shell and tube result
DESCRIPTION
data of shell and tube heat exchanger experimentTRANSCRIPT
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3. RESULTS
3.1 Temperature Profiles of Hot and Cold Stream
For counter current flow, the temperature profiles of each stream in the heat exchanger for
each experimental run are plotted in the Figure 3.1., Figure 3.2., Figure 3.3. and for co-current
flow, temperature profile is plotted in the Figure 3.4 and the data shown in Table 3.1.
0 20 40 60 80 1000
10
20
30
40
50
60
70
Counter-current Flow
Qcold=340L/h-Th
Qcold=340L/h-Tc
Length (cm)
T(C)
Figure 3.1. Counter-current flow temperature profile for un1
0 20 40 60 80 1000
5
10
15
20
25
30
Counter current Flow
Q=500L/h-Th
Q=500L/h-Tc
Length(cm)
T(C)
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Figure 3.2. Counter-current flow temperature profile for un2
0 20 40 60 80 1000
5
10
15
20
25
Counter-current Flow
Q=660L/h-Th
Q=660L/h-Tc
Length(cm)
T(C)
Figure 3.3. Counter-current flow temperature profile for un3
0 10 20 30 40 50 60 70 80 90 1000
10
20
30
40
50
60
70
Co-current Flow
Q=660L/h-Th
Q=660L/h-Tc
Length (cm)
T(C)
Figure 3.4. Co-current flow temperature profiles for un1
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Tale 3.1. Temperatures of each stream in different run
Flo! T"pe
Counter#
$urrent
%&ot'L(&
)
%$old'L(&
)
T&ot*in'oC
)
T&ot*out'oC
)
T$old*out'oC
)
T$old*in'oC
)
Run1 3!! 34! "#,3 4$,# 2%,% 14,!
Run2 3!! #!! "4,$ 4",1 2#,# 14,!
Run3 3!! ""! "3,1 44,2 23,2 14,1
Co#Current %&ot'L(&
)
%$old'L(&
)
T&ot*in T&ot*out T$old*out T$old*in
Run1 3!! ""! "4,2 4#," 23,2 14,1
3.2 Heat Transfer Rates
&eat transfer rates are calculated from below e'uations. This calculation is shown in(ppendix and results are tabulated below.
&eat Transfer ate for Cold )tream*
QC = mC ×CpC × (T Cin−T Cout )
&eat Transfer ate for &ot )tream*
Q H =m H ×Cp H × (T Hin−T Hout )
Tale 3.2. (+erage heat transfer rates for each streams and each run
Flo! T"pe
Counter#$urrent %&ot'L(&) %$old'L(&) %$'+) %&'+) %a,g'+)
Run1 3!! 34! "24% #$3! "!3%,#
Run2 3!! #!! ""$ "#1# "#%",#
Run3 3!! ""! "%# "#$# "$!
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Co#Current %&ot'L(&) %$old'L(&) %$'+) %&'+) %a,g'+)
Run1 3!! ""! "$%% "4$1 ""%!
3.3 -,erall Heat Transfer Coeffi$ients
+erall heat transfer coefficients are calculated for each stream b using heat transfer rates
and stead state inlet and outlet temperatures of the streams b using the below e'uations.
This calculation is shown in (ppendix. +erall transfer coefficient for each stream is
tabulated below.
U =Q
A× ΔT LM
and
ΔT
¿(¿¿1/ ΔT 2)
ΔT LM =
ΔT 1− ΔT 2¿
Tale 3.3. +erall &eat Transfer Coefficients of each run
Flo! T"pe
Counter#$urrent %&ot'L(&
)
%$old'L(&) %a,g'+) Tlm / U0'+(m2.)
Run1 3!! 34! "!3%,# 34,%4$! !,141 122#,"
Run2 3!! #!! "#%",# 3#,#$"" !,141 1314,%
Run3 3!! ""! "$! 34,!13 !,141 13$2,%
Co#Current %&ot'L(&
)
%$old'L(&) %a,g'+) Tlm / U0'+(m2.)
Run1 3!! ""! ""%! 34,4$21 !,141 13",1
3.4 Heat Transfer Coeffi$ients for Tue Side '&io)
&eat transfer coefficients for tube side /hi0 are calculated from nielinsi 'uation for each
run. This calculation is shown in (ppendix for un 1 and calculated enolds umber and
heat transfer coefficients for the tube side for each run are tabulated below.
Tale 3.4. &eat transfer coefficients for tube side /hio0 for each run
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Flo! T"pe
Counter#$urrent %&ot'L(&) %$old'L(&) Re"nolds umer &io'+(m2.)
Run1 3!! 34! 3124,1 13$,1"
Run2 3!! #!! 43$2, 2!"2,$!
Run3 3!! ""! #"#4,! 22".!$Co#Current %&ot'L(&) %$old'L(&) Re"nolds umer &io'+(m2.)
Run1 3!! ""! #"#4,! 22",!$
2000 4000 60001000
1200
1400
1600
1800
2000
2200
2400
2600
2800
3000
Individual Heat Transfer Coecient vs Reynolds um!er
Individual Heat Tan!"e
#oe$cient v! %e&nold!
'u()e
Linea *Individual Heat
Tan!"e #oe$cient v!
%e&nold! 'u()e+
Reynolds num!er
hio("#m$%&)
Figure 3.. &eat Transfer Coefficient for Tube )ide +s enolds umber raph
3. Heat Transfer Coeffi$ient for S&ell Side '&o)
&eat transfer coefficients for the shell side are calculated from the 5onohue 'uation. Thiscalculation is shown in (ppendix for un 1 and calculated heat transfer coefficients for the
shell side for different runs are tabulated below.
Tale 3.. &eat transfer coefficients for tube side /ho0 for each run
Flo! T"pe
Counter#$urrent %&ot'L(&) %$old'L(&) Re"nolds umer &o'+(m2.)
Run1 3!! 34! 13$#4,$ #!",%
Run2 3!! #!! 13"#%,3 4%"!,"Run3 3!! ""! 13222,1 413,4
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Co#Current %&ot'L(&) %$old'L(&) Re"nolds umer &o'+(m2.)
Run1 3!! ""! 1342",# 4""$,3
13000 13500 140004000
4200
4400
4600
4800
5000
5200
5400
5600
5800
Individual Heat Transfer Coecient vs Reynolds um!er
Individual Heat Tan!"e#oe$cient v! %e&nold!
'u()e
Linea *Individual Heat
Tan!"e #oe$cient v!
%e&nold! 'u()e+
Reynolds num!er
h'("#m$%&)
Figure 3.. 6ndi+idual &eat Transfer Coefficient +s enolds umber for )hell )ide
3. -,erall Heat Transfer Coeffi$ients from &io and &o
+erall heat transfer coefficients are recalculated b using the heat transfer coefficient for
shell and tube side. This calculation is done b using appropriate e'uations and sample
calculation of it for un 1 is shown in (ppendix.
Tale 3.. Theoretical +erall Transfer Coefficients for each run
Flo! T"pe
Counter#$urrent %&ot'L(&) %$old'L(&) U'+(m2.)
Run1 3!! 34! 13!,$$
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Run2 3!! #!! 1#$,!$
Run3 3!! ""! 1",$
Co#Current %&ot'L(&) %$old'L(&) U'+(m2.)
Run1 3!! ""! 1",4$
3.5. Heat Transfer Rate from -,erall Heat Transfer Coeffi$ients
&eat transfer rates for each run are calculated b using the o+erall heat transfer coefficient
calculated in (ppendix. This calculation is done b using the following e'uation.
Q=UA∆T LM
Tale 3.5 &eat Transfer ates from theoretical o+erall heat transfer coefficients
Flo! T"pe
Counter#$urrent %&ot'L(&) %$old'L(&) U'+(m2.) Tlm / %'+)
Run1 3!! 34! 13!,$$ 34,%4$! !,141 "44,%
Run2 3!! #!! 1#$,!$ 3#,#$"" !,141 %3,!2
Run3 3!! ""! 1",$ 34,!13 !,141 $"",$Co#Current %&ot'L(&) %$old'L(&) U'+(m2.) Tlm / %'+)
Run1 3!! ""! 1",4$ 34,4$21 !,141 $#,%4