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+
+
+// 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