The present work aims to investigate the influence of extended surfaces (fins) on the multi-objective optimization of a tubular heat exchanger network (THEN). An increase in the heat transfer area using various extended surfaces (fins) to enhance the performance of the heat exchanger was used while considering the effectiveness and total heat transfer area as two objective functions. In addition to the simulation of simple fins, a new set of fins, called constructal fins, was designed based on the constructal theory. Tubular heat exchanger network design parameters were chosen as optimization variables, and optimization results were achieved in such a way as to enhance the effectiveness and decrease the total heat transfer area. The results show the importance of constructal fins in improving the objective functions of heat exchangers. For instance, the simple fins case enhances the effectiveness by up to 5.3% compared to that without fins (usual heat exchanger) while using constructal fins, in addition to the 7% increment of effectiveness, reduces the total heat transfer area by 9.47%. In order to optimize the heat exchanger, the heat transfer rate and cold fluid temperature must increase, and at the same time, the hot exiting fluid temperature should decrease at the same constant total heat transfer area, which is higher in the constructal fins case. Finally, optimized design variables were studied for different cases, and the effects of various fins were reported.
Cross sectional area of inlet flow to annulus space side/m2
A1
First part heat transfer area/m2
A2
Second part heat transfer area/m2
cp
Specific heat/(J·kg–1·K–1)
CL
Tube layout constant
CTP
Constant for number of tube pass
di
Inner diameter of tube/m
do
Outer diameter of tube/m
De
Equivalent diameter/m
Dh
Hydraulic diameter/m
Ds
Shell diameter/m
f
Fanning friction factor
h
Convection heat transfer coefficient/(W·m–2·K–1)
Ke
Exit pressure loss coefficient
Kc
Entrance pressure loss factor
L1
Fin first part length/m
L2
Fin second part length/m
Nt
Tube number
NHE
Heat exchanger number
NTU
Number of transfer units
LMTD
Logarithmic mean temperature difference
Nu
Nusselt number
Np
Number of tube pass
Pr
Prandtl number
pt
Tube pitch/m
Qmax
Maximum heat transfer rate/kW
Re
Reynolds number
R
Fouling resistance/(K·m2·W–1)
t1
Fin thickness in the first part/m
t2
Fin thickness in the second part/m
Uo
Overall heat transfer coefficient/(W·m–2 ·K–1)
v
Fluid flow velocity/(m·s–1)
μ
Viscosity/(kg·m–1·s–1)
?Ptotal
Total pressure drop/kPa
ρ
Density/(kg·m–3)
Effectiveness
σ
Porosity/(gr·cm–3)
Subscripts
c
Cold side
h
Hot side
F
Fin
i
Inner
o
Outer
s
Shell
t
Tube
w
Wall
tot
Total
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