8 files changed, 445 insertions, 0 deletions
diff --git a/1244/CH7/EX7.1/Example71.sce b/1244/CH7/EX7.1/Example71.sce
new file mode 100755
index 000000000..f958d005e
--- /dev/null
+++ b/1244/CH7/EX7.1/Example71.sce
@@ -0,0 +1,38 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.1 ")
+
+//Diameter in m
+D = 0.3;
+//Cruising speed in m/s
+Uinfinity = 150;
+
+//At an altitude of 7500 m the standard atmospheric air pressure is 38.9 kPa and the density of the air is 0.566 kg/m3 (From Table 38 in Appendix 2).
+rho = 0.566;
+//Dynamic viscosity in kgm/s
+mu = 0.0000174;
+//Prandtl number
+Pr = 0.72;
+//Thermal conductivity in W/mK
+k = 0.024;
+
+//The heat transfer coefficient at the stagnation point (0) is, according to Eq. (7.2)
+
+disp("Heat transfer coefficient at stagnation point in W/m2K")
+//Heat transfer coefficient at stagnation point in W/m2K
+h = (((k*1.14)*((((rho*Uinfinity)*D)/mu)^0.5))*(Pr^0.4))/D
+
+disp("Distribution of the convection heat trans-fer coefficient over the forward portion of the wing")
+for o = 0:15:75 //o is the parameter used in the loop
+    //convection heat trans-fer coefficients in W/m2K
+  ho = h*(1-(o/90)^3);
+  // L.26: No simple equivalent, so mtlb_fprintf() is called.
+  mtlb_fprintf("At an angle of %5.2f degree, heat transfer coeffcient is %5.2f\n",o,ho)
+end;
diff --git a/1244/CH7/EX7.2/Example72.sce b/1244/CH7/EX7.2/Example72.sce
new file mode 100755
index 000000000..6e3cea7cb
--- /dev/null
+++ b/1244/CH7/EX7.2/Example72.sce
@@ -0,0 +1,55 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.2 ")
+
+//Diameter of wire in m
+D = 0.000025;
+//Length of wire in m
+L = 0.006;
+//Free stream temperature of air in degeee C
+T = 20;
+//Wire temperature to be maintain in degree C
+Tw = 230;
+//Resistivity of platinum in ohm-cm
+Re = 0.0000171;
+
+//Since the wire is very thin, conduction along it can be neglected; also, the temperature gradient in the wire at any cross section can be disregarded.
+
+//At freestream temperature, for air:
+
+//Thermal conductivity in W/mC
+k = 0.0251;
+//Kinematic viscosity in m2/s
+nu = 0.0000157;
+
+//Reynolds number at velocity = 2m/s
+Rey = (2*D)/nu;
+if Re<40 then
+  //Using the correlation equa-tion from Eq. (7.3) and Table 7.1
+  //Average convection heat transfer coefficient as a function of velocity
+  //is
+  //hc=799U^0.4 W/m2C
+
+  //At this point, it is necessary to estimate the heat transfer coefficient for radiant heat flow.
+  //According to Eq. (1.21), we have approximately
+  //hr=sigma*epsilon*((Ts+Tinfinity)^3)/4
+
+  //The emissivity of polished platinum from Appendix 2, Table 7 is about 0.05, so hr is about 0.05 W/m2C.
+
+  //The rate at which heat is transferred from the wire is therefore
+  //0.0790U^4 W.
+
+  //The electrical resistance of the wire in ohm is
+  R = ((Re*L)*4)/(((100*%pi)*D)*D);
+end;
+
+//A heat balance with the current i gives
+disp("Current in ampere as a function of velocity is")
+disp("i=0.19*U^0.2")
diff --git a/1244/CH7/EX7.3/Example73.sce b/1244/CH7/EX7.3/Example73.sce
new file mode 100755
index 000000000..c825a7080
--- /dev/null
+++ b/1244/CH7/EX7.3/Example73.sce
@@ -0,0 +1,40 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.3 ")
+
+//Velocity of air in m/s
+Uinfinity = 0.5;
+//Length and breadth of square shaped array in m
+L = 2.5;
+//Surface temperature in degree C
+Ts = 70;
+//Ambient temperature in degree C
+Ta = 20;
+
+//At free stream temperature of air
+//Kinematic viscosity in m2/s
+nu = 0.0000157;
+//Density in kg/m3
+rho = 1.16;
+//Specific heeat in Ws/kgC
+c = 1012;
+//Prandtl number
+Pr = 0.71;
+
+//Reynolds number
+Re = (Uinfinity*L)/nu;
+
+//From equation 7.18
+//The average heat transfer coefficient in W/m2C is
+//Heat transfer coefficient in W/m2C 
+h = (((0.0033*(Pr^(-2/3)))*c)*rho)*Uinfinity;
+disp("Heat loss from array in W is")
+//Heat loss in W 
+q = ((h*L)*L)*(Ts-Ta)
diff --git a/1244/CH7/EX7.4/Example74.sce b/1244/CH7/EX7.4/Example74.sce
new file mode 100755
index 000000000..23d7d3bfc
--- /dev/null
+++ b/1244/CH7/EX7.4/Example74.sce
@@ -0,0 +1,58 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.4 ")
+
+//Diameter of pipe in m
+D = 7.62/100;
+//Diameter and length of cylinder in m
+d = 0.93/100;
+l = 1.17/100;
+//Initial temperature in degree C
+Ti = 50;
+//Final temperature in degree C
+Tf = 350;
+//Temperature of pipe surface in degree C
+Tp = 400;
+//Therefore film temp. at inlet in degree C
+Tfi = (Ti+Tp)/2;
+//Therefore film temp. at outlet in degree C
+Tfo = (Tf+Tp)/2;
+//Average film temp. in degree C
+Tf = (Tfi+Tfo)/2;
+
+//At this film temperature
+//Kinematic viscosity in m2/s
+nu = 0.0000482;
+//Thermal conductivity in W/mC
+k = 0.042;
+//Density in kg/m3
+rho = 0.6;
+//Specific heat in J/kgC
+c = 1081;
+//Prandtl number
+Pr = 0.71;
+//Flow rte of gas in kg/h is
+m = 5;
+
+//Superficial velocity in m/h
+Us = m/((((rho*%pi)*D)*D)/4);
+//Cylinder packaging volume in m3
+V = (((%pi*d)*d)*l)/4;
+//Surface area in m2
+A = (((2*%pi)*d)*d)/4+(%pi*d)*l;
+//Equivalent packaging dia in meter
+Dp = (6*V)/A;
+
+//REynolds number based on this dia
+Re = ((Us*3600)*Dp)/nu;
+//From eq. 7.23
+disp("Heat transfer coefficient in W/m2C is")
+//Heat transfer coefficient in W/m2C
+h = (14.3*k)/Dp
diff --git a/1244/CH7/EX7.5/Example75.sce b/1244/CH7/EX7.5/Example75.sce
new file mode 100755
index 000000000..a250856c3
--- /dev/null
+++ b/1244/CH7/EX7.5/Example75.sce
@@ -0,0 +1,99 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.5 ")
+
+//Initial temperature in degree F
+Ti = 58;
+//Final temperature in degree F
+Tf = 86;
+//Film temperature of air in degree F
+Tair = (Ti+Tf)/2;
+//Temperature of condensing steam in degree F
+Tsteam = 212;
+//Heat transfer coeffcient in Btuh/ft2F
+ho = 1000;
+//Length of tube in ft
+L = 2;
+//Diameter of tube in in
+d = 0.5;
+//Wall thickness in inches
+t = 0.049;
+//Pitch in inches
+p = 3/4;
+//Width in ft and height in inches of rectangular shell
+H = 15;
+W = 2;
+//Mass flow rate of air in lb/h
+m = 32000;
+
+//Appendix 2, Table 28 then gives for the properties of air at this mean
+//bulk temperature
+
+//Density in lb/ft3
+rho = 0.072;
+//Thermal conductivity in Btu/h F ft
+k = 0.0146;
+//Dynamic viscosity in lb/fth
+mu = 0.0444;
+//Prandtl number for air and steam
+Pr = 0.71;
+
+//Calcaulating minimum free area in ft2
+A = ((H/p)*W)*((p-d)/12);
+//Maximum gas velocity in lb/h.ft2
+Gmax = m/A;
+//Hence the reynolds number is
+Re = (Gmax*d)/(12*mu);
+
+//Assuming that more than 10 rows will be required, the heat transfer coefficient is calculated from Eq. (7.29)
+
+//h value in Btu/h ft2 F
+h = ((((k*12)/d)*(Pr^0.36))*0.27)*(Re^0.63);
+
+//The resistance at the steam side per tube in h F/Btu
+R1 = 12/(((ho*%pi)*(d-2*t))*L);
+
+//The resistance of the pipe wall in h F/Btu
+R2 = 0.049/(((60*%pi)*L)*(d-t));
+
+//The resistance at the outside of the tube in h F/Btu
+R3 = 1/((((h*%pi)*d)*L)/12);
+
+//Total resistance in h F/Btu
+R = R1+R2+R3;
+
+//Mean temperature difference between air and steam in degree F is
+deltaT = Tsteam-Tair;
+
+//Specific heat of air in Btu/lb F
+c = 0.241;
+
+//Equating the rate of heat flow from the steam to the air to the rate of enthalpy rise of the air
+
+//Solving for N gives
+disp("Total number of transverse tubes needed are")
+//Total number of transverse tubes
+N = (((m*c)*(Tf-Ti))*R)/(20*deltaT)
+disp("Rounding off = 5 tubes")
+
+if N<10 then
+  //Correction for h value, again in Btu/h ft2 F
+  h = 0.92*h;
+end;
+
+//The pressure drop is obtained from Eq. (7.37) and Fig. 7.25.
+
+//Velocity in ft/s
+Umax = Gmax/(3600*rho);
+//Acceleration due to gravity in ft/s2
+g = 32.2;
+disp("Corresponding pressure drop in lb/ft2")
+//Corresponding pressure drop in lb/ft2
+P = ((((6*0.75)*rho)*Umax)*Umax)/(2*g)
diff --git a/1244/CH7/EX7.6/Example76.sce b/1244/CH7/EX7.6/Example76.sce
new file mode 100755
index 000000000..f9e81cdf6
--- /dev/null
+++ b/1244/CH7/EX7.6/Example76.sce
@@ -0,0 +1,62 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.6 ")
+
+//Temperature of methane in degree C
+T = 20;
+//Outer dia of tube in m
+D = 4/100;
+//Longitudinal spacing in m
+SL = 6/100;
+//Transverse spacing in m
+ST = 8/100;
+//Wall temperature in degree C
+Tw = 50;
+//Methane flow velocity in m/s
+v = 10;
+
+//For methane at 20°C, Table 36, Appendix 2 gives
+
+//Density in kg/m3
+rho = 0.668;
+//Thermal conductivity in W/mK
+k = 0.0332;
+//Kinematic viscosity in m2/s
+nu = 0.00001627;
+//Prandtl number
+Pr = 0.73;
+
+//From the geometry of the tube bundle, we see that the minimum flow
+//area is between adjacent tubes in a row and that this area is half
+//the frontal area of the tube bundle. Thus,
+//Velocity in m/s
+Umax = 2*v;
+
+//Reynolds number
+Re = (Umax*D)/nu;
+
+//Since ST/SL<2, we use Eq. (7.30)
+
+//Nusselt number
+Nu = ((0.35*((ST/SL)^0.2))*(Re^0.6))*(Pr^0.36);
+
+//Heat transfer coefficient in W/m2K
+h = (Nu*k)/D;
+
+//Since there are fewer than 10 rows, the correlation factor in Table 7.3 gives
+disp("Heat transfer coefficient in W/m2K")
+//Heat transfer coefficient in W/m2K
+h = 0.92*h
+
+//Tube-bundle pressure drop is given by Eq. (7.37). The insert in Fig. (7.26) gives the correction factor x.
+
+disp("Corresponding pressure drop in N/m2")
+//Corresponding pressure drop in N/m2
+P = ((((5*0.25)*rho)*Umax)*Umax)/2
diff --git a/1244/CH7/EX7.7/Example77.sce b/1244/CH7/EX7.7/Example77.sce
new file mode 100755
index 000000000..494b788e8
--- /dev/null
+++ b/1244/CH7/EX7.7/Example77.sce
@@ -0,0 +1,45 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.7 ")
+
+
+//Temperature of jet in degree C
+T = 20;
+//Thermal conductivity in W/mK
+k = 0.597;
+//Dynamic viscosity in Ns/m2
+mu = 0.000993;
+//Prandtl number
+Pr = 7;
+//Mass flow rate in kg/s
+m = 0.008;
+//Diameter of jet in m
+d = 6/1000;
+//Total heat flux in W/m2
+q = 70000;
+
+//Reynolds number
+Re = (4*m)/((%pi*d)*mu);
+
+disp("For r=3mm")
+//From Eq. (7.45)
+//Heat transfer coefficient in W/m2K
+h = (63*k)/d;
+disp("Surface temperature at r=3mm in degree C is")
+//Surface temperature in degree C
+Ts = T+q/h
+
+disp("For r=12mm")
+//From Eq. (7.48)
+//Heat transfer coefficient in W/m2K
+h = (35.3*k)/d;
+disp("Surface temperature at r=12mm in degree C is")
+//Surface temperature in degree C
+Ts = T+q/h
diff --git a/1244/CH7/EX7.8/Example78.sce b/1244/CH7/EX7.8/Example78.sce
new file mode 100755
index 000000000..5643bf3e9
--- /dev/null
+++ b/1244/CH7/EX7.8/Example78.sce
@@ -0,0 +1,48 @@
+
+
+// Display mode
+mode(0);
+
+// Display warning for floating point exception
+ieee(1);
+
+clc;
+disp("Principles of Heat Transfer, 7th Ed. Frank Kreith et. al Chapter - 7 Example # 7.8 ")
+
+//Temperature of plate in degree C
+Tplate = 60;
+//Temperature of jet in degree C
+T = 20;
+//Thermal conductivity in W/mK
+k = 0.0265;
+//Dynamic viscosity in Ns/m2
+mu = 0.00001912;
+//Prandtl number
+Pr = 0.71;
+//Density in kg/m3
+rho = 1.092;
+//Mass flow rate in kg/s
+m = 0.008;
+//Width of jet in m
+w = 3/1000;
+//Length of jet in m
+l = 20/1000;
+//Velocity of jet in m/s
+v = 10;
+//Exit distance in m
+z = 0.01;
+//Width given for plate in m
+L = 0.04;
+//Reynolds number
+Re = ((rho*v)*w)/mu;
+
+//From Eq. (7.68) with x= 0.02 m, z =0.01 m, and w= 0.003 m
+//Nusselt number
+Nu = 11.2;
+// ! L.33: mtlb(d) can be replaced by d() or d whether d is an M-file or not.
+//Heat transfer coefficient in W/m2K
+h = (Nu*k)/mtlb(w);
+
+disp("Heat transfer rate from the plate in W is")
+//Heat transfer rate from the plate in W
+q = ((h*L)*l)*(Tplate-T)