[W/m^2.K]
+q = 11.25; //[W]
+m = (h*P/(k*Ac))^.5;
+Rtf = (h*P*k*Ac)^(-.5)/ tanh(m*Lf);
+Rtc = Rtcy/(2*Lc*Wc);
+Rtbase = tb/(2*k*Lc*Wc);
+Rtb = 1/[h*(2*Wc-N*tf)*Lc];
+Rtfn = Rtf/N;
+Requiv = [Rtb^-1 + Rtfn^-1]^-1;
+Rtot = Rtc + Rtbase + Requiv;
+
+Tc2 = Tsurr +q*(Rtot);
+
+printf("\n\n (a) Power consumed by fan is more than the generated power of fuel cell, and hence system cannot produce net power = %.2f W \n\n (b) Actual fuel cell Temp is close enough to %.1f degC for reducing the fan power consumption by half ie Pnet = %.1f W, we require 22 fins, 11 on top and 11 on bottom.",Pnet, Tc2-273, C*Vf/2);
+
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.12/3_12_Human_Heat_Loss_part3.sce b/534/CH3/EX3.12/3_12_Human_Heat_Loss_part3.sce new file mode 100644 index 000000000..29515666e --- /dev/null +++ b/534/CH3/EX3.12/3_12_Human_Heat_Loss_part3.sce @@ -0,0 +1,37 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.12 Page 163 \n'); //Example 3.12
+// Heat loss from body & temp at inner surface
+
+hair = 2; //[W/m^2.K] Heat convection coefficient air
+hwater = 200; //[W/m^2.K] Heat convection coefficient water
+hr = 5.9 ; //[W/m^2.K] Heat radiation coefficient
+Tsurr = 297; //[K] Temperature of surrounding air
+Tc = 37+273; //[K] Temp inside
+e = .95;
+A = 1.8 ; //[m^2] area
+//Prop of blood
+w = .0005 ; //[s^-1] perfusion rate
+pb = 1000; //[kg/m^3] blood density
+cb = 3600; //[J/kg] specific heat
+//Dimensions & properties of muscle & skin/fat
+Lm = .03 ; //[m]
+Lsf = .003 ; //[m]
+km = .5 ; //[W/m.K]
+ksf = .3; //[W/m.K]
+q = 700; //[W/m^3] Metabolic heat generation rate
+
+Rtotair = (Lsf/ksf + 1/(hair + hr))/A;
+Rtotwater = (Lsf/ksf + 1/(hwater))/A;
+
+m = (w*pb*cb/km)^.5;
+Theta = -q/(w*pb*cb);
+
+Tiair = (Tsurr*sinh(m*Lm) + km*A*m*Rtotair*[Theta + (Tc + q/(w*pb*cb))*cosh(m*Lm)])/(sinh(m*Lm)+km*A*m*Rtotair*cosh(m*Lm));
+qair = (Tiair - Tsurr)/Rtotair;
+
+Tiwater = (Tsurr*sinh(m*Lm) + km*A*m*Rtotwater*[Theta + (Tc + q/(w*pb*cb))*cosh(m*Lm)])/(sinh(m*Lm)+km*A*m*Rtotwater*cosh(m*Lm));
+qwater = (Tiwater - Tsurr)/Rtotwater;
+
+printf("\n\n For Air \n Temp excess Ti = %.1f degC and Heat loss rate =%.1f W \n\n For Water \n Temp excess Ti = %.1f degC and Heat loss rate =%.1f W ",Tiair-273,qair,Tiwater-273,qwater);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.2/3_2_Chip_Operating_Temperature.sce b/534/CH3/EX3.2/3_2_Chip_Operating_Temperature.sce new file mode 100644 index 000000000..efa8e4165 --- /dev/null +++ b/534/CH3/EX3.2/3_2_Chip_Operating_Temperature.sce @@ -0,0 +1,21 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.2 Page 107 \n'); //Example 3.2
+// Chip Operating Temperature
+
+Tf = 25+273; //[K] - Temperature of Fluid Flow
+
+L=.008; //[m] - Thickness of Aluminium
+k=239; // [W/m.K] Effective Thermal Conductivity of Aluminium
+Rc=.9*10^-4; //[K.m^2/W] Maximum permeasible Resistane of Epoxy Joint
+q=10^4; //[W/m^2] Heat dissipated by Chip
+h=100; //[W/m^2.k] - Thermal Convectivity from chip to air
+
+//Temperature of Chip
+//q=(Tc-Tf)/(1/h)+(Tc-Tf)/(Rc+(L/k)+(1/h))
+
+Tc = Tf + q*(h+1/(Rc+(L/k)+(1/h)))^-1;
+
+printf("\n\n Temperature of Chip = %.2f degC",Tc-273);
+printf("\n Chip will Work well below its maximum allowable Temperature ie 85 degC")
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.3/3_3_Carbon_Nanotube.sce b/534/CH3/EX3.3/3_3_Carbon_Nanotube.sce new file mode 100644 index 000000000..5777c56d4 --- /dev/null +++ b/534/CH3/EX3.3/3_3_Carbon_Nanotube.sce @@ -0,0 +1,42 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.3 Page 109 \n'); //Example 3.3
+// Find Thermal conductivity of Carbon Nanotube
+
+D = 14 * 10^-9; // [m]Dia of Nanotube
+s = 5*10^-6; // [m]Distance between the islands
+Ts = 308.4; //[K] Temp of sensing island
+Tsurr = 300; //[K] Temp of surrounding
+q = 11.3*10^-6; //[W] Total Rate of Heat flow
+
+//Dimension of platinum line
+wpt = 10^-6; //[m]
+tpt = 0.2*10^-6; //[m]
+Lpt = 250*10^-6; //[m]
+//Dimension of Silicon nitride line
+wsn = 3*10^-6; //[m]
+tsn = 0.5*10^-6; //[m]
+Lsn = 250*10^-6; //[m]
+//From Table A.1 Platinum Temp Assumed = 325K
+kpt = 71.6; //[W/m.K]
+//From Table A.2, Silicon Nitride Temp Assumed = 325K
+ksn = 15.5; //[W/m.K]
+
+Apt = wpt*tpt; //Cross sectional area of platinum support beam
+Asn = wsn*tsn-Apt; //Cross sectional area of Silicon Nitride support beam
+Acn = %pi*D^2/4; //Cross sectional Area of Carbon nanotube
+
+Rtsupp = [kpt*Apt/Lpt + ksn*Asn/Lsn]^-1; //[K/W] Thermal Resistance of each support
+
+qs = 2*(Ts-Tsurr)/Rtsupp; //[W] Heat loss through sensing island support
+qh = q - qs; //[W] Heat loss through heating island support
+
+Th = Tsurr + qh*Rtsupp/2; //[K] Temp of Heating island
+
+//For portion Through Carbon Nanotube
+//qs = (Th-Ts)/(s/(kcn*Acn));
+
+kcn = qs*s/(Acn*(Th-Ts));
+
+printf("\n\n Thermal Conductivity of Carbon nanotube = %.2f W/m.K",kcn);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.4/3_4_Conical_Section.sce b/534/CH3/EX3.4/3_4_Conical_Section.sce new file mode 100644 index 000000000..6a5ab42a3 --- /dev/null +++ b/534/CH3/EX3.4/3_4_Conical_Section.sce @@ -0,0 +1,21 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.4 Page 113 \n'); //Example 3.4
+// Temperature Distribution And Heat rate
+
+a = 0.25;
+x1 = .05; //[m] Distance of smaller end
+x2 = .25; //[m] Distance of larger end
+T1 = 400; //[K] Temperature of smaller end
+T2 = 600; //[K] Temperature of larger end
+k = 3.46; //[W/m.K] From Table A.2, Pyroceram at Temp 285K
+
+x = linspace(0.05,.25,100);
+T=(T1 + (T1-T2)*[(x^-1 - x1^-1)/(x1^-1 - x2^-1)]);
+clf();
+plot(x,T);
+xtitle(" Temp vs distance x", "x (m)", "T (K)");
+
+qx = %pi*a^2*k*(T1-T2)/(4*[1/x1 - 1/x2]); //[W]
+printf("\n\n Heat Transfer rate = %.2f W",qx);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.5/3_5_Critical_Thickness.sce b/534/CH3/EX3.5/3_5_Critical_Thickness.sce new file mode 100644 index 000000000..6010ca20d --- /dev/null +++ b/534/CH3/EX3.5/3_5_Critical_Thickness.sce @@ -0,0 +1,22 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.5 Page 119 \n'); //Example 3.5
+// Critical Thickness
+
+k = .055; //[W/m.K] From Table A.3, Cellular glass at Temp 285K
+h = 5; //[W/m^2.K]
+ri = 5*10^-3; //[m] radius of tube
+
+rct = k/h; // [m] Critical Thickness of Insulation for maximum Heat loss or minimum resistance
+
+x = linspace(0,.07,100);
+ycond=(2.30*log10((x+ri)/ri)/(2*%pi*k));
+yconv=(2*%pi*(x+ri)*h)^-1;
+ytot=yconv+ycond;
+clf();
+plot(x,ycond,x,yconv,x,ytot);
+xtitle("Resistance vs Radii", "r-ri (m)", "R (m.K/W)");
+legend ("Rcond", "Rconv", "Rtotal");
+
+printf("\n\n Critical Radius is = %.3f m \n Heat transfer will increase with the addition of insulation up to a thickness of %.3f m",rct,rct-ri);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.6/3_6_Spherical_Composite.sce b/534/CH3/EX3.6/3_6_Spherical_Composite.sce new file mode 100644 index 000000000..8cc30f96a --- /dev/null +++ b/534/CH3/EX3.6/3_6_Spherical_Composite.sce @@ -0,0 +1,30 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.6 Page 122 \n'); //Example 3.6
+// Heat conduction through Spherical Container
+
+k = .0017; //[W/m.K] From Table A.3, Silica Powder at Temp 300K
+h = 5; //[W/m^2.K]
+r1 = 25*10^-2; //[m] Radius of sphere
+r2 = .275; //[m] Radius including Insulation thickness
+
+//Liquid Nitrogen Properties
+T = 77; //[K] Temperature
+rho = 804; //[kg/m^3] Density
+hfg = 2*10^5; //[J/kg] latent heat of vaporisation
+
+//Air Properties
+Tsurr = 300; //[K] Temperature
+h = 20 ;//[W/m^2.K] convection coefficient
+
+Rcond = (1/r1-1/r2)/(4*%pi*k); //Using Eq 3.36
+Rconv = 1/(h*4*%pi*r2^2);
+q = (Tsurr-T)/(Rcond+Rconv);
+
+printf("\n\n (a)Rate of Heat transfer to Liquid Nitrogen %.2f W",q);
+
+//Using Energy Balance q - m*hfg = 0
+m=q/hfg; //[kg/s] mass of nirtogen lost per second
+mc = m/rho*3600*24*10^3;
+printf("\n\n (b)Mass rate of nitrogen boil off %.2f Litres/day",mc);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.7/3_7_Composite_Plane_Wall.sce b/534/CH3/EX3.7/3_7_Composite_Plane_Wall.sce new file mode 100644 index 000000000..158bf8276 --- /dev/null +++ b/534/CH3/EX3.7/3_7_Composite_Plane_Wall.sce @@ -0,0 +1,24 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.7 Page 129 \n'); //Example 3.7
+// Composite Plane wall
+
+Tsurr = 30+273; //[K] Temperature of surrounding Water
+h = 1000; //[W/m^2.K] Heat Convection Coeff of Water
+kb = 150; //[W/m.K] Material B
+Lb = .02; //[m] Thickness Material B
+ka = 75; //[W/m.K] Material A
+La = .05; //[m] Thickness Material A
+qa = 1.5*10^6; //[W/m^3] Heat generation at wall A
+qb = 0; //[W/m^3] Heat generation at wall B
+
+T2 = Tsurr + qa*La/h;
+
+Rcondb = Lb/kb;
+Rconv = 1/h;
+T1 = Tsurr +(Rcondb + Rconv)*(qa*La);
+//From Eqn 3.43
+T0 = qa*La^2/(2*ka) + T1;
+
+printf("\n\n (a) Inner Temperature of Composite To = %i degC \n (b) Outer Temperature of the Composite T2 = %i degC",T0-273,T2-273);
+//END
\ No newline at end of file diff --git a/534/CH3/EX3.8/3_8_Theoretical_Problem.sce b/534/CH3/EX3.8/3_8_Theoretical_Problem.sce new file mode 100644 index 000000000..53252c834 --- /dev/null +++ b/534/CH3/EX3.8/3_8_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.8 Page 134 \n')// Example 3.8
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH3/EX3.9/3_9_Rod_Fin.sce b/534/CH3/EX3.9/3_9_Rod_Fin.sce new file mode 100644 index 000000000..45d279305 --- /dev/null +++ b/534/CH3/EX3.9/3_9_Rod_Fin.sce @@ -0,0 +1,40 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 3.9 Page 145 \n'); //Example 3.9
+// Heat conduction through Rod
+
+kc = 398; //[W/m.K] From Table A.1, Copper at Temp 335K
+kal = 180; //[W/m.K] From Table A.1, Aluminium at Temp 335K
+kst = 14; //[W/m.K] From Table A.1, Stainless Steel at Temp 335K
+h = 100; //[W/m^2.K] Heat Convection Coeff of Air
+Tsurr = 25+273; //[K] Temperature of surrounding Air
+D = 5*10^-3; //[m] Dia of rod
+To = 100+273.15; //[K] Temp of opposite end of rod
+
+//For infintely long fin m = h*P/(k*A)
+mc = (4*h/(kc*D))^.5;
+mal = (4*h/(kal*D))^.5;
+mst = (4*h/(kst*D))^.5;
+x = linspace(0,.300,100);
+Tc = Tsurr + (To - Tsurr)*2.73^(-mc*x) - 273;
+Tal = Tsurr + (To - Tsurr)*2.73^(-mal*x) -273;
+Tst = Tsurr + (To - Tsurr)*2.73^(-mst*x) -273;
+clf();
+plot(x,Tc,x,Tal,x,Tst);
+xtitle("Temp vs Distance", "x (m)", "T (degC)");
+legend ("Cu", "2024 Al", "316 SS");
+
+//Using eqn 3.80
+qfc = (h*%pi*D*kc*%pi/4*D^2)^.5*(To-Tsurr);
+qfal = (h*%pi*D*kal*%pi/4*D^2)^.5*(To-Tsurr);
+qfst = (h*%pi*D*kst*%pi/4*D^2)^.5*(To-Tsurr);
+
+printf("\n\n (a) Heat rate \n For Copper = %.2f W \n For Aluminium = %.2f W \n For Stainless steel = %.2f W",qfc,qfal,qfst);
+
+//Using eqn 3.76 for satisfactory approx
+Linfc = 2.65/mc;
+Linfal = 2.65/mal;
+Linfst = 2.65/mst;
+
+printf("\n\n (a) Rods may be assumed to be infinite Long if it is greater than equal to \n For Copper = %.2f m \n For Aluminium = %.2f m \n For Stainless steel = %.2f m",Linfc,Linfal,Linfst);
+//END
\ No newline at end of file diff --git a/534/CH4/EX4.1/4_1_Eccentric_Wire.sce b/534/CH4/EX4.1/4_1_Eccentric_Wire.sce new file mode 100644 index 000000000..97ff4e5de --- /dev/null +++ b/534/CH4/EX4.1/4_1_Eccentric_Wire.sce @@ -0,0 +1,21 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 4.1 Page 211 \n'); //Example 4.1
+// Thermal resistance of wire coating associated with peripheral variations in coating thickness
+
+d = .005; //[m] Diameter of wire
+k = .35; //[W/m.K] Thermal Conductivity
+h = 15; //[W/m^2.K] Total coeff with Convection n Radiation
+
+rcr = k/h; // [m] critical insulation radius
+tcr = rcr - d/2; // [m] critical insulation Thickness
+
+Rtcond = 2.302*log10(rcr/(d/2))/(2*%pi*k); //[K/W] Thermal resistance
+
+//Using Table 4.1 Case 7
+z = .5*tcr;
+D=2*rcr;
+Rtcond2D = (acosh((D^2 + d^2 - 4*z^2)/(2*D*d)))/(2*%pi*k);
+
+printf("\n\n The reduction in thermal resistance of the insulation is %.2f K/W ", Rtcond-Rtcond2D);
+//END
\ No newline at end of file diff --git a/534/CH4/EX4.2/4_2_Theoretical_Problem.sce b/534/CH4/EX4.2/4_2_Theoretical_Problem.sce new file mode 100644 index 000000000..21ba9886b --- /dev/null +++ b/534/CH4/EX4.2/4_2_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 4.2 Page 218 \n')// Example 4.2
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH4/EX4.3/4_3_Column_Matrix.sce b/534/CH4/EX4.3/4_3_Column_Matrix.sce new file mode 100644 index 000000000..064caa7f9 --- /dev/null +++ b/534/CH4/EX4.3/4_3_Column_Matrix.sce @@ -0,0 +1,33 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 4.3 Page 224 \n'); //Example 4.2
+// Temperature Distribution and Heat rate per unit length
+
+Ts = 500; //[K] Temp of surface
+Tsurr = 300; //[K] Temp of surrounding Air
+h = 10; //[W/m^2.K] Heat Convection soefficient
+//Support Column
+delx = .25; //[m]
+dely = .25; //[m]
+k = 1; //[W/m.K] From Table A.3, Fireclay Brick at T = 478K
+
+//Applying Eqn 4.42 and 4.48
+A = [-4 1 1 0 0 0 0 0;
+ 2 -4 0 1 0 0 0 0;
+ 1 0 -4 1 1 0 0 0;
+ 0 1 2 -4 0 1 0 0;
+ 0 0 1 0 -4 1 1 0;
+ 0 0 0 1 2 -4 0 1;
+ 0 0 0 0 2 0 -9 1;
+ 0 0 0 0 0 2 2 -9 ];
+
+C = [-1000; -500; -500; 0; -500; 0; -2000; -1500 ];
+
+T = inv(A)*C;
+
+printf("\n Temp Distribution = ");
+printf("\n %.2f K ", T);
+
+q = 2*h*[(delx/2)*(Ts-Tsurr)+delx*(T(7)-Tsurr)+delx*(T(8)-Tsurr)/2];
+printf("\n\n Heat rate from column to the airstream %.1f W/m ", q);
+//END
\ No newline at end of file diff --git a/534/CH4/EX4.4/4_4_Turbine_Matrix.sce b/534/CH4/EX4.4/4_4_Turbine_Matrix.sce new file mode 100644 index 000000000..490bed5e7 --- /dev/null +++ b/534/CH4/EX4.4/4_4_Turbine_Matrix.sce @@ -0,0 +1,73 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 4.4 Page 230 \n'); //Example 4.4
+// Temperature Field and Rate of Heat Transfer
+
+//Operating Conditions
+
+ho = 1000; //[W/m^2.K] Heat Convection coefficient
+hi = 200; //[W/m^2.K] Heat Convection coefficient
+Ti = 400; //[K] Temp of Air
+Tg = 1700; //[K] Temp of Gas
+h = 10 ; //[W/m^2.K] Heat Convection coefficient
+
+A = 2*6*10^-6 ; //[m^2] Cross section of each Channel
+x = .004 ; //[m] Spacing between joints
+t = .006; //[m] Thickness
+k = 25; //[W/m.K] Thermal Conductivity of Blade
+delx = .001 ; //[m]
+dely = .001 ; //[m]
+
+//Applying Eqn 4.42 and 4.48
+A = [-(2+ho*delx/k) 1 0 0 0 0 1 0 0 0 0 0 0 0 0 0 0 0 0 0 0;
+ 1 -2*(2+ho*delx/k) 1 0 0 0 0 2 0 0 0 0 0 0 0 0 0 0 0 0 0;
+ 0 1 -2*(2+ho*delx/k) 1 0 0 0 0 2 0 0 0 0 0 0 0 0 0 0 0 0;
+ 0 0 1 -2*(2+ho*delx/k) 1 0 0 0 0 2 0 0 0 0 0 0 0 0 0 0 0;
+ 0 0 0 1 -2*(2+ho*delx/k) 1 0 0 0 0 2 0 0 0 0 0 0 0 0 0 0;
+ 0 0 0 0 1 -(2+ho*delx/k) 0 0 0 0 0 1 0 0 0 0 0 0 0 0 0;
+ 1 0 0 0 0 0 -4 2 0 0 0 0 1 0 0 0 0 0 0 0 0;
+ 0 1 0 0 0 0 1 -4 1 0 0 0 0 1 0 0 0 0 0 0 0;
+ 0 0 1 0 0 0 0 1 -4 1 0 0 0 0 1 0 0 0 0 0 0;
+ 0 0 0 1 0 0 0 0 1 -4 1 0 0 0 0 1 0 0 0 0 0;
+ 0 0 0 0 1 0 0 0 0 1 -4 1 0 0 0 0 1 0 0 0 0;
+ 0 0 0 0 0 1 0 0 0 0 2 -4 0 0 0 0 0 1 0 0 0;
+ 0 0 0 0 0 0 1 0 0 0 0 0 -4 2 0 0 0 0 1 0 0;
+ 0 0 0 0 0 0 0 1 0 0 0 0 1 -4 1 0 0 0 0 1 0;
+ 0 0 0 0 0 0 0 0 2 0 0 0 0 2 -2*(3+hi*delx/k) 1 0 0 0 0 1;
+ 0 0 0 0 0 0 0 0 0 2 0 0 0 0 1 -2*(2+hi*delx/k) 1 0 0 0 0;
+ 0 0 0 0 0 0 0 0 0 0 2 0 0 0 0 1 -2*(2+hi*delx/k) 1 0 0 0;
+ 0 0 0 0 0 0 0 0 0 0 0 1 0 0 0 0 1 -(2+hi*delx/k) 0 0 0;
+ 0 0 0 0 0 0 0 0 0 0 0 0 1 0 0 0 0 0 -2 1 0;
+ 0 0 0 0 0 0 0 0 0 0 0 0 0 2 0 0 0 0 1 -4 1;
+ 0 0 0 0 0 0 0 0 0 0 0 0 0 0 1 0 0 0 0 1 -(2+hi*delx/k)];
+
+C = [-ho*delx*Tg/k;
+ -2*ho*delx*Tg/k;
+ -2*ho*delx*Tg/k;
+ -2*ho*delx*Tg/k;
+ -2*ho*delx*Tg/k;
+ -ho*delx*Tg/k;
+ 0;
+ 0;
+ 0;
+ 0;
+ 0;
+ 0;
+ 0;
+ 0;
+ -2*hi*delx*Ti/k;
+ -2*hi*delx*Ti/k;
+ -2*hi*delx*Ti/k;
+ -hi*delx*Ti/k;
+ 0;
+ 0;
+ -hi*delx*Ti/k];
+
+T = inv(A)*C;
+
+printf("\n Temp Distribution = ");
+printf("\n %.1f K ", T);
+
+q = 4*ho*[(delx/2)*(Tg-T(1))+delx*(Tg-T(2))+delx*(Tg-T(3))+ delx*(Tg-T(4))+delx*(Tg-T(5))+delx*(Tg-T(6))/2];
+printf("\n\n Heat rate Transfer %.1f W/m ", q);
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.1/5_1_Thermocouple_junction.sce b/534/CH5/EX5.1/5_1_Thermocouple_junction.sce new file mode 100644 index 000000000..f41c10e04 --- /dev/null +++ b/534/CH5/EX5.1/5_1_Thermocouple_junction.sce @@ -0,0 +1,27 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.1 Page 261 \n'); //Example 5.1
+// Junction Diameter and Time Calculation to attain certain temp
+
+//Operating Conditions
+
+h = 400; //[W/m^2.K] Heat Convection coefficient
+k = 20; //[W/m.K] Thermal Conductivity of Blade
+c = 400; //[J/kg.K] Specific Heat
+rho = 8500; //[kg/m^3] Density
+Ti = 25+273; //[K] Temp of Air
+Tsurr = 200+273; //[K] Temp of Gas Stream
+TimeConstt = 1; //[sec]
+
+//From Eqn 5.7
+D = 6*h*TimeConstt/(rho*c);
+Lc = D/6;
+Bi = h*Lc/k;
+
+//From eqn 5.5 for time to reach
+T = 199+273; //[K] Required temperature
+
+t = rho*D*c*2.30*log10((Ti-Tsurr)/(T-Tsurr))/(h*6);
+
+printf("\n\n Junction Diameter needed for a time constant of 1 s = %.2e m \n\n Time Required to reach 199degC in a gas stream = %.1f sec ", D, t);
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.10/5_10_Finite_Difference2_slab.sce b/534/CH5/EX5.10/5_10_Finite_Difference2_slab.sce new file mode 100644 index 000000000..5db5cf98b --- /dev/null +++ b/534/CH5/EX5.10/5_10_Finite_Difference2_slab.sce @@ -0,0 +1,108 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.10 Page 311 \n'); //Example 5.10
+// Using Explicit Finite Difference method, determine temperatures at the surface and 150 mm from the surface after an elapsed time of 2 min
+// Repeat the calculations using the Implicit Finite Difference Method
+// Determine the same temperatures analytically
+
+//Operating Conditions
+
+delx = .075; //[m] Metre
+T = 20+273; //[K] Temperature
+q = 3*10^5; //[W/m^3] Volumetric Rate
+
+//From Table A.1 copper 300 K
+k = 401; //[W/m.K] Conductivity
+a = 117*10^-6; //[m^2/s]
+
+//By using stability criterion reducing further Fourier Number
+Fo = (2)^-1;
+//By definition
+delt = Fo*delx^2/a;
+format('v',5);
+
+//System of Equation for Explicit Finite difference Fo = 1/2
+Tv1(1,:) = [20 20 20 20 20]; //At p=0 Initial Temperature t - 20 degC
+for i = 2:6
+ Tv1(i,1) = 56.1 + Tv1(i-1,2);
+ Tv1(i,2) = (Tv1(i-1,3) + Tv1(i-1,1))/2;
+ Tv1(i,3) = (Tv1(i-1,4) + Tv1(i-1,2))/2;
+ Tv1(i,4) = (Tv1(i-1,5) + Tv1(i-1,3))/2;
+ Tv1(i,5) = Tv1(i-1,5);
+end
+for j=1:6
+ T1(j,:)=[j-1 delt*(j-1) Tv1(j,:)];
+end
+printf("\n\n EXPLICIT FINITE-DIFFERENCE SOLUTION FOR Fo = 1/2\n p t(s) T0 T1 T2 T3 T4\n");
+disp(T1);
+printf('\n Hence after 2 min, the surface and the desirde interior temperature T0 = %.2f degC and T2 = %.1f degC',T1(6,3),T1(6,5));
+
+//By using stability criterion reducing further Fourier Number
+Fo = (4)^-1;
+//By definition
+delt = Fo*delx^2/a;
+//System of Equation for Explicit Finite difference for Fo = 1/4
+Tv2(1,:) = [20 20 20 20 20 20 20 20 20]; //At p=0 Initial Temperature t - 20 degC
+for i=2:11
+ Tv2(i,1)=1/2*(q*delx/k + Tv2(i-1,2)) +Tv2(i-1,1)/2;
+ Tv2(i,2)=(Tv2(i-1,1)+Tv2(i-1,3))/4 + Tv2(i-1,2)/2;
+ Tv2(i,3)=(Tv2(i-1,2)+Tv2(i-1,4))/4 + Tv2(i-1,3)/2;
+ Tv2(i,4)=(Tv2(i-1,3)+Tv2(i-1,5))/4 + Tv2(i-1,4)/2;
+ Tv2(i,5)=(Tv2(i-1,4)+Tv2(i-1,6))/4 + Tv2(i-1,5)/2;
+ Tv2(i,6)=(Tv2(i-1,5)+Tv2(i-1,7))/4 + Tv2(i-1,6)/2;
+ Tv2(i,7)=(Tv2(i-1,6)+Tv2(i-1,8))/4 + Tv2(i-1,7)/2;
+ Tv2(i,8)=(Tv2(i-1,7)+Tv2(i-1,9))/4 + Tv2(i-1,8)/2;
+ Tv2(i,9)= Tv2(i-1,9);
+end
+for j=1:11
+ T2(j,:)=[j-1 delt*(j-1) Tv2(j,:)];
+end
+printf("\n\n EXPLICIT FINITE-DIFFERENCE SOLUTION FOR Fo = 1/4\n p t(s) T0 T1 T2 T3 T4 T5 T6 T7 T8\n")
+disp(T2)
+printf('\n Hence after 2 min, the surface and the desirde interior temperature T0 = %.2f degC and T2 = %.1f degC',T2(11,3),T2(11,5))
+
+
+//(b)Implicit Finite Difference solution
+Fo = (4)^-1;
+//By definition
+delt = Fo*delx^2/a;
+
+T3 = rand(6,11); //Random Initital Distribution
+function[Tm]=Tvalue(i)
+function[f]=F(x)
+ f(1)= 2*x(1) - x(2) - q*delx/k - T3(i,3);
+ f(2)= -x(1)+4*x(2)-x(3)-2*T3(i,4);
+ f(3)= -x(2)+4*x(3)-x(4)-2*T3(i,5);
+ f(4)= -x(3)+4*x(4)-x(5)-2*T3(i,6);
+ f(5)= -x(4)+4*x(5)-x(6)-2*T3(i,7);
+ f(6)= -x(5)+4*x(6)-x(7)-2*T3(i,8);
+ f(7)= -x(6)+4*x(7)-x(8)-2*T3(i,9);
+ f(8)= -x(7)+4*x(8)-x(9)-2*T3(i,10);
+ f(9)= -x(9)+T3(i,11);
+ funcprot(0);
+endfunction
+x = [30 30 30 30 30 30 30 30 30];
+Tm = fsolve(x,F);
+ funcprot(0)
+endfunction
+
+//At p=0 Initial Temperature t - 20 degC
+T3(1,:) = [0 delt*0 20 20 20 20 20 20 20 20 20];
+for j=1:5
+ T3(j+1,:)=[j delt*j Tvalue(j)];
+end
+printf("\n\n IMPLICIT FINITE-DIFFERENCE SOLUTION FOR Fo = 1/4\n p t(s) T0 T1 T2 T3 T4 T5 T6 T7 T8\n");
+disp(T3);
+printf('\n Hence after 2 min, the surface and the desirde interior temperature T0 = %.2f degC and T2 = %.1f degC',T3(6,3),T3(6,5));
+
+t = 120; //[seconds]
+//(c) Approximating slab as semi-infinte medium
+Tc = T -273 + 2*q*(a*t/%pi)^.5/k;
+
+//At interior point x=0.15 m
+x =.15; //[metre]
+//Analytical Expression
+Tc2 = T -273 + 2*q*(a*t/%pi)^.5/k*exp(-x^2/(4*a*t))-q*x/k*[1-erf(.15/(2*sqrt(a*t)))];
+
+printf(' \n\n (c) Approximating slab as a semi infinte medium, Analytical epression yields \n At surface after 120 seconds = %.1f degC \n At x=.15 m after 120 seconds = %.1f degC',Tc,Tc2);
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.2/5_2_Thermocouple_junction2.sce b/534/CH5/EX5.2/5_2_Thermocouple_junction2.sce new file mode 100644 index 000000000..cedc27399 --- /dev/null +++ b/534/CH5/EX5.2/5_2_Thermocouple_junction2.sce @@ -0,0 +1,49 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.2 Page 265 \n'); //Example 5.2
+// Steady State Temperature of junction
+// Time Required for thermocouple to reach a temp that is within 1 degc of its steady-state value
+
+//Operating Conditions
+
+h = 400; //[W/m^2.K] Heat Convection coefficient
+k = 20; //[W/m.K] Thermal Conductivity of Blade
+c = 400; //[J/kg.K] Specific Heat
+e = .9; //Absorptivity
+rho = 8500; //[kg/m^3] Density
+Ti = 25+273; //[K] Temp of Air
+Tsurr = 400+273; //[K] Temp of duct wall
+Tg = 200+273; //[K] Temp of Gas Stream
+TimeConstt = 1; //[sec]
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+
+//From Eqn 5.7
+D = 6*h*TimeConstt/(rho*c);
+As = %pi*D^2;
+V = %pi*D^3/6;
+
+//Balancing Energy on thermocouple Junction
+//Newton Raphson method for 4th order eqn
+T=500;
+while(1>0)
+f=(e*stfncnstt*(Tsurr^4-T^4)-(h*(T-Tg)));
+fd=(-3*e*stfncnstt*T^3)-h;
+Tn=T-f/fd;
+if((e*stfncnstt*(Tsurr^4-Tn^4)-(h*(Tn-Tg)))<=.01)
+ break;
+end;
+T=Tn;
+end
+printf("\n (a) Steady State Temperature of junction = %.2f degC\n",T-273);
+
+//Using Eqn 5.15 and Integrating the ODE
+// Integration of the differential equation
+// dT/dt=-A*[h*(T-Tg)+e*stefncnstt*(T^4-Tsurr^4)]/(rho*V*c) , T(0)=25+273, and finds the minimum time t such that T(t)=217.7+273.15
+deff("[Tdot]=f(t,T)","Tdot=-As*[h*(T-Tg)+e*stfncnstt*(T^4-Tsurr^4)]/(rho*V*c)");
+deff("[z]=g(t,T)","z=T-217.7-273");
+
+T0=25+273;ng=1;
+[T,rd]=ode("roots",T0,0,217.7+273,f,ng,g);
+printf("\n (b) Time Required for thermocouple to reach a temp that is within 1 degc of its steady-state value = %.2f s\n",rd(1));
+
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.3/5_3_Two_step_process.sce b/534/CH5/EX5.3/5_3_Two_step_process.sce new file mode 100644 index 000000000..b481ac7dc --- /dev/null +++ b/534/CH5/EX5.3/5_3_Two_step_process.sce @@ -0,0 +1,75 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.2 Page 267 \n'); //Example 5.3
+// Total Time t required for two step process
+
+//Operating Conditions
+
+ho = 40; //[W/m^2.K] Heat Convection coefficient
+hc = 10; //[W/m^2.K] Heat Convection coefficient
+k = 177; //[W/m.K] Thermal Conductivity
+e = .8; //Absorptivity
+L = 3*10^-3/2; //[m] Metre
+Ti = 25+273; //[K] Temp of Aluminium
+Tsurro = 175+273; //[K] Temp of duct wall heating
+Tsurrc = 25+273; //[K] Temp of duct wall
+Tit = 37+273; //[K] Temp at cooling
+Tc = 150+273; //[K] Temp critical
+
+stfncnstt=5.67*10^(-8); // [W/m^2.K^4] - Stefan Boltzmann Constant
+p = 2770; //[kg/m^3] density of aluminium
+c = 875; //[J/kg.K] Specific Heat
+
+//To assess the validity of the lumped capacitance approximation
+Bih = ho*L/k;
+Bic = hc*L/k;
+printf("\n Lumped capacitance approximation is valid as Bih = %f and Bic = %f", Bih, Bic);
+
+//Eqn 1.9
+hro = e*stfncnstt*(Tc+Tsurro)*(Tc^2+Tsurro^2);
+hrc = e*stfncnstt*(Tc+Tsurrc)*(Tc^2+Tsurrc^2);
+printf("\n Since The values of hro = %.1f and hrc = %.1f are comparable to those of ho and hc, respectively radiation effects must be considered", hro,hrc);
+
+// Integration of the differential equation
+// dy/dt=-1/(p*c*L)*[ho*(y-Tsurro)+e*stfncnstt*(y^4 - Tsurro^4)] , y(0)=Ti, and finds the minimum time t such that y(t)=150 degC
+deff("[ydot]=f1(t,y)","ydot=-1/(p*c*L)*[ho*(y-Tsurro)+e*stfncnstt*(y^4 - Tsurro^4)]");
+deff("[z]=g1(t,y)","z=y-150-273");
+y0=Ti;
+[y,tc]=ode("root",y0,0,150+273,f1,1,g1);
+te = tc(1) + 300;
+
+//From equation 5.15 and solving the two step process using integration
+function Tydot=f(t,T)
+ Tydot=-1/(p*c*L)*[ho*(T-Tsurro)+e*stfncnstt*(T^4 - Tsurro^4)];
+ funcprot(0)
+endfunction
+Ty0=Ti;
+t0=0;
+t=0:10:te;
+Ty=ode("rk",Ty0,t0,t,f);
+
+// solution of integration of the differential equation
+// dy/dt=-1/(p*c*L)*[hc*(y-Tsurrc)+e*stfncnstt*(y^4 - Tsurrc^4)] , y(rd(1))=Ty(43), and finds the minimum time t such that y(t)=37 degC=Tit
+deff("[Tdot]=f2(t,T)","Tdot=-1/(p*c*L)*[hc*(T-Tsurrc)+e*stfncnstt*(T^4 - Tsurrc^4)]");
+for(tt=0:1:900)
+ tq=ode(Ty(43),0,tt,f2);
+ if(tq-Tit<=10^-2)
+ break;
+ end
+end
+
+function Ty2dot=f2(t,T)
+ Ty2dot=-1/(p*c*L)*[hc*(T-Tsurrc)+e*stfncnstt*(T^4 - Tsurrc^4)];
+ funcprot(0)
+endfunction
+Ty20=Ty(43);
+t20=te;
+t2=te:10:1200;
+Ty2=ode("rk",Ty20,t20,t2,f2);
+clf();
+plot(t,Ty-273,t2,Ty2-273,[tc(1) tc(1)],[0 Tc-273],[te te],[0 Ty(43)-273],[tt+te tt+te],[0 tq-273]);
+xtitle('Plot of the Two-Step Process','t (s)','T (degC)');
+legend('Heating','Cooling','tc','te','tt');
+
+printf('\n\n Total time for the two-step process is t = %i s with intermediate times of tc = %i s and te = %i s.',tt+te,tc(1),te);
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.4/5_4_Radial_Two_Step.sce b/534/CH5/EX5.4/5_4_Radial_Two_Step.sce new file mode 100644 index 000000000..64b3b4b7b --- /dev/null +++ b/534/CH5/EX5.4/5_4_Radial_Two_Step.sce @@ -0,0 +1,40 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.4 Page 278 \n'); //Example 5.4
+// Radial System with Convection
+
+//Operating Conditions
+
+h = 500; //[W/m^2.K] Heat Convection coefficientat inner surface
+k = 63.9; //[W/m.K] Thermal Conductivity
+rho = 7832; //[kg/m^3] Density
+c = 434; //[J/kg.K] Specific Heat
+alpha = 18.8*10^-6; //[m^2/s]
+L = 40*10^-3; //[m] Metre
+Ti = -20+273; //[K] Initial Temp
+Tsurr = 60+273; //[K] Temp of oil
+t = 8*60 ; //[sec] time
+D = 1 ; //[m] Diameter of pipe
+
+//Using eqn 5.10 and 5.12
+Bi = h*L/k;
+Fo = alpha*t/L^2;
+
+//From Table 5.1 at this Bi
+C1 = 1.047;
+eta = 0.531;
+theta0=C1*exp(-eta^2*Fo);
+T = Tsurr+theta0*(Ti-Tsurr);
+
+//Using eqn 5.40b
+x=1;
+theta = theta0*cos(eta);
+Tl = Tsurr + (Ti-Tsurr)*theta;
+q = h*[Tl - Tsurr];
+
+//Using Eqn 5.44, 5.46 and Vol per unit length V = pi*D*L
+Q = [1-(sin(eta)/eta)*theta0]*rho*c*%pi*D*L*(Ti-Tsurr);
+
+printf("\n (a) After 8 min Biot number = %.2f and Fourier Numer = %.2f \n\n (b) Temperature of exterior pipe surface after 8 min = %i degC \n\n (c) Heat Flux to the wall at 8 min = %i W/m^2 \n\n (d) Energy transferred to pipe per unit length after 8 min = %.2e J/m",Bi,Fo, T-273,q,Q);
+
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.5/5_5_Sphere_Two_Step.sce b/534/CH5/EX5.5/5_5_Sphere_Two_Step.sce new file mode 100644 index 000000000..f0fb0366d --- /dev/null +++ b/534/CH5/EX5.5/5_5_Sphere_Two_Step.sce @@ -0,0 +1,34 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.5 Page 280 \n'); //Example 5.5
+// Two step cooling process of Sphere
+
+//Operating Conditions
+
+ha = 10; //[W/m^2.K] Heat Convection coefficientat air
+hw = 6000; //[W/m^2.K] Heat Convection coefficientat water
+k = 20; //[W/m.K] Thermal Conductivity
+rho = 3000; //[kg/m^3] Density
+c = 1000; //[J/kg.K] Specific Heat
+alpha = 6.66*10^-6; //[m^2/s]
+Tiw = 335+273; //[K] Initial Temp
+Tia = 400+273; //[K] Initial Temp
+Tsurr = 20+273; //[K] Temp of surrounding
+T = 50+273; //[K] Temp of center
+ro = .005; //[m] radius of sphere
+
+//Using eqn 5.10 and
+Lc = ro/3;
+Bi = ha*Lc/k;
+ta = rho*ro*c*2.30*(log10((Tia-Tsurr)/(Tiw-Tsurr)))/(3*ha);
+
+//From Table 5.1 at this Bi
+C1 = 1.367;
+eta = 1.8;
+Fo = -1*2.30*log10((T-Tsurr)/((Tiw-Tsurr)*C1))/eta^2;
+
+tw = Fo*ro^2/alpha;
+
+printf("\n (a) Time required to accomplish desired cooling in air ta = %.1f s\n\n (b) Time required to accomplish desired cooling in water bath tw = %.2f s",ta,tw);
+
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.6/5_6_Burial_Depth.sce b/534/CH5/EX5.6/5_6_Burial_Depth.sce new file mode 100644 index 000000000..7cc458dd7 --- /dev/null +++ b/534/CH5/EX5.6/5_6_Burial_Depth.sce @@ -0,0 +1,22 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.6 Page 288 \n'); //Example 5.6
+// Burial Depth
+
+//Operating Conditions
+
+k = .52; //[W/m.K] Thermal Conductivity
+rho = 2050; //[kg/m^3] Density
+c = 1840; //[J/kg.K] Specific Heat
+Ti = 20+273; //[K] Initial Temp
+Ts = -15+273; //[K] Temp of surrounding
+T = 0+273; //[K] Temp at depth xm after 60 days
+t = 60*24*3600; //[sec] time perod
+
+alpha = k/(rho*c); //[m^2/s]
+//Using eqn 5.57
+xm = erfinv((T-Ts)/(Ti-Ts))*2*(alpha*t)^.5;
+
+printf("\n Depth at which after 60 days soil freeze = %.2f m",xm);
+
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.7/5_7_Spherical_Tumor.sce b/534/CH5/EX5.7/5_7_Spherical_Tumor.sce new file mode 100644 index 000000000..3104f4932 --- /dev/null +++ b/534/CH5/EX5.7/5_7_Spherical_Tumor.sce @@ -0,0 +1,38 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.7 Page 293 \n'); //Example 5.7
+// Spherical Tumor
+
+//Operating Conditions
+
+k = .5; //[W/m.K] Thermal Conductivity Healthy Tissue
+kappa = .02*10^3; //[m] extinction coefficient
+p = .05; // reflectivity of skin
+D = .005; //[m] Laser beam Dia
+rho = 989.1 ; //[kg/m^3] Density
+c = 4180 ; //[J/kg.K] Specific Heat
+Tb = 37+273; //[K] Temp of healthy tissue
+Dt = .003 ; //[m] Dia of tissue
+d = .02 ; //[m] depth beneath the skin
+Ttss = 55+273 ; //[K] Steady State Temperature
+Tb = 37+273 ; //[K] Body Temperature
+Tt = 52+273 ; //[K] Tissue Temperature
+q = .170 ; //[W]
+
+//Case 12 of Table 4.1
+q = 2*%pi*k*Dt*(Ttss-Tb);
+
+//Energy Balancing
+P = q*(D^2)*exp(kappa*d)/((1-p)*Dt^2);
+
+//Using Eqn 5.14
+t = rho*(%pi*Dt^3/6)*c*(Tt-Tb)/q;
+
+alpha=k/(rho*c);
+Fo = 10.3;
+//Using Eqn 5.68
+t2 = Fo*Dt^2/(4*alpha);
+
+printf("\n (a) Heat transferred from the tumor to maintain its surface temperature at Ttss = 55 degC is %.2f W \n\n (b) Laser power needed to sustain the tumor surface temperautre at Ttss = 55 degC is %.2f W \n\n (c) Time for tumor to reach Tt = 52 degC when heat transfer to the surrounding tissue is neglected is %.2f sec \n\n (d) Time for tumor to reach Tt = 52 degC when Heat transfer to thesurrounding tissue is considered and teh thermal mass of tumor is neglected is %.2f sec" ,q,P,t,t2);
+
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.8/5_8_Nanostructured_Material.sce b/534/CH5/EX5.8/5_8_Nanostructured_Material.sce new file mode 100644 index 000000000..71fc149ad --- /dev/null +++ b/534/CH5/EX5.8/5_8_Nanostructured_Material.sce @@ -0,0 +1,33 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.8 Page 300 \n'); //Example 5.8
+// Thermal Conductivity of Nanostructured material
+
+//Operating Conditions
+
+k = 1.11 ; //[W/m.K] Thermal Conductivity
+rho = 3100; //[kg/m^3] Density
+c = 820 ; //[J/kg.K] Specific Heat
+//Dimensions of Strip
+w = 100*10^-6; //[m] Width
+L = .0035 ; //[m] Long
+d = 3000*10^-10; //[m] Thickness
+delq = 3.5*10^-3; //[W] heating Rate
+delT1 =1.37 ; //[K] Temperature 1
+f1 = 2*%pi ; //[rad/s] Frequency 1
+delT2 =.71 ; //[K] Temperature 2
+f2 = 200*%pi; //[rad/s] Frequency 2
+
+A = [delT1 -delq/(L*%pi);
+ delT2 -delq/(L*%pi)] ;
+
+C= [delq*-2.30*log10(f1/2)/(2*L*%pi);
+ delq*-2.30*log10(f2/2)/(2*L*%pi)] ;
+
+B = inv(A)*C;
+
+alpha = k/(rho*c);
+delp = [(alpha/f1)^.5 (alpha/f2)^.5];
+printf("\n C2 = %.2f k = %.2f W/m.K \n\n Thermal Penetration depths are %.2e m and %.2e m at frequency 2*pi rad/s and 200*pi rad/s" ,B(2),B(1), delp);
+
+//END
\ No newline at end of file diff --git a/534/CH5/EX5.9/5_9_Finite_Difference1.sce b/534/CH5/EX5.9/5_9_Finite_Difference1.sce new file mode 100644 index 000000000..b527b3273 --- /dev/null +++ b/534/CH5/EX5.9/5_9_Finite_Difference1.sce @@ -0,0 +1,56 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 5.9 Page 305 \n'); //Example 5.9
+// Temperature distribution 1.5s after a change in operating power
+
+//Operating Conditions
+
+L = .01; //[m] Metre
+Tsurr = 250+273; //[K] Temperature
+h = 1100; //[W/m^2.K] Heat Convective Coefficient
+q1 = 10^7; //[W/m^3] Volumetric Rate
+q2 = 2*10^7; //[W/m^3] Volumetric Rate
+k = 30; //[W/m.K] Conductivity
+a = 5*10^-6; //[m^2/s]
+
+delx = L/5; //Space increment for numerical solution
+Bi = h*delx/k; //Biot Number
+//By using stability criterion for Fourier Number
+Fo = (2*(1+Bi))^-1;
+//By definition
+t = Fo*delx^2/a;
+printf('\n As per stability criterion delt = %.3f s, hence setting stability limit as .3 s.',t)
+// Using Finite time increment of .3s
+delt = 1*.3;
+Fo1 = a*delt/delx^2;
+x = [0 delx delx*2 delx*3 delx*4 delx*5];
+
+//At p=0 Using equation 3.46
+for i = 1: length(x)
+T(1,i) = q1*L^2/(2*k)*(1-x(i)^2/L^2)+Tsurr + q1*L/h -273 ;
+end
+//System of Equation in Finite Difference method
+for j = 2:6
+ T(j,1)=Fo1*(2*T(j-1,2)+q2*delx^2/k) + (1 -2*Fo1)*T(j-1,1);
+ T(j,2)=Fo1*(T(j-1,1)+T(j-1,3)+q2*delx^2/k) + (1 -2*Fo1)*T(j-1,2);
+ T(j,3)=Fo1*(T(j-1,2)+T(j-1,4)+q2*delx^2/k) + (1 -2*Fo1)*T(j-1,3);
+ T(j,4)=Fo1*(T(j-1,3)+T(j-1,5)+q2*delx^2/k) + (1 -2*Fo1)*T(j-1,4);
+ T(j,5)=Fo1*(T(j-1,4)+T(j-1,6)+q2*delx^2/k) + (1 -2*Fo1)*T(j-1,5);
+ T(j,6)=2*Fo1*(T(j-1,5)+Bi*(Tsurr-273)+q2*delx^2/(2*k)) + (1 -2*Fo1-2*Bi*Fo1)*T(j-1,6);
+end
+//At p=infinity Using equation 3.46
+x = [0 delx delx*2 delx*3 delx*4 delx*5];
+for i = 1:length(x)
+T(7,i) = q2*L^2/(2*k)*(1-x(i)^2/L^2)+Tsurr+q2*L/h-273;
+end
+
+for j= 1:6
+Tans(j,:) = [j-1 delt*(j-1) T(j,:)];
+end
+
+printf("\n\n Tabulated Nodal Temperatures \n\n p t(s) T0 T1 T2 T3 T4 T5\n");
+format('v',6);
+disp(Tans);
+printf(" inf inf %.1f %.1f %.1f %.1f %.1f %.1f",T(7,1),T(7,2),T(7,3),T(7,4),T(7,5),T(7,6));
+
+//END
\ No newline at end of file diff --git a/534/CH6/EX6.1/6_1_Theoretical_Problem.sce b/534/CH6/EX6.1/6_1_Theoretical_Problem.sce new file mode 100644 index 000000000..03c38fd2a --- /dev/null +++ b/534/CH6/EX6.1/6_1_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.1 Page 355 \n')// Example 6.1
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH6/EX6.2/6_2_Napthalene_Sublimation.sce b/534/CH6/EX6.2/6_2_Napthalene_Sublimation.sce new file mode 100644 index 000000000..e8bcdb3d4 --- /dev/null +++ b/534/CH6/EX6.2/6_2_Napthalene_Sublimation.sce @@ -0,0 +1,19 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.2 Page 356 \n'); //Example 6.2
+// Napthalene Sublimation rate per unit length
+
+//Operating Conditions
+
+h = .05; //[W/m^2.K] Heat Convection coefficient
+D = .02; //[m] Diameter of cylinder
+Cas = 5*10^-6; //[kmol/m^3] Surface molar Conc
+Casurr = 0; //[kmol/m^3] Surrounding molar Conc
+Ma = 128; //[Kg/kmol] Molecular weight
+
+//From Eqn 6.15
+Na = h*(%pi*D)*(Cas-Casurr);
+na = Ma*Na;
+
+printf("\n\n Mass sublimation Rate is = %.2e kg/s.m ", na);
+//END
\ No newline at end of file diff --git a/534/CH6/EX6.3/6_3_Convection_Coefficient.sce b/534/CH6/EX6.3/6_3_Convection_Coefficient.sce new file mode 100644 index 000000000..92f162cc5 --- /dev/null +++ b/534/CH6/EX6.3/6_3_Convection_Coefficient.sce @@ -0,0 +1,18 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.3 Page 357 \n'); //Example 6.3
+// Convection Mass Transfer coefficient
+
+//Operating Conditions
+
+Dab = .288*10^-4; //[m^2/s] Table A.8 water vapor-air (319K)
+pas = .1; //[atm] Partial pressure at surface
+pasurr = .02; //[atm] Partial pressure at infinity
+y0 = .003; //[m] Tangent at y = 0 intercepts y axis at 3 mm
+
+//From Measured Vapor Pressure Distribution
+delp = (0 - pas)/(y0 - 0); //[atm/m]
+hmx = -Dab*delp/(pas - pasurr); //[m/s]
+
+printf("\n\n Convection Mass Transfer coefficient at prescribed location = %.4f m/s", hmx);
+//END
\ No newline at end of file diff --git a/534/CH6/EX6.4/6_4_Convection_Coeff_Plate.sce b/534/CH6/EX6.4/6_4_Convection_Coeff_Plate.sce new file mode 100644 index 000000000..276c4b2f0 --- /dev/null +++ b/534/CH6/EX6.4/6_4_Convection_Coeff_Plate.sce @@ -0,0 +1,37 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.4 Page 362 \n'); //Example 6.4
+// Convection Mass Transfer coefficient
+
+//Operating Conditions
+v = 1; //[m/s] Velocity of water
+L = 0.6; //[m] Plate length
+Tw1 = 300; //[K]
+Tw2 = 350; //[K]
+//Coefficients [W/m^1.5 . K]
+Clam1 = 395;
+Cturb1 = 2330;
+Clam2 = 477;
+Cturb2 = 3600;
+
+//Water Properties at T = 300K
+p1 = 997; //[kg/m^3] Density
+u1 = 855*10^-6; //[N.s/m^2] Viscosity
+//Water Properties at T = 350K
+p2 = 974; //[kg/m^3] Density
+u2 = 365*10^-6; //[N.s/m^2] Viscosity
+
+
+Rec = 5*10^5; //Transititon Reynolds Number
+xc1 = Rec*u1/(p1*v); //[m]Transition length at 300K
+xc2 = Rec*u2/(p2*v); //[m]Transition length at 350K
+
+//Integrating eqn 6.14
+//At 300 K
+h1 = [Clam1*xc1^.5/.5 + Cturb1*(L^.8-xc1^.8)/.8]/L;
+
+//At 350 K
+h2 = [Clam2*xc2^.5/.5 + Cturb2*(L^.8-xc2^.8)/.8]/L;
+
+printf("\n\n Average Convection Coefficient over the entire plate for the two temperatures at 300K = %.2f W/m^2.K and at 350K = %.2f W/m^2.K", h1,h2);
+//END
\ No newline at end of file diff --git a/534/CH6/EX6.5/6_5_Heat_flux_Plate.sce b/534/CH6/EX6.5/6_5_Heat_flux_Plate.sce new file mode 100644 index 000000000..4474214ba --- /dev/null +++ b/534/CH6/EX6.5/6_5_Heat_flux_Plate.sce @@ -0,0 +1,24 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.5 Page 372 \n'); //Example 6.5
+// Heat Flux to blade when surface temp is reduced
+// Heat flux to a larger turbine blade
+
+//Operating Conditions
+v = 160; //[m/s] Velocity of air
+L = 0.04; //[m] Blade length
+Tsurr = 1150+273; //[K]
+Ts = 800+273; //[K] Surface Temp
+q = 95000; //[W/m^2] Original heat flux
+
+//Case 1
+Ts1 = 700+273; //[K] Surface Temp
+q1 = q*(Tsurr-Ts1)/(Tsurr-Ts);
+
+//Case 2
+L2 = .08; //[m] Length
+q2 = q*L/L2; //[W/m^2] Heat flux
+
+
+printf("\n\n (a) Heat Flux to blade when surface temp is reduced = %i KW/m^2 \n (b) Heat flux to a larger turbine blade = %.2f KW/m^2", q1/1000,q2/1000);
+//END
\ No newline at end of file diff --git a/534/CH6/EX6.6/6_6_Molar_flux_Plate.sce b/534/CH6/EX6.6/6_6_Molar_flux_Plate.sce new file mode 100644 index 000000000..8557b8d8f --- /dev/null +++ b/534/CH6/EX6.6/6_6_Molar_flux_Plate.sce @@ -0,0 +1,36 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.6 Page 379 \n'); //Example 6.6
+// Water vapor conc and flux associated with the same location on larger surface of the same shape
+
+//Operating Conditions
+v = 100; //[m/s] Velocity of air
+Tsurr = 20+273; //[K] Surrounding Air Temperature
+L1 = 1; //[m] solid length
+Ts = 80+273; //[K] Surface Temp
+qx = 10000; //[W/m^2] heat flux at a point x
+Txy = 60+273; //[K] Temp in boundary layer above the point
+
+//Table A.4 Air Properties at T = 323K
+v = 18.2*10^-6; //[m^2/s] Viscosity
+k = 28*10^-3; //[W/m.K] Conductivity
+Pr = 0.7; //Prandttl Number
+//Table A.6 Saturated Water Vapor at T = 323K
+pasat = 0.082; //[kg/m^3]
+Ma = 18; //[kg/kmol] Molecular mass of water vapor
+//Table A.8 Water Vapor-air at T = 323K
+Dab = .26*10^-4; //[m^2/s]
+
+//Case 1
+Casurr = 0;
+Cas = pasat/Ma; //[kmol/m^3] Molar conc of saturated water vapor at surface
+Caxy = Cas + (Casurr - Cas)*(Txy - Ts)/(Tsurr - Ts);
+
+//Case 2
+L2 = 2;
+hm = L1/L2*Dab/k*qx/(Ts-Tsurr);
+Na = hm * (Cas - Casurr);
+
+
+printf("\n (a) Water vapor Concentration above the point = %.4f Kmol/m^3 \n (b) Molar flux to a larger surface = %.2e Kmol/s.m^2", Caxy,Na);
+//END
\ No newline at end of file diff --git a/534/CH6/EX6.7/6_7_Evaporative_Cooling.sce b/534/CH6/EX6.7/6_7_Evaporative_Cooling.sce new file mode 100644 index 000000000..d9ce18e61 --- /dev/null +++ b/534/CH6/EX6.7/6_7_Evaporative_Cooling.sce @@ -0,0 +1,26 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 6.7 Page 383 \n'); //Example 6.7
+// Steady State Temperature of Beverage
+
+//Operating Conditions
+Tsurr = 40+273; //[K] Surrounding Air Temperature
+//Volatile Wetting Agent A
+hfg = 100; //[kJ/kg]
+Ma = 200; //[kg/kmol] Molecular mass
+pasat = 5000; //[N/m^2] Saturate pressure
+Dab = .2*10^-4; //[m^2/s] Diffusion coefficient
+
+//Table A.4 Air Properties at T = 300K
+p = 1.16; //[kg/m^3] Density
+cp = 1.007; //[kJ/kg.K] Specific Heat
+alpha = 22.5*10^-6; //[m^2/s]
+R = 8.314; //[kJ/kmol] Universal Gas Constt
+
+//Applying Eqn 6.65 and setting pasurr = 0
+// Ts^2 - Tsurr*Ts + B = 0 , where the coefficient B is
+B = Ma*hfg*pasat*10^-3/[R*p*cp*(alpha/Dab)^(2/3)];
+Ts = [Tsurr + sqrt(Tsurr^2 - 4*B)]/2;
+
+printf("\n Steady State Surface Temperature of Beverage = %.1f degC", Ts-273);
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.1/7_1_Cooling_rate.sce b/534/CH7/EX7.1/7_1_Cooling_rate.sce new file mode 100644 index 000000000..cfb77c486 --- /dev/null +++ b/534/CH7/EX7.1/7_1_Cooling_rate.sce @@ -0,0 +1,28 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.1 Page 415 \n'); //Example 7.1
+// Cooling rate per Unit Width of the Plate
+
+//Operating Conditions
+v = 10; //[m/s] Air velocity
+p = 6000; //[N/m^2] Air pressure
+Tsurr = 300+273; //[K] Surrounding Air Temperature
+L = .5; //[m] Length of plate
+Ts = 27+273; //[K] Surface Temp
+
+//Table A.4 Air Properties at T = 437K
+uv = 30.84*10^-6*(101325/6000); //[m^2/s] Kinematic Viscosity at P = 6000 N/m^2
+k = 36.4*10^-3; //[W/m.K] Thermal COnductivity
+Pr = .687; //Prandtl number
+
+Re = v*L/uv; //Reynolds number
+printf("\n Since Reynolds Number is %i, The flow is laminar over the entire plate",Re);
+
+//Correlation 7.30
+NuL = .664*Re^.5*Pr^.3334; //Nusselt Number over entire plate length
+hL = NuL*k/L; // Average Convection Coefficient
+//Required cooling rate per unit width of plate
+q = hL*L*(Tsurr-Ts);
+
+printf("\n\n Required cooling rate per unit width of plate = %i W/m", q);
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.2/7_2_Turb_over_Plate.sce b/534/CH7/EX7.2/7_2_Turb_over_Plate.sce new file mode 100644 index 000000000..9833317a7 --- /dev/null +++ b/534/CH7/EX7.2/7_2_Turb_over_Plate.sce @@ -0,0 +1,53 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.2 Page 417 \n'); //Example 7.2
+// Maximum Heater Power Requirement
+
+//Operating Conditions
+v = 60; //[m/s] Air velocity
+Tsurr = 25+273; //[K] Surrounding Air Temperature
+w = 1; //[m] Width of plate
+L = .05; //[m] Length of stripper
+Ts = 230+273; //[K] Surface Temp
+
+//Table A.4 Air Properties at T = 400K
+uv = 26.41*10^-6; //[m^2/s] Kinematic Viscosity
+k = .0338; //[W/m.K] Thermal COnductivity
+Pr = .690; //Prandtl number
+
+Re = v*L/uv; //Reynolds number
+
+Rexc = 5*10^5; //Transition Reynolds Number
+xc = uv*Rexc/v; //Transition Length
+printf("\n Reynolds Number based on length L = .05m is %i. \n And the transition occur at xc = %.2f m ie fifth plate",Re,xc);
+
+//For first heater
+//Correlation 7.30
+Nu1 = .664*Re^.5*Pr^.3334; //Nusselt Number
+h1 = Nu1*k/L; // Average Convection Coefficient
+q1 = h1*(L*w)*(Ts-Tsurr); // Convective Heat exchange
+
+//For first four heaters
+Re4 = 4*Re;
+L4 = 4*L;
+Nu4 = .664*Re4^.5*Pr^.3334; //Nusselt Number
+h4 = Nu4*k/L4; // Average Convection Coefficient
+
+//For Fifth heater from Eqn 7.38
+Re5 = 5*Re;
+A = 871;
+L5 = 5*L;
+Nu5 = (.037*Re5^.8-A)*Pr^.3334; //Nusselt Number
+h5 = Nu5*k/L5; // Average Convection Coefficient
+q5 = (h5*L5-h4*L4)*w*(Ts-Tsurr);
+
+//For Sixth heater from Eqn 7.38
+Re6 = 6*Re;
+L6 = 6*L;
+Nu6 = (.037*Re6^.8-A)*Pr^.3334 ; //Nusselt Number
+h6 = Nu6*k/L6 ; // Average Convection Coefficient
+q6 = (h6*L6-h5*L5)*w*(Ts-Tsurr);
+
+printf("\n\n Power requirement are \n qconv1 = %i W qconv5 = %i W qconv6 = %i W", q1,q5,q6);
+printf("\n Hence %i > %i > %i and the sixth plate has largest power requirement", q6,q1,q5);
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.3/7_3_Daily_water_loss.sce b/534/CH7/EX7.3/7_3_Daily_water_loss.sce new file mode 100644 index 000000000..aa0dd4c4b --- /dev/null +++ b/534/CH7/EX7.3/7_3_Daily_water_loss.sce @@ -0,0 +1,37 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.3 Page 417 \n'); //Example 7.2
+// Daily Water Loss
+
+//Operating Conditions
+v = 2; //[m/s] Air velocity
+Tsurr = 25+273; //[K] Surrounding Air Temperature
+H = .5; // Humidity
+w = 6; //[m] Width of pool
+L1 = 12; //[m] Length of pool
+e = 1.5; //[m] Deck Wide
+Ts = 25+273; //[K] Surface Temp of water
+
+//Table A.4 Air Properties at T = 298K
+uv = 15.7*10^-6; //[m^2/s] Kinematic Viscosity
+//Table A.8 Water vapor-Air Properties at T = 298K
+Dab = .26*10^-4; //[m^2/s] Diffusion Coefficient
+Sc = uv/Dab;
+//Table A.6 Air Properties at T = 298K
+rho = .0226; //[kg/m^3]
+
+L = L1+e;
+Re = v*L/uv; //Reynolds number
+
+//Equation 7.41 yields
+ShLe = .037*Re^.8*Sc^.3334;
+//Equation 7.44
+p = 8; //Turbulent Flow
+ShL = (L/(L-e))*ShLe*[1-(e/L)^((p+1)/(p+2))]^(p/(p+1));
+
+hmL = ShL*(Dab/L);
+n = hmL*(L1*w)*rho*(1-H);
+
+printf("\n Reynolds Number is %.2e. Hence for turbulent Flow p = 8 in Equation 7.44.\n Daily Water Loss due to evaporation is %i kg/day",Re,n*86400);
+
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.4/7_4_Zukauskas_Correlation.sce b/534/CH7/EX7.4/7_4_Zukauskas_Correlation.sce new file mode 100644 index 000000000..3e80499cc --- /dev/null +++ b/534/CH7/EX7.4/7_4_Zukauskas_Correlation.sce @@ -0,0 +1,36 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.4 Page 428 \n'); //Example 7.4
+// Convection Coefficient associated with operating conditions
+// Convection Coefficient from an appropriate correlation
+
+//Operating Conditions
+v = 10; //[m/s] Air velocity
+Tsurr = 26.2+273; //[K] Surrounding Air Temperature
+P = 46; // [W] Power dissipation
+L = .094; //[m] Length of cylinder
+D = .0127; //[m] Diameter of cylinder
+Ts = 128.4+273; //[K] Surface Temp of water
+q = 46-.15*46; //[W] Actual power dissipation without the 15% loss
+
+//Table A.4 Air Properties at T = 300K
+uv = 15.89*10^-6; //[m^2/s] Kinematic Viscosity
+k = 26.3*10^-3; //[W/m.K] Thermal conductivity
+Pr = .707; //Prandtl Number
+//Table A.4 Air Properties at T = 401K
+Prs = .690; //Prandtl Number
+
+A = %pi*D*L;
+h = q/(A*(Ts-Tsurr));
+
+Re = v*D/uv; //Reynolds number
+//Using Zukauskas Relation, Equation 7.53
+C = .26;
+m = .6;
+n = .37;
+Nu = C*Re^m*Pr^n*(Pr/Prs)^.25;
+havg = Nu*k/D;
+
+printf("\n Convection Coefficient associated with operating conditions %i W/m^2.K. \n Reynolds Number is %i. Hence taking suitable corresponding data from Table 7.4.\n Convection Coefficient from an appropriate Zukauskas correlation %i W/m^2.K",h,Re,havg);
+
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.5/7_5_Hydrogen_fuel_cell.sce b/534/CH7/EX7.5/7_5_Hydrogen_fuel_cell.sce new file mode 100644 index 000000000..3f8208c16 --- /dev/null +++ b/534/CH7/EX7.5/7_5_Hydrogen_fuel_cell.sce @@ -0,0 +1,32 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.5 Page 431 \n'); //Example 7.5
+// Convective Heat transfer to the canister and the additional heating needed
+
+//Operating Conditions
+v = 23; //[m/s] Air velocity
+Tsurr = 296; //[K] Surrounding Air Temperature
+L = .8; //[m] Length of cylinder
+Di = .1; //[m] Diameter of cylinder
+t = .005; //[m] Thickness of cylinder
+
+//Table A.4 Air Properties at T = 285K
+uv = 14.56*10^-6; //[m^2/s] Kinematic Viscosity
+k = 25.2*10^-3; //[W/m.K] Thermal conductivity
+Pr = .712; //Prandtl Number
+//Table A.1 AISI 316 Stainless steel Properties at T = 300K
+kss = 13.4; //[W/m.K]Conductivity
+
+pH2 = 1.01; //[N]
+Ti = -3550/(2.30*log10(pH2) - 12.9);
+Eg = -(1.35*10^-4)*(29.5*10^6);
+
+Re = v*(Di+2*t)/uv; //Reynolds number
+// Equation 7.54
+Nu = .3+.62*Re^.5*Pr^.3334/[1+(.4/Pr)^.6668]^.25*[1+(Re/282000)^(5/8)]^.8;
+h = Nu*k/(Di+2*t);
+
+qconv = (Tsurr-Ti)/[(1/(%pi*L*(Di+2*t)*h))+(2.30*log10((Di+2*t)/Di)/(2*%pi*kss*L))];
+printf("\n Additional Thermal Energy must be supplied to canister to mainatin steady-state operating temperatue %i W",-qconv-Eg);
+
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.6/7_6_Plastic_Film.sce b/534/CH7/EX7.6/7_6_Plastic_Film.sce new file mode 100644 index 000000000..c36cf4224 --- /dev/null +++ b/534/CH7/EX7.6/7_6_Plastic_Film.sce @@ -0,0 +1,35 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.6 Page 434 \n'); //Example 7.6
+// Time required to cool from Ti = 75 degC to 35 degC
+
+//Operating Conditions
+v = 10; //[m/s] Air velocity
+Tsurr = 23+273; //[K] Surrounding Air Temperature
+D = .01; //[m] Diameter of sphere
+Ti = 75+273; //[K] Initial temp
+Tt = 35+273; //[K] Temperature after time t
+p = 1; //[atm]
+
+//Table A.1 Copper at T = 328K
+rho = 8933; //[kg/m^3] Density
+k = 399; //[W/m.K] Conductivity
+cp = 388; //[J/kg.K] specific
+//Table A.4 Air Properties T = 296 K
+u = 182.6*10^-7; //[N.s/m^2] Viscosity
+uv = 15.53*10^-6; //[m^2/s] Kinematic Viscosity
+k = 25.1*10^-3; //[W/m.K] Thermal conductivity
+Pr = .708; //Prandtl Number
+//Table A.4 Air Properties T = 328 K
+u2 = 197.8*10^-7; //[N.s/m^2] Viscosity
+
+Re = v*D/uv; //Reynolds number
+//Using Equation 7.56
+Nu = 2+(0.4*Re^.5 + 0.06*Re^.668)*Pr^.4*(u/u2)^.25;
+h = Nu*k/D;
+//From equation 5.4 and 5.5
+t = rho*cp*D*2.30*log10((Ti-Tsurr)/(Tt-Tsurr))/(6*h);
+
+printf("\nTime required for cooling is %.1f sec",t);
+
+//END
\ No newline at end of file diff --git a/534/CH7/EX7.7/7_7_Staggered_Arrangement.sce b/534/CH7/EX7.7/7_7_Staggered_Arrangement.sce new file mode 100644 index 000000000..aebb758cc --- /dev/null +++ b/534/CH7/EX7.7/7_7_Staggered_Arrangement.sce @@ -0,0 +1,57 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 7.7 Page 443 \n'); //Example 7.7
+// Air side Convection coefficient and Heat rate
+// pressure Drop
+
+//Operating Conditions
+v = 6; //[m/s] Air velocity
+Tsurr = 15+273; //[K] Surrounding Air Temperature
+D = .0164; //[m] Diameter of tube
+Ts = 70+273; //[K] Temp of tube
+//Staggered arrangement dimensions
+St = .0313; //[m]
+Sl = .0343; //[m]
+
+//Table A.4 Air Properties T = 288 K
+rho = 1.217; //[kg/m^3] Density
+cp = 1007; //[J/kg.K] specific heat
+uv = 14.82*10^-6; //[m^2/s] Kinematic Viscosity
+k = 25.3*10^-3; //[W/m.K] Thermal conductivity
+Pr = .71; //Prandtl Number
+//Table A.4 Air Properties T = 343 K
+Pr2 = .701; //Prandtl Number
+//Table A.4 Air Properties T = 316 K
+uv3 = 17.4*10^-6; //[m^2/s] Kinematic Viscosity
+k3 = 27.4*10^-3; //[W/m.K] Thermal conductivity
+Pr3 = .705; //Prandtl Number
+
+Sd = [Sl^2 + (St/2)^2]^.5;
+Vmax = St*v/(St-D);
+
+Re = Vmax*D/uv; //Reynolds number
+
+C = .35*(St/Sl)^.2;
+m = .6;
+C2 = .95;
+N = 56;
+Nt = 8;
+//Using Equation 7.64 & 7.65
+Nu = C2*C*Re^m*Pr^.36*(Pr/Pr2)^.25;
+h = Nu*k/D;
+
+//From Eqnn 7.67
+Tso = (Ts-Tsurr)*exp(-(%pi*D*N*h)/(rho*v*Nt*St*cp));
+Tlm = ((Ts-Tsurr) - Tso)/(2.30*log10((Ts-Tsurr)/Tso));
+q = N*(h*%pi*D*Tlm);
+
+Pt = St/D;
+//From Fig 7.14
+X = 1.04;
+f = .35;
+NL = 7;
+press = NL*X*(rho*Vmax^2/2)*f;
+
+printf("\n Air side Convection coefficient h = %.1f W/m^2.k and Heat rate q = %.1f kW/m \n Pressure Drop = %.2e bars",h,q/1000,press/100000);
+
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.1/8_1_Theoretical_Problem.sce b/534/CH8/EX8.1/8_1_Theoretical_Problem.sce new file mode 100644 index 000000000..0b95efe7a --- /dev/null +++ b/534/CH8/EX8.1/8_1_Theoretical_Problem.sce @@ -0,0 +1,8 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.1 Page 494 \n')// Example 8.1
+//Theoretical Problem
+
+printf('\n The given example is theoretical and does not involve any numerical computation')
+
+//End
diff --git a/534/CH8/EX8.2/8_2_Internal_flow.sce b/534/CH8/EX8.2/8_2_Internal_flow.sce new file mode 100644 index 000000000..3ad632e03 --- /dev/null +++ b/534/CH8/EX8.2/8_2_Internal_flow.sce @@ -0,0 +1,25 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.2 Page 499 \n'); //Example 8.2
+// Length of tube needed to achieve the desired outlet temperature
+//Local convection coefficient at the outlet
+
+//Operating Conditions
+m = .1; //[kg/s] mass flow rate of water
+Ti = 20+273; //[K] Inlet temp
+To = 60+273; //[K] Outlet temperature
+Di = .02; //[m] Inner Diameter
+Do = .04; //[m] Outer Diameter
+q = 10^6; //[w/m^3] Heat generation Rate
+Tsi = 70+273; //[K] Inner Surface Temp
+//Table A.4 Air Properties T = 313 K
+cp = 4179; //[J/kg.K] specific heat
+
+L = 4*m*cp*(To-Ti)/(%pi*(Do^2-Di^2)*q);
+
+//From Newtons Law of cooling, Equation 8.27, local heat convection coefficient is
+h = q*(Do^2-Di^2)/(Di*4*(Tsi-To));
+
+printf("\n Length of tube needed to achieve the desired outlet temperature = %.1f m \n Local convection coefficient at the outlet = %i W/m^2.K",L,h);
+
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.3/8_3_Internal_flow_steam.sce b/534/CH8/EX8.3/8_3_Internal_flow_steam.sce new file mode 100644 index 000000000..e4f290563 --- /dev/null +++ b/534/CH8/EX8.3/8_3_Internal_flow_steam.sce @@ -0,0 +1,23 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.3 Page 503 \n'); //Example 8.3
+// average convection coefficient
+
+//Operating Conditions
+m = .25; //[kg/s] mass flow rate of water
+Ti = 15+273; //[K] Inlet temp
+To = 57+273; //[K] Outlet temperature
+D = .05; //[m] Diameter
+L = 6; //[m] Length of tube
+Ts = 100+273; //[K] outer Surface Temp
+
+//Table A.4 Air Properties T = 309 K
+cp = 4178; //[J/kg.K] specific heat
+
+Tlm = ((Ts-To)-(Ts-Ti))/(2.30*log10((100-57)/(100-15)));
+
+h = m*cp*(To-Ti)/(%pi*D*L*Tlm);
+
+printf("\n Average Heat transfer Convection Coefficient = %i W/m^2.K",h);
+
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.4/8_4_Solar_Energy.sce b/534/CH8/EX8.4/8_4_Solar_Energy.sce new file mode 100644 index 000000000..2dae80a47 --- /dev/null +++ b/534/CH8/EX8.4/8_4_Solar_Energy.sce @@ -0,0 +1,35 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.4 Page 506 \n'); //Example 8.4
+// Length of tube for required heating
+// Surface temperature Ts at outlet section
+
+//Operating Conditions
+m = .01; //[kg/s] mass flow rate of water
+Ti = 20+273; //[K] Inlet temp
+To = 80+273; //[K] Outlet temperature
+D = .06; //[m] Diameter
+q = 2000; //[W/m^2] Heat flux to fluid
+
+//Table A.4 Air Properties T = 323 K
+cp = 4178; //[J/kg.K] specific heat
+//Table A.4 Air Properties T = 353 K
+k = .670; //[W/m] Thermal Conductivity
+u = 352*10^-6; //[N.s/m^2] Viscosity
+Pr = 2.2; //Prandtl Number
+cp = 4178; //[J/kg.K] specific heat
+
+L = m*cp*(To-Ti)/(%pi*D*q);
+
+//Using equation 8.6
+Re = m*4/(%pi*D*u);
+printf("\n (a) Length of tube for required heating = %.2f m\n\n (b)As Reynolds Number is %i. The flow is laminar.",L,Re);
+
+Nu = 4.364; //Nusselt Number
+h = Nu*k/D; //[W/m^2.K] Heat convection Coefficient
+
+Ts = q/h+To; //[K]
+
+printf("\n Surface Temperature at tube outlet = %i degC",Ts-273);
+
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.5/8_5_Blood_Artery.sce b/534/CH8/EX8.5/8_5_Blood_Artery.sce new file mode 100644 index 000000000..ce381e771 --- /dev/null +++ b/534/CH8/EX8.5/8_5_Blood_Artery.sce @@ -0,0 +1,52 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.5 Page 509 \n'); //Example 8.5
+// Length of Blood Vessel
+
+//Operating Conditions
+um1 = .13; //[m/s] Blood stream
+um2 = 3*10^-3; //[m/s] Blood stream
+um3 = .7*10^-3; //[m/s] Blood stream
+D1 = .003; //[m] Diameter
+D2 = .02*10^-3; //[m] Diameter
+D3 = .008*10^-3; //[m] Diameter
+Tlm = .05;
+kf = .5; //[W/m.K] Conductivity
+//Table A. Water Properties T = 310 K
+rho = 993; //[kg/m^3] density
+cp = 4178; //[J/kg.K] specific heat
+u = 695*10^-6; //[N.s/m^2] Viscosity
+kb = .628; //[W/m.K] Conductivity
+Pr = 4.62; //Prandtl Number
+i=1;
+//Using equation 8.6
+ Re1 = rho*um1*D1/u;
+ Nu = 4;
+ hb = Nu*kb/D1;
+ hf = kf/D1;
+ U1 = (1/hb + 1/hf)^-1;
+ L1 = -rho*um1*D1/U1*cp*2.303*log10(Tlm)/4;
+ xfdh1 = .05*Re1*D1;
+ xfdr1 = xfdh1*Pr;
+
+ Re2 = rho*um2*D2/u;
+ Nu = 4;
+ hb = Nu*kb/D2;
+ hf = kf/D2;
+ U2 = (1/hb + 1/hf)^-1;
+ L2 = -rho*um2*D2/U2*cp*2.303*log10(Tlm)/4;
+ xfdh2 = .05*Re2*D2;
+ xfdr2 = xfdh2*Pr;
+
+ Re3 = rho*um3*D3/u;
+ Nu = 4;
+ hb = Nu*kb/D3;
+ hf = kf/D3;
+ U3 = (1/hb + 1/hf)^-1;
+ L3 = -rho*um3*D3/U3*cp*2.303*log10(Tlm)/4;
+ xfdh3 = .05*Re3*D3;
+ xfdr3 = xfdh3*Pr;
+
+printf("\n Vessel Re U(W/m^2.K) L(m) xfdh(m) xfdr(m)\n Artery %i %i %.1f %.2f %.1f \n Anteriole %.3f %i %.1e %.1e %.1e \n Capillary %.3f %i %.1e %.1e %.1e",Re1,U1,L1,xfdh1,xfdr1,Re2,U2,L2,xfdh2,xfdr2,Re3,U3,L3,xfdh3,xfdr3);
+
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.6/8_6_Metal_Duct.sce b/534/CH8/EX8.6/8_6_Metal_Duct.sce new file mode 100644 index 000000000..6c3fb77ef --- /dev/null +++ b/534/CH8/EX8.6/8_6_Metal_Duct.sce @@ -0,0 +1,37 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.6 Page 516 \n'); //Example 8.6
+// Heat Loss from the Duct over the Length L, q
+// Heat flux and suface temperature at x=L
+
+//Operating Conditions
+m = .05; //[kg/s] mass flow rate of water
+Ti = 103+273; //[K] Inlet temp
+To = 77+273; //[K] Outlet temperature
+D = .15; //[m] Diameter
+L = 5; //[m] length
+ho = 6; //[W/m^2.K] Heat transfer convective coefficient
+Tsurr = 0+273; //[K] Temperature of surrounding
+
+//Table A.4 Air Properties T = 363 K
+cp = 1010; //[J/kg.K] specific heat
+//Table A.4 Air Properties T = 350 K
+k = .030; //[W/m] Thermal Conductivity
+u = 20.82*10^-6; //[N.s/m^2] Viscosity
+Pr = .7; //Prandtl Number
+
+q = m*cp*(To-Ti);
+
+Re = m*4/(%pi*D*u);
+printf("\n As Reynolds Number is %i. The flow is Turbulent.",Re);
+
+//Equation 8.6
+n = 0.3;
+Nu = .023*Re^.8*Pr^.3;
+h = Nu*k/D;
+q2 = (To-Tsurr)/[1/h + 1/ho];
+Ts = -q2/h+To;
+
+printf("\n\n Heat Loss from the Duct over the Length L, q = %i W \n Heat flux and suface temperature at x=L is %.1f W/m^2 & %.1f degC respectively",q,q2,Ts-273);
+
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.7/8_7_Microchannel.sce b/534/CH8/EX8.7/8_7_Microchannel.sce new file mode 100644 index 000000000..3cf5ee7f2 --- /dev/null +++ b/534/CH8/EX8.7/8_7_Microchannel.sce @@ -0,0 +1,57 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.7 Page 525 \n'); //Example 8.5
+// Time needed to bring the reactants to within 1 degC of processing temperature
+
+//Operating Conditions
+T1 = 125+273; //[K] Chip Temperature 1
+T2 = 25+273; //[K] Chip Temperature 2
+Ti = 5+273; //[K] Inlet Temperature
+D = .01; //[m] Diameter
+L = .02; //[m] length
+delP = 500*10^3; //[N/m^2] Pressure drop
+//Dimensions
+a = 40*10^-6;
+b = 160*10^-6;
+s = 40*10^-6;
+
+//Table A.5 Ethylene Glycol Properties T = 288 K
+rho = 1120.2; //[kg/m^3] Density
+cp = 2359; //[J/kg.K] Specific Heat
+u = 2.82*10^-2; //[N.s/m^2] Viscosity
+k = 247*10^-3; //[W/m.K] Thermal Conductivity
+Pr = 269; //Prandtl number
+//Table A.5 Ethylene Glycol Properties T = 338 K
+rho2 = 1085; //[kg/m^3] Density
+cp2 = 2583; //[J/kg.K] Specific Heat
+u2 = .427*10^-2; //[N.s/m^2] Viscosity
+k2 = 261*10^-3; //[W/m.K] Thermal Conductivity
+Pr2 = 45.2; //Prandtl number
+
+P = 2*a+2*b; //Perimeter of microchannel
+Dh = 4*a*b/P; //Hydraulic Diameter
+
+um2 = 2/73*Dh^2/u2*delP/L; //[[m/s] Equation 8.22a
+Re2 = um2*Dh*rho2/u2; //Reynolds Number
+xfdh2 = .05*Dh*Re2; //[m] From Equation 8.3
+xfdr2 = xfdh2*Pr2; //[m] From Equation 8.23
+m2 = rho2*a*b*um2; //[kg/s]
+Nu2 = 4.44; //Nusselt Number from Table 8.1
+h2 = Nu2*k2/Dh; //[W/m^2.K] Convection Coeff
+Tc2 = 124+273; //[K]
+xc2 = m2/P*cp2/h2*2.303*log10((T1-Ti)/(T1-Tc2));
+tc2 = xc2/um2;
+
+um = 2/73*Dh^2/u*delP/L; //[[m/s] Equation 8.22a
+Re = um*Dh*rho/u; //Reynolds Number
+xfdh = .05*Dh*Re; //[m] From Equation 8.3
+xfdr = xfdh*Pr; //[m] From Equation 8.23
+m = rho2*a*b*um; //[kg/s]
+Nu = 4.44; //Nusselt Number from Table 8.1
+h = Nu*k/Dh; //[W/m^2.K] Convection Coeff
+Tc = 24+273; //[K]
+xc = m/P*cp/h*2.303*log10((T2-Ti)/(T2-Tc));
+tc = xc/um;
+
+printf("\n Temp [degC] %i %i\n\n Flow rate [m/s] %.3f %.3f\n Reynolds Number %.1f %.1f\n Hydrodynamic entrance Length [m] %.1e %.1e\n Thermal entrance Length [m] %.1e %.1e\n Mass Flow rate [kg/s] %.2e %.2e\n Convective Coeff [W/m^2.K] %.2e %.2e\n Transition Length [m] %.2e %.2e\n Required Time [s] %.3f %.3f",T2-273,T1-273,um,um2,Re,Re2,xfdh,xfdh2,xfdr,xfdr2,m,m2,h,h2,xc,xc2,tc,tc2);
+//END
\ No newline at end of file diff --git a/534/CH8/EX8.8/8_8_Ammonia_tube.sce b/534/CH8/EX8.8/8_8_Ammonia_tube.sce new file mode 100644 index 000000000..608bca238 --- /dev/null +++ b/534/CH8/EX8.8/8_8_Ammonia_tube.sce @@ -0,0 +1,27 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 8.8 Page 529 \n'); //Example 8.8
+// Average mass trasnfer convection coefficient for the tube
+
+//Operating Conditions
+m = .0003; //[kg/s] mass flow rate of water
+T = 25+273; //[K] Temperature of surrounding and tube
+D = .01; //[m] Diameter
+L = 1; //[m] length
+
+//Table A.4 Air Properties T = 298 K
+uv = 15.7*10^-6; //[m^2/s] Kinematic Viscosity
+u = 18.36*10^-6; //[N.s/m^2] Viscosity
+//Table A.8 Ammonia-Air Properties T = 298 K
+Dab = .28*10^-4; //[m^2/s] Diffusion coeff
+Sc = .56;
+
+Re = m*4/(%pi*D*u);
+printf("\n As Reynolds Number is %i. The flow is Laminar.",Re);
+
+//Using Equation 8.57
+Sh = 1.86*(Re*Sc*D/L)^.3334;
+h = Sh*Dab/D;
+printf("\n Average mass trasnfer convection coefficient for the tube %.3f m/s",h);
+
+//END
\ No newline at end of file diff --git a/534/CH9/EX9.1/9_1_Vertical_Plate.sce b/534/CH9/EX9.1/9_1_Vertical_Plate.sce new file mode 100644 index 000000000..5030e4211 --- /dev/null +++ b/534/CH9/EX9.1/9_1_Vertical_Plate.sce @@ -0,0 +1,27 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 9.1 Page 569 \n'); //Example 9.1
+// Boundary Layer thickness at trailing edge.
+
+//Operating Conditions
+Ts = 70+273; //[K] Surface Temperature
+Tsurr = 25+273; //[K] Surrounding Temperature
+v1 = 0; //[m/s] Velocity of free air
+v2 = 5; //[m/s] Velocity of free air
+L = .25; //[m] length
+
+//Table A.4 Air Properties T = 320 K
+uv = 17.95*10^-6; //[m^2/s] Kinematic Viscosity
+be = 3.12*10^-3; //[K^-1] Tf^-1
+Pr = 269; // Prandtl number
+g = 9.81; //[m^2/s]gravitational constt
+
+Gr = g*be*(Ts-Tsurr)*L^3/uv^2;
+del = 6*L/(Gr/4)^.25;
+printf("\n Boundary Layer thickness at trailing edge for no air stream %.3f m",del);
+
+Re = v2*L/uv;
+printf("\n\n For air stream at 5 m/s As the Reynolds Number is %.2e the free convection boundary layer is Laminar",Re);
+del2 = 5*L/(Re)^.5;
+printf("\n Boundary Layer thickness at trailing edge for air stream at 5 m/s is %.4f m",del2);
+//END
\ No newline at end of file diff --git a/534/CH9/EX9.2/9_2_Glass_door.sce b/534/CH9/EX9.2/9_2_Glass_door.sce new file mode 100644 index 000000000..b0fb82b80 --- /dev/null +++ b/534/CH9/EX9.2/9_2_Glass_door.sce @@ -0,0 +1,28 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 9.2 Page 572 \n'); //Example 9.2
+// Heat transfer by convection between screen and room air.
+
+//Operating Conditions
+Ts = 232+273; //[K] Surface Temperature
+Tsurr = 23+273; //[K] Surrounding Temperature
+L = .71; //[m] length
+w = 1.02; //[m] Width
+
+//Table A.4 Air Properties T = 400 K
+k = 33.8*10^-3 ;//[W/m.K]
+uv = 26.4*10^-6 ;//[m^2/s] Kinematic Viscosity
+al = 38.3*10^-6 ;//[m^2/s]
+be = 2.5*10^-3 ;//[K^-1] Tf^-1
+Pr = .69 ;// Prandtl number
+g = 9.81 ;//[m^2/s] gravitational constt
+
+Ra = g*be*(Ts-Tsurr)/al*L^3/uv;
+printf("\n\n As the Rayleigh Number is %.2e the free convection boundary layer is turbulent",Ra);
+//From equatiom 9.23
+Nu = [.825 + .387*Ra^.16667/[1+(.492/Pr)^(9/16)]^(8/27)]^2;
+h = Nu*k/L;
+q = h*L*w*(Ts-Tsurr);
+
+printf("\n Heat transfer by convection between screen and room air is %i W",q);
+//END
\ No newline at end of file diff --git a/534/CH9/EX9.3/9_3_Rectangular_Duct.sce b/534/CH9/EX9.3/9_3_Rectangular_Duct.sce new file mode 100644 index 000000000..587ded94a --- /dev/null +++ b/534/CH9/EX9.3/9_3_Rectangular_Duct.sce @@ -0,0 +1,35 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 9.3 Page 577 \n'); //Example 9.3
+// Heat Loss from duct per meter of length
+
+//Operating Conditions
+Ts = 45+273; //[K] Surface Temperature
+Tsurr = 15+273 ;//[K] Surrounding Temperature
+H = .3 ;//[m] Height
+w = .75 ;//[m] Width
+
+//Table A.4 Air Properties T = 303 K
+k = 26.5*10^-3 ;//[W/m.K]
+uv = 16.2*10^-6 ;//[m^2/s] Kinematic Viscosity
+al = 22.9*10^-6 ;//[m^2/s] alpha
+be = 3.3*10^-3 ;//[K^-1] Tf^-1
+Pr = .71 ;// Prandtl number
+g = 9.81 ;//[m^2/s] gravitational constt
+
+Ra = g*be*(Ts-Tsurr)/al*H^3/uv; //Length = Height
+//From equatiom 9.27
+Nu = [.68 + .67*Ra^.25/[1+(.492/Pr)^(9/16)]^(4/9)];
+//for Sides
+hs = Nu*k/H;
+
+Ra2 = g*be*(Ts-Tsurr)/al*(w/2)^3/uv; //Length = w/2
+//For top eq 9.31
+ht = [k/(w/2)]*.15*Ra2^.3334;
+//For bottom Eq 9.32
+hb = [k/(w/2)]*.27*Ra2^.25;
+
+q = (2*hs*H+ht*w+hb*w)*(Ts-Tsurr);
+
+printf("\n Rate of heat loss per unit length of duct is %i W/m",q);
+//END
\ No newline at end of file diff --git a/534/CH9/EX9.4/9_4_Steam_Pipe.sce b/534/CH9/EX9.4/9_4_Steam_Pipe.sce new file mode 100644 index 000000000..4653eb1cd --- /dev/null +++ b/534/CH9/EX9.4/9_4_Steam_Pipe.sce @@ -0,0 +1,30 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 9.4 Page 580 \n'); //Example 9.4
+// Heat Loss from pipe per meter of length
+
+//Operating Conditions
+Ts = 165+273; //[K] Surface Temperature
+Tsurr = 23+273; //[K] Surrounding Temperature
+D = .1 ;//[m] Diameter
+e = .85 ;// emissivity
+stfncnstt=5.67*10^(-8) ;// [W/m^2.K^4] - Stefan Boltzmann Constant
+
+//Table A.4 Air Properties T = 303 K
+k = 31.3*10^-3 ;//[W/m.K] Conductivity
+uv = 22.8*10^-6 ;//[m^2/s] Kinematic Viscosity
+al = 32.8*10^-6 ;//[m^2/s] alpha
+be = 2.725*10^-3 ;//[K^-1] Tf^-1
+Pr = .697 ;// Prandtl number
+g = 9.81 ;//[m^2/s] gravitational constt
+
+Ra = g*be*(Ts-Tsurr)/al*D^3/uv;
+//From equatiom 9.34
+Nu = [.60 + .387*Ra^(1/6)/[1+(.559/Pr)^(9/16)]^(8/27)]^2;
+h = Nu*k/D;
+
+qconv = h*%pi*D*(Ts-Tsurr);
+qrad = e*%pi*D*stfncnstt*(Ts^4-Tsurr^4);
+
+printf("\n Rate of heat loss per unit length of pipe is %i W/m",qconv+qrad);
+//END
\ No newline at end of file diff --git a/534/CH9/EX9.5/9_5_Radiation_Shield.sce b/534/CH9/EX9.5/9_5_Radiation_Shield.sce new file mode 100644 index 000000000..614664f2b --- /dev/null +++ b/534/CH9/EX9.5/9_5_Radiation_Shield.sce @@ -0,0 +1,33 @@ +clear;
+clc;
+printf('FUNDAMENTALS OF HEAT AND MASS TRANSFER \n Incropera / Dewitt / Bergman / Lavine \n EXAMPLE 9.5 Page 592 \n'); //Example 9.5
+// Heat Loss from pipe per unit of length
+// Heat Loss if air is filled with glass-fiber blanket insulation
+
+//Operating Conditions
+To = 35+273 ;//[K] Shield Temperature
+Ti = 120+273 ;//[K] Tube Temperature
+Di = .1 ;//[m] Diameter inner
+Do = .12 ;//[m] Diameter outer
+L = .01 ;//[m] air gap insulation
+
+//Table A.4 Air Properties T = 350 K
+k = 30*10^-3 ;//[W/m.K] Conductivity
+uv = 20.92*10^-6 ;//[m^2/s] Kinematic Viscosity
+al = 29.9*10^-6 ;//[m^2/s] alpha
+be = 2.85*10^-3 ;//[K^-1] Tf^-1
+Pr = .7 ;// Prandtl number
+g = 9.81 ;//[m^2/s] gravitational constt
+//Table A.3 Insulation glass fiber T=300K
+kins = .038 ;//[W/m.K] Conductivity
+
+Lc = 2*[2.303*log10(Do/Di)]^(4/3)/((Di/2)^-(3/5)+(Do/2)^-(3/5))^(5/3);
+Ra = g*be*(Ti-To)/al*Lc^3/uv;
+keff = .386*k*(Pr/(.861+Pr))^.25*Ra^.25;
+q = 2*%pi*keff*(Ti-To)/(2.303*log10(Do/Di));
+
+//From equatiom 9.58 and 3.27
+qin = q*kins/keff;
+
+printf("\n Heat Loss from pipe per unit of length is %i W/m \n Heat Loss if air is filled with glass-fiber blanket insulation %i W/m",q,qin);
+//END
\ No newline at end of file |