Chemical Engineering May 2014 - 53

NomeNclature
Ach
Ae
A1
β
Ch
Cp
De
Dp
F
Fm
h
k
kw
Kp
Lc
Cross-sectional flow area of one
channel, m2
Total effective heat-transfer area, m2
Plate true surface area, m2
A1p Plate planar projected area, m2
b
Mean channel flow gap, m
Chevron angle, deg
Heat-transfer correlation coefficient
Specific heat capacity, J/kg-K
Hydraulic diameter, m
Port diameter, m
∆p Pressure drop, Pa
f
Fanning friction factor
LMTD correction F-factor
Fouling margin, %
Convective heat-transfer coefficient,
W/m2-K
Fluid thermal conductivity, W/m-K
Plate thermal conductivity, W/m-K
Empirical coefficient of the Fanning
friction factor for each type of chevron
plate and Reynolds number
Compressed-plate pack length measured
between the two head
plates, m
Lhoriz Horizontal port-to-port center
distance, m
Lp
Lvert
Lw
Vertical distance between top port
bottom edge to bottom port top
edge, m
Effective flow length between the
vertical ports, m
Effective channel width (between
gasket grooves), m
LMTD Log-mean temperature difference, °C
mch Mass flowrate through each flow
channel, kg/s
µ
µb
Fluid viscosity, N-s/m2
Bulk fluid viscosity, N-s/m2
µw Fluid viscosity at the wall, N-s/m2
Ncp Number of channels per pass
Ne
Effective number of plates
Npass Number of passes
Nt
p
ϕ
Pr
Re
Prandtl number
Q Heat duty, W
Rf
Fouling resistance, m2K/W
Reynolds number
Figure 2.
There are two
typical plate
types used in a
PHE: intermating
type (left) and
chevron type
(right)
Total number of plates
Compressed pitch per plate, m
Surface enlargement factor
ρ
t
T1
T2
t1
t2
U
Vch
Vp
Density, kg/m3
Plate thickness, m
Hot side inlet temperature, °C
Hot side outlet temperature, °C
Cold side inlet temperature, °C
Cold side outlet temperature, °C
Overall heat-transfer coefficient,
W/m2-K
Fluid velocity in a flow channel, m/s
Fluid velocity through the port, m/s
W Mass flowrate through either hot
side or cold side, kg/s
Superscripts
m Power exponent for Reynolds number
effect on pressure drop (for calculation
of Fanning friction factor f)
n Power exponent for Reynolds number effect
on convective heat-transfer coefficient
Subscripts
c
Clean
Cold side
ch Channel
cl
e
f
Effective
Fouled
h
Hot side
p Port
t
Total
TABLE 1. TYPICAL MAXIMUM
OPERATING TEMPERATURES FOR
COMMON GASKET MATERIALS
Gasket material
Natural rubber/Neoprene
Nitrile/Viton
Butyl materials
Silicone
°C
70-90
125-135
100-155
180-250
ers are a better option than PHEs.
Some of the disadvantages associated
with the use of PHEs are
as follows:
* If gaskets deteriorate, especially
in the presence of hazardous fluids
or hydrocarbon mixtures, the
equipment is more susceptible to
atmospheric leaks
* A higher pressure drop is required
to induce turbulent flow at
smaller flow passages (2-5 mm);
at the same pressure drop, a PHE
may not provide the desired heattransfer
enhancement effect.
* Leaks are easily detectable
* The ability to individually remove
and clean plates decreases
maintenance and cleaning efforts
for both fluid sides; S&T heat
exchangers are more difficult to
open, especially on the shellside
* Turbulence can be achieved at a
relatively low Reynolds number,
typically less than 500
* Lower sensitivity to vibration
than S&T heat exchangers
* Very heat-sensitive process fluids
can be capably handled
However, there are some applications
where S&T heat exchang*
PHEs have limited use for gas-togas
heat-exchanger or boiling services
where volume expansion is
large, because the required outlet
nozzle will be too big
* Gasket materials selection can
impose constraints on operating
pressure and temperature
(See Table 1 for specific temperaChemiCal
engineering www.Che.Com may 2014 53
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Chemical Engineering May 2014

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