Condensation for Vertical Tubes.

The Dukler thoery assumes that three fixed factors must be known to establish the value of the average heat-transfer coefficient for condensing inside vertical tubes. These are the terminal Reynolds number, the Prandtl number of the ocndensed phase, and a dimensioless group A_d. The Reynolds number and Pradtl numbers are related to the condensing coefficient in Fig 7-17. However, that figure is based on A_d = 0, which assumes no interfacial shear. A table is provided by Chopey (page 7-50) that provides factors that are function of Reynolds number and A_d.

more on verticle and horizontal tubes

Module for calculation of heat transfer coefficient for condensation in tubes for different orientation

ρL (liquid density, lb per ft3)
ρV (vapor density, lb per ft3)
kL (liquid thermal conductivity, BTU per hr per ft per deg F)
μL (liquid viscosity, lb per ft per hr)
μV (vapor viscosity, lb per ft per hr)
L (tube length, in)
n (number of tubes)
W (condensate flow rate, lb per hr)
Γ (condensate rate per unit periphery)
GL (liquid mass velocity, lb per hr per ft<sup>2)
GV (vapor mass velocity, lb per hr per ft2)
Di (inside tube diameter, in)
cL (liquid specific heat, BTU per lb per deg F)
ReL (liquid Reynolds number)
ReV (vapor Reynolds number)
h (heat-transfer coefficient, BTU per hr per ft2 per deg F)
hgroup (Figure 10-10 Perry)
y_h (Figure 7-3 Chopey)
CondensationVertical Tubes Inside Horizontal Tubes Outside Horizontal Tubes