See discussions, stats, and author profiles for this publication at: https://www.researchgate.net/publication/342397348
Thermofluids Laboratory: Heat Exchangers
Experiment Findings · October 2019
CITATIONS
READS
0
417
5 authors, including:
Cameron Little
Wesam Alnahri
New York Institute of Technology
WJN LLC
2 PUBLICATIONS 0 CITATIONS
14 PUBLICATIONS 0 CITATIONS
SEE PROFILE
Some of the authors of this publication are also working on these related projects:
Material Transfer View project
All content following this page was uploaded by Wesam Alnahri on 23 June 2020.
The user has requested enhancement of the downloaded file.
SEE PROFILE
Group E
MENG343: Thermofluids Laboratory
Lab#2: Heat Exchangers
Cameron Little – Lead
John Hayes
Louis LaFemina
Leasean McDonald
Wesam Alnahri
Performed on
9/25/2019 & 10/2/2019
Submitted on
10/9/2019
Group E
Table of Contents
Abstract ................................................................................................................................ 1
Theory ................................................................................................................................... 1
Equipment: ............................................................................................................................ 5
Procedure .............................................................................................................................. 7
Results .................................................................................................................................. 8
Conclusion ........................................................................................................................... 15
Appendices: ............................................................................................................................i
Table of Figures
Figure 1: Temperature vs location plots for counter flow and equations from manual. ............... 2
Figure 2: Temperature vs location plots for cocurrent flow and equations from manual. ............ 3
Figure 3: Parallel and counter flow specific heats ratio effects on effectiveness. ......................... 5
Figure 4: Schematics of the HT33 Shell & Tube Heat Exchanger. ................................................... 6
Figure 5: Tube and Shell heat exchanger picture of equipment. ....................................................ii
Figure 6: Plate heat exchanger picture of equipment. ...................................................................iii
Table of Tables
Table 1: Calculated data counter tube and shell. ........................................................................... 8
Table 2: : Calculated data parallel tube and shell.. ......................................................................... 9
Table 3: Raw data counter current base case tube and shell. ..........................................................iv
Table 4: Raw data counter current slower cold water case tube and shell. ....................................iv
Table 5: Raw data counter current slower hot water case tube and shell. .......................................v
Table 6: Raw data counter current hotter inlet temperature case tube and shell. ...........................vi
Table 7: Raw data parallel current base case tube and shell. ......................................................... vii
Table 8: Raw data parallel current slower cold water case tube and shell. ................................... vii
Table 9: Raw data parallel current slower hot water case tube and shell. .................................... viii
Table 10: Raw data parallel current hotter inlet temperature case tube and shell. ....................... viii
Table 11: Raw data counter current base case plate. ...................................................................... ix
Table 12: Raw data counter current slower cold water case plate. ................................................. ix
Table 13: Raw data counter current slower hot water case plate. ....................................................x
Group E
Abstract
The point of this lab was to determine which configuration of a heat exchanger would
give the better heat recovery, heat effectiveness, and NTUs. Heat exchangers are devices that are
used to efficiently transfer heat from one fluid to another. When sizing heat exchangers, the
overall effectiveness is one of the most important parameters. This is the most important
parameter to compare between the two different flow arrangements of counterflow and parallel
flow. We tested both parallel flow and counter flow across both tube and shell and plate heat
exchangers. Since there were 4 total temperatures we were employing into our heat transfer
equation, we used the log mean temperature difference.
Our results displayed consistent patterns between the changes to the variables we made
throughout this experiment. According to our results, for the tube and shell heat exchanger in
counter flow, our base case of 50°C and 4.0 L/min flow rate for the cold and hot water gave us
an NTU of 0.1399, and effectiveness of 0.1227, and a heat recovery of 85%. By slowing the cold
flow rate, this will lower the NTU to 0.0971 and the effectiveness to 0.0885, and a higher heat
recovery of 96% compared to the base. By slowing the hot flow rate, this will raise the NTU to
0.1945 and the effectiveness to 0.1629, and a higher heat recovery of 92% compared to the base.
By raising the temperature, this will lower the NTU to 0.1275 and the effectiveness to 0.1130,
and a higher heat recovery of 90% compared to the base. According to our results, for the tube
and shell heat exchanger in parallel flow, our base case of 50°C and 4.0 L/min flow rate for the
cold and hot water gave us an NTU of 0.1495, and effectiveness of 0.1293, and a heat recovery
of 93%. By slowing the cold flow rate, this will lower the NTU to 0.1104 and the effectiveness
to 0.0990, and a higher heat recovery of 97% compared to the base. By slowing the hot flow rate,
this will raise the NTU to 0.2142 and the effectiveness to 0.1742, and a higher heat recovery of
99% compared to the base. By raising the temperature, this will lower the NTU to 0.1427 and the
effectiveness to 0.1242, and a higher heat recovery of 96% compared to the base.
We tested the area based on the data from the DAQ system and compared it to the actual
area. The experimental area for the tube and shell heat exchanger is derived from Q=UA*ΔT.
Rearranging this and plugging in the values, we get A=Q/(U*ΔT)= 946W/(1996W/m^2K*28.84
K)= 0.01643 m^2. The actual area is calculated through the use of A=Q/(U*ΔT)=
3.1415*((0.00635m+0.00515m)/2)*1.008m. This gives us an actual area of 0.01643 m^2. The
percent error for these values is 11% for the base case.
Theory
From manual for Shell & Tube to figure the effects of cocurrent and counter flow on the heat
transfer and the temperature efficiencies:
Counter Operation
The hot and cold flows are opposite of each other with respect to the heat exchange as indicated
in figure (counter operation plot and schematics). The hot fluid will be in the seven small tubes
surrounded by the cold water.
Below: counter operation plot and schematics and equations
1
Group E
Figure 1: Temperature vs location plots for counter flow and equations from manual.
Cocurrent operation
The hot and cold flows are moving in a parallel manner with respect to the inlet and outlet of the
heat exchanger holder as indicated in figure (cocurrent operation plot and schematics).
Below: cocurrent operation plot and schematics
2
Group E
Figure 2: Temperature vs location plots for cocurrent flow and equations from manual.
The plate tube:
The hot and cold fluids flow between opposite sides of the plates which uses conduction to
transfer the heat into the colder fluid.
Remember that the 1-D convection heat transfer equation is:
q = hAΔT
Where :
q = heat transfer rate (BTU/hr)
h = convective heat transfer coefficient
A = heat transfer surface area
ΔT= temperature difference at a given location
For Heat Exchangers the above equation can hold at each point along the heat transfer path. This
can be solved numerically. Instead one can employ the LMTD formulation.
LMTD (Log mean Temperature Difference).
LMTD = (ΔT –ΔT )/(ln(ΔT /ΔT ))
a
b
a
b
3
Group E
Where:
“a” and “b” are locations (ends) for the heat exchanger, and the ΔT is the temperature
difference between the two fluids at the location “a” and “b”.
We can then construct the equation
q = UA*LMTD
Where:
𝐵𝑇𝑈
q = heat rate (e.g.; ℎ𝑟 )
𝐵𝑇𝑈
U = unit heat conductance ( ℎ𝑟 𝑓𝑡 2
A = area of interfacing area (ft2)
The LMTD formulation can be further refined by using a correction factor, “F”.
q = UA*LMTD*F
One can measure the LMTD, and look up the correction factor “F”
Heat Recovery:
This is simply a measure of the amount of heat transferred from one fluid to the other. By the
first law of thermodynamics, this will be 100% provided there is no other heat gains of losses
from our system (the HX), or work done by the system (unlikely).
Heat effectiveness, ε
HX Effectiveness (ε) is defined as the ratio of the actual heat transfer rate in the HX to that of its
maximum value limited only by the second law of thermo. (entropy) (see Kreith p. 497)
Q = εC (T -T )
Where:
C is the smaller of m c and m c (these are the hourly heat capacitances)
m is the mass flow rate
c is the specific heat. (h = hot, c = cold for the subscripts)
min
min
h in
c in
h
ph
c
pc
p
Depending on which of the hourly heat capacitances is smaller we have (see Kreith)
𝐶ℎ(𝑇ℎ 𝑖𝑛 – 𝑇ℎ 𝑜𝑢𝑡)
𝜀 =
𝐶𝑚𝑖𝑛(𝑇ℎ 𝑖𝑛 – 𝑇𝑐 𝑖𝑛)
Or
𝐶𝑐(𝑇𝑐𝑜𝑢𝑡 – 𝑇𝑐𝑖𝑛 )
𝜀 =
𝐶𝑚𝑖𝑛 (𝑇ℎ𝑖𝑛 − 𝑇𝑐𝑖𝑛 )
The benefit is once ε is known for a HX at one condition, it will hold for others where you no
longer need the temperature outlet conditions, only the temp inlet conditions to determine q
Number of Heat Transfer Units. NTU
This term is a measure of the heat transfer terms to that of the first law energy balance term.
𝑈𝐴
𝑁𝑇𝑈 =
𝐶𝑚𝑖𝑛
This unit is used for sizing HXs and is a function of the type of HX.
a) If one knows the NTU, the mass flow rates of the fluid streams with their heat
capacitance factors (that is Cmin and Cmax) one can determine the effectiveness of the
HX.
4
Group E
b) Alternatively, if one knows the effectiveness, the mass flow rates of the fluid
streams with their heat capacitance factors (that is Cmin and Cmax), one can determine
the NTUs and with knowing U can find the surface area needed.
Below is a sample of what the number of transfer units (NTU) vs the Heat Exchanger
Effectiveness should look like for parallel flow and counterflow.
Figure 3: Parallel and counter flow specific heats ratio effects on effectiveness.
NTU – effectiveness methods:
-Case 1 Relationships for Parallel Flow HX
e
= 1-exp{-NTU(1+ C /C )}/ 1+ C /C
NTU
= -ln{1-e(1 + C /C )}/ 1+ C /C
-Case 2 Relationships for counter Flow HX:
e
= 1-exp{-NTU(1- C /C )}/ 1- (C /C )exp{-NTU(1- C /C )}
e
= NTU/(1+NTU) ref. FE handbook
NTU
= ln{1-e(C /C )/[1 - e]}/ (1- C /C )
NTU
= e/(1-e) ref. FE handbook
parallel flow
min
parallel flow
min
counter flow
min
max
max
max
min
max
min
max
min
max
min
max
counter flow
counter flow
min
max
min
max
counter flow
Equipment:
Heat Exchanger apparatus with different heat exchangers. These include a Tube in shell and a
cross flow Plate.
5
Group E
Figure 4: Schematics of the HT33 Shell & Tube Heat Exchanger.
6
Group E
Controls:
Hot water temp- controlled by computer software
Hot water flow rate- controlled by computer software
Cold water flow rate- controlled by computer software
Heater control- controlled by computer software
Unit power control- controlled by computer software
Flow arrangement- we always have the program set to counterflow, but we manually
change the tubing in order to switch the flow arrangement
Sensors:
Flow meters- measures the flow with a typical uncertainty of ± 0.5%
Temperature sensors- measures the temperature with a typical uncertainty of ± 0.4%
DAQ:
Temperature Cold Before HX- reading of cold temperature before the heat exchanger
Temperature Cold After HX- reading of cold temperature after the heat exchanger
Temperature Hot Before HX- reading of hot temperature before the heat exchanger
Temperature Hot After HX- reading of hot temperature after the heat exchanger
Cold Water Flow- reading of the flow of the cold water
Hot Water Flow- reading of the flow of the hot water
Procedure
Reference HX Lab Manual for proper set up and operation of the unit (HT30XC).
1. Switch on the unit mains to on and pull the emergency stop button.
2. Ensure that the pressure regulator is closed, set the cold water flow control in the
software to 100%, and turn on the cold water supply at the source then increase the flow
of cold water by turning the knob on the regulator. For HT31, HT33, and HT36 units it
should be 4.9 L/min, and for HT32, HT34, and HT37 it should be 3 L/min.
a. It is important to note that a reading of 5.0 L/min can indicate that the sensor is
saturated and the actual flow rate is higher. Exceeding a flow of 5 L/min may
cause the flow control valve to lock.
b. Lock the knob when the correct flow values are achieved.
3. In the software, set the cold water flow control to 0%. The cold water flow valve is
driven from 0% to 100% in steps of 1%, as directed by the operator through the software.
.
The actual flow rate is measured by a flow meter and displayed in L/min on the computer
screen DAQ.
4. The hot water flow rate can be controlled from the computer software by varying the
rotational speed of the recirculation pump. The hot water flow valve is also driven from
0% to 100% in steps of 1%, as directed by the operator through the software.
.
In counter flow, the direction of flow of the hot water will be opposite as that of the cold
water. The parallel flow will consist of the hot and cold water flow moving in the same direction.
7
Group E
5. Using automatic flow, we can adjust the set point temperature, proportional band,
derivative time, and cycle time.
6. IMPORTANT: If a parameter is not being used as a variable at the given stage, use the
hot water flow as 4.0 L/min, the cold water flow as 4.0 L/min, and the hot temperature at
50°C. Use a time derivative of 10 seconds for 100 seconds, which will give 10 total data
points throughout time.
7. Set the Tube and Shell Heat Exchanger hot and cold flow to 4 L/min.
8. Starting at 50°C, increase the hot water temperature to 60°C while keeping the other
parameters constant. Run a table when the system appears to reach equilibrium.
9. Set the temperature back to 50°C, manually decrease the hot water flow rate from 4.0
L/min to 2.0 L/min. Run a table when the system appears to reach equilibrium.
10. Like the hot water flow in step 8, repeat the same process but with the cold water flow
until it reaches 2.0 L/min. Run a table when the system appears to reach equilibrium.
11. Save the data table generated from software for calculations following the experiment.
12. Switch the tubing of the heat exchanger to allow for parallel flow conditions (but keep
the DAQ program set to counter flow).
13. Repeat Steps 6 to 12 for the Plate Heat Exchangers.
There will be 16 total tables for this experiment. There is a base case and 3 cases that include
changing one of the variables for counter flow. We do the same for parallel flow, which provides
us with 8 tables for the tube and shell heat exchanger. Including 8 from the plate heat exchanger,
we will have a total of 16 tables.
Results
Tube and Shell Counterflow
Base: 50°C, 4.0 L/min
Slower Cold Flow Rate: 2.0 L/min
Slower Hot Flow Rate: 2.0 L/min
Hotter Temperature: 60°C
Table 1: Calculated data counter tube and shell.
NTU
Effectiveness
Heat Recovery
Base
0.1399 ± 0.002
0.1227 ± 0.002
85%
Slower Cold Flow Rate
0.0971± 0.002
0.0885 ± 0.002
96%
Slower Hot Flow Rate
0.1945 ± 0.005
0.1629 ± 0.004
92%
Hotter Temperature
0.1275 ± 0.007
0.1130 ± 0.006
90%
Tube and Shell Parallel Flow
Base: 50°C, 4.0 L/min
Slower Cold Flow Rate: 2.0 L/min
Slower Hot Flow Rate: 2.0 L/min
Hotter Temperature: 60°C
8
Group E
Table 2: : Calculated data parallel tube and shell..
NTU
Effectiveness
Heat Recovery
Base
0.1495 ± 0.003
0.1293 ± 0.002
93%
Slower Cold Flow Rate
0.1104 ± 0.003
0.0990 ± 0.003
97%
Slower Hot Flow Rate
0.2142 ± 0.005
0.1742 ± 0.003
99%
Hotter Temperature
0.1427 ± 0.004
0.1242 ± 0.003
96%
ΔT left side= 25.1
ΔT right side= 32.6
9
Group E
ΔT left side= 25.7
ΔT right side= 34.6
ΔT left side= 33.4
ΔT right side= 43.9
10
Group E
ΔT left side= 25.3
ΔT right side= 33.2
ΔT left side= 28.4
ΔT right side= 25.6
11
Group E
ΔT left side= 28.8
ΔT right side= 29.2
ΔT left side= 37.2
ΔT right side= 57.6
12
Group E
ΔT left side= 28.1
ΔT right side= 31.3
ΔT left side= 3.3
ΔT right side= 31.8
13
Group E
ΔT left side= 0
ΔT right side= 31.8
ΔT left side= 1.5
ΔT right side= 34.3
14
Group E
Conclusion
The effects we see from the changes of the cold/hot flow rates and temperatures were
consistent for both trials. Lowering the cold flow rate would always decrease the NTU and
effectiveness, but it would increase the heat recovery. Lowering the hot flow rate would always
increase the NTU, the effectiveness, and the heat recovery. Raising the temperature would
always decrease the NTU and effectiveness, but it would increase the heat recovery. Also, the
parallel flow would result in a greater NTU, effectiveness, and heat recovery than the counter
flow. Therefore, based on our results, the best overall tube and shell heat exchanger is one that is
run in parallel flow, with a faster cold flow rate, a slower hot flow rate, and a lower hot
temperature. Since the NTU varies with flow rate, and the unit heat conductance varies linearly,
then the unit heat conductance U is a function of hot and cold flow rate.
Theoretically, a heat exchanger will be performing at its best when the outlet
temperatures are equal. The closer the outlet temperatures are, the more effective the heat
exchanger is. Typically, counterflow heat exchangers are more efficient than parallel flow heat
exchangers because they create a more uniform temperature difference between the fluids over
the entire length of the fluid’s path. However, according to our results, the parallel flow heat
exchanger was more effective overall. Therefore, our experiment was not able to validate the
theory.
A source of error in this experiment is not being able to account for the loss of heat in the
heat exchanger due to the environment. Also, the heat exchanger set-up and DAQ system seemed
to have problems responding to the plate heat exchanger. When we inserted the plate heat
exchanger, the pump became more inconsistent with the flow rate of the cold water, and the
heater would not provide enough heat to adequately reach the temperature we set. Due to this, we
were unable to complete full data sets for the plate heat exchanger. However, we still provided
the graphs for the figure of the temperature change across inlet/outlet destinations. Also, the
DAQ system printed out a lot of 0’s for columns that were necessary for calculations. In order to
improve this experiment, we would suggest to move the heat exchanger lab to other side of the
room, since it is right next to the heat transfer lab. This can create temperature differences in the
environment that can cause a randomized error in the testing. The uncertainty for our
calculations were determined by taking the average difference between the maximum and
minimum values within each run values. Then, we took the average of all the uncertainties in a
column and used that as the uncertainty for the variable in the column of the tables.
15
Group E
Appendices:
Effectiveness:
Base case: Th = 50.4°, Vhot = 4 liters/min, Vcold = 4 liters/min
Tube and Shell
Ɛ = Cpmax ( Thot in - Thot out) / Cpmin (Thot in -Tcold out)
Cp hot = 4.180 kj/kg K, Cp cold 4.182 kj/kg K meaning that Cp = Cp min
Thus Ɛ = (Thot in - Thot out)/ (Thot in - Tcold)
Ɛ = (50.374° C - 46.314° C) / (50.374° C - 17.941° C)
Ɛ = 0.12318 +/- 0.002
Thot out and Tcold out are also measured from the DAQ
NTU:
Type: Countercurrent, Tube and Shell
From the skeletal experimental plan:
NTU = (Ɛ)/ (1- Ɛ) = (.12318 +/- 0.002)/ (1- 0.12318+/- 0.002)
NTU = 0.140485 +/- 0.002
Alternatively,
NTU = ln ((1-Ɛ(Cmin/Cmax))/(1-Ɛ))/(1-(Cmin/Cmax))
NTU = .140481 +/- 0.002
For Cmin/Cmax ≂ 1 the aforementioned equation is valid. In this case,
Cmin/Cmax = 4.1800 kj/kg K/ 4.1818 kj/kg K = 0.99957
So not much, if any, precision is lost through using equation NTU = (Ɛ)/(1-Ɛ)
Heat Recovery
% Recovery = q cold / q hot = (mc cp cold ΔT)/ (mh cp hot ΔT)
% Recovery = (0.06660 kj/s)(4.1818 kj/kg K)(3.4460° C)/ (0.065817 kg/s)(4.1800 kj/kg
K)(3.9949° C)
Heat Recovery % = 0.87328 = 87.328%
Dimensional Analysis:
Convection Heat Transfer
q= hAΔT
Btu/hr = (W)/(m^2 K)(m^2)(K)
ML^2/ ϴ^3 = ((ML^2/ϴ^3))/ ((L^2)(T)) (L^2) (T)
Btu/hr W → Units of power
i
Group E
Power → Energy per time
→ Force x Distance
→ ((ML/ϴ^2) x( L)) / ϴ = ML^2/ϴ^3
ML^2/ϴ^3 = (ML^4)(T) /(L^2)(ϴ^3)(T) = (ML^2)/ (ϴ^3)
Hence q = hAΔT
Q = UA(LMTD) where LMTD = ((ΔTa-ΔTb/ln(ΔTc/ΔTh))⍺T
ML^2/ϴ^3 = U(L^2)(T) → U⍺ (ML^2)/(ϴ^3)(T)(L^2)
U is the unit heat conductance with units
Btu/hr ft^2 ° F with dimensions (ML^2)/(ϴ^2) / (ϴ)(L^2)(T) = ML^2/ϴ^3)(L^2)(T)
Hence the equation is also dimensionally equivalent.
q = UA(LMTD)
Heat Effectiveness
Ɛ = Q / Cmin(Thot-Tcold) = (Btu)/((Btu)/(lbm R))(lbm)(° R) Cmin = mCpmin
= ((ML^2)/(ϴ^2))/ ((ML^2/ϴ^2)(M)(T))(M)(T)
(ML^2)/(ϴ^2)(M)(T)
Effectiveness is a ratio, which must be a dimensionless quantity. As expected, the dimensions
cancel out, and this expression is dimensionally homogeneous.
Ɛ = (Q)/Cmin(T hot- T cold)
A similar method will trivially show that NTU = UA /Cmin is dimensionless and equivalent.
Figure 5: Tube and Shell heat exchanger picture of equipment.
ii
Group E
Figure 6: Plate heat exchanger picture of equipment.
iii
Group E
Table 3: Raw data counter current base case tube and shell.
Sampl
e
Numb
er
1
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
21.4
45.00
0
4.0
90
4.00
4.180
4.182
48.376
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
50.4
46.4
17.9
Densit
y
Hot
Fluid
[kg/m³
]
988.8
Cold fluid
Average
Temperatu
re
[°C]
19.664
Densit
y
Cold
Fluid
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
3.4
0.06
6
0.06
7
1099.1
959.8
139.3
0.06
7
Tho
t
Tcol
d
[kg/m³
]
[°C]
[°C]
998.3
4.0
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
Overall
Heat
Transfer
Coefficie
nt
U
87.3
12.3
10.6
11.5
28.71
2014.69
Overall
Efficien
cy
[%]
2
50.3
46.4
17.9
21.4
45.00
0
4.0
90
4.00
4.180
4.182
48.345
988.8
19.649
998.3
3.9
3.4
0.06
6
1082.0
951.1
130.8
87.9
12.1
10.5
11.3
28.70
1984.42
3
50.3
46.4
18.0
21.3
45.00
0
4.0
90
3.91
4.180
4.182
48.377
988.8
19.65
998.3
3.9
3.4
0.06
6
0.06
5
1081.8
911.5
170.3
84.3
12.1
10.4
11.3
28.73
1981.94
4
50.4
46.4
17.9
21.3
45.00
0
4.0
90
4.07
4.180
4.182
48.376
988.8
19.633
998.3
4.0
3.4
0.06
7
0.06
8
1111.1
958.2
152.9
86.2
12.3
10.4
11.4
28.74
2034.49
21.4
46.00
0
3.4
0.06
5
0.06
5
1060.7
937.3
123.4
88.4
12.0
10.6
11.3
28.82
1936.86
21.4
45.00
0
3.4
0.06
6
0.06
4
1106.0
928.1
177.9
83.9
12.2
10.6
11.4
28.87
2016.40
21.4
46.00
0
3.4
0.06
5
0.06
5
1093.9
928.8
165.1
84.9
12.3
10.4
11.4
28.99
1985.69
21.4
45.00
0
3.5
0.06
5
0.06
7
1080.3
968.4
111.9
89.6
12.1
10.6
11.4
29.03
1958.86
21.4
45.00
0
3.5
0.06
6
0.06
7
1098.0
968.9
129.1
88.2
12.2
10.7
11.5
28.89
2000.70
21.4
45.00
0
0.06
8
0.06
5
1120.7
954.6
166.0
85.2
12.2
10.8
11.5
28.82
2046.34
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
Overall
Heat
Transfer
Coefficie
nt
U
5
6
7
8
9
10
50.4
50.5
50.7
50.7
50.5
50.5
46.5
46.5
46.6
46.7
46.5
46.5
17.9
17.9
17.9
17.9
17.9
17.9
4.0
4.0
4.0
4.0
4.0
90
90
90
90
90
3.91
3.87
3.91
4.00
4.00
4.180
4.180
4.180
4.180
4.180
4.182
4.182
4.182
4.182
4.182
48.487
48.534
48.643
48.707
48.534
4.1
90
3.91
4.180
4.182
48.487
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
4.0
40
2.00
4.181
4.181
50.567
988.7
988.7
988.6
988.6
988.7
988.7
19.664
998.3
19.664
998.3
19.649
998.3
19.68
998.3
19.648
998.3
19.663
3.9
4.0
4.0
4.0
4.0
998.3
4.0
3.5
Densit
y
Cold
Fluid
Tho
t
Tcol
d
[kg/m³
]
[°C]
[°C]
998.0
3.1
5.9
0.06
6
0.03
3
857.5
825.4
32.2
96.2
9.0
17.3
13.2
29.70
1519.43
5.9
0.06
6
0.03
3
847.5
825.1
22.4
97.4
8.9
17.2
13.1
29.88
1492.99
5.8
0.06
6
0.03
3
867.2
812.2
55.1
93.7
9.0
16.9
13.0
30.05
1518.86
5.9
0.06
6
0.03
3
848.9
820.8
28.1
96.7
8.9
17.1
13.0
30.06
1486.06
6.0
0.06
6
0.03
3
831.2
813.7
17.5
97.9
8.7
17.2
13.0
30.13
1452.08
5.9
0.06
5
0.03
3
830.6
816.7
13.9
98.3
8.8
16.9
12.9
30.19
1447.92
5.9
0.06
6
0.03
3
856.9
816.2
40.7
95.2
8.9
16.9
12.9
30.24
1491.54
5.9
0.06
6
0.03
3
830.8
821.0
9.8
98.8
8.7
17.0
12.9
30.22
1446.81
5.8
0.06
5
0.03
3
835.5
817.4
18.1
97.8
8.8
16.8
12.8
30.36
1448.16
5.9
0.06
6
0.03
4
838.3
842.6
-4.3
100.5
8.7
17.0
12.9
30.38
1452.36
Table 4: Raw data counter current slower cold water case tube and shell.
Sampl
e
Numb
er
1
2
3
4
5
6
7
8
9
10
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
52.1
49.0
17.9
23.8
45.00
0
23.8
45.00
0
23.7
45.00
0
23.8
45.00
0
23.8
45.00
0
23.7
45.00
0
23.8
45.00
0
23.8
45.00
0
23.7
45.00
0
23.8
45.00
0
52.3
52.5
52.5
52.5
52.6
52.7
52.6
52.7
52.8
49.2
49.3
49.4
49.5
49.5
49.6
49.6
49.7
49.7
17.9
17.9
17.9
17.9
17.9
17.9
17.9
17.9
17.9
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
4.0
40
40
40
40
40
40
40
40
40
2.00
2.00
2.00
1.96
2.00
2.00
2.00
2.01
2.04
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
4.181
50.772
50.897
50.944
51.008
51.023
51.133
51.071
51.212
51.243
Densit
y
Hot
Fluid
[kg/m³
]
987.8
987.7
987.6
987.6
987.6
987.6
987.5
987.5
987.5
987.5
Cold fluid
Average
Temperatu
re
[°C]
20.841
20.873
998.0
20.827
998.0
20.858
998.0
20.857
998.0
20.81
998.0
20.874
998.0
20.826
998.0
20.827
998.0
20.841
998.0
iv
3.1
3.1
3.1
3.0
3.1
3.1
3.0
3.1
3.1
Overall
Efficien
cy
[%]
Group E
Table 5: Raw data counter current slower hot water case tube and shell.
Sampl
e
Numb
er
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
Densit
y
Hot
Fluid
Cold fluid
Average
Temperatu
re
[°C]
Densit
y
Cold
Fluid
[kg/m³
]
Tho
t
Tcol
d
[°C]
[°C]
[kg/m³
]
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
0.03
3
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
0.06
7
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overall
Efficien
cy
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
Overall
Heat
Transfer
Coefficie
nt
U
742.1
704.3
37.8
94.9
16.3
7.7
12.0
28.80
1356.11
[%]
1
50.5
45.2
17.8
20.3
26.00
0
2.0
89
4.00
4.180
4.182
47.866
989.0
19.041
998.4
5.3
2.5
2
50.6
45.2
17.8
20.2
26.00
0
2.0
89
3.87
4.180
4.182
47.913
989.0
19.025
998.4
5.4
2.4
0.03
2
0.06
4
723.8
654.5
69.3
90.4
16.3
7.4
11.9
28.86
1319.77
3
50.7
45.4
17.8
20.3
26.00
0
2.0
89
4.00
4.180
4.182
48.07
988.9
19.041
998.4
5.4
2.5
0.03
3
0.06
7
727.9
704.3
23.7
96.8
16.2
7.7
12.0
29.01
1320.84
4
50.9
45.4
17.8
20.3
26.00
0
2.0
89
4.00
4.180
4.182
48.148
988.9
19.058
998.4
5.4
2.5
0.03
3
0.06
7
740.5
695.1
45.4
93.9
16.5
7.5
12.0
29.07
1340.89
5
50.9
45.6
17.8
20.3
26.00
0
2.0
89
3.87
4.180
4.182
48.29
988.8
19.058
998.4
5.3
2.6
0.03
2
0.06
4
714.0
689.9
24.2
96.6
15.9
7.7
11.8
29.21
1286.49
6
51.2
45.8
17.8
20.3
25.00
0
2.0
89
3.91
4.180
4.182
48.494
988.7
19.058
998.4
5.4
2.6
0.03
3
0.06
5
748.8
696.7
52.1
93.0
16.1
7.7
11.9
29.41
1339.74
7
51.2
45.7
17.8
20.3
26.00
0
2.0
89
4.00
4.180
4.182
48.462
988.7
19.058
998.4
5.6
2.5
0.03
3
0.06
7
756.6
695.1
61.4
91.9
16.6
7.5
12.1
29.38
1355.42
8
51.3
45.8
17.8
20.4
26.00
0
2.0
89
3.85
4.180
4.182
48.588
988.7
19.09
998.4
5.5
2.6
0.03
2
0.06
4
742.8
685.3
57.5
92.3
16.4
7.6
12.0
29.47
1326.42
9
51.4
45.9
17.8
20.3
25.00
0
2.0
89
3.97
4.180
4.182
48.635
988.6
19.074
998.4
5.5
2.5
0.03
3
0.06
6
761.4
698.4
63.0
91.7
16.3
7.5
11.9
29.54
1356.74
10
51.3
45.9
17.8
20.3
26.00
0
2.0
89
3.91
4.180
4.182
48.573
988.7
19.074
998.4
5.4
2.5
0.03
3
0.06
5
752.9
687.8
65.1
91.4
16.2
7.6
11.9
29.48
1344.31
v
Group E
Table 6: Raw data counter current hotter inlet temperature case tube and shell.
Sampl
e
Numb
er
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
Densit
y
Hot
Fluid
Cold fluid
Average
Temperatu
re
[°C]
[kg/m³
]
Densit
y
Cold
Fluid
Tho
t
Tcol
d
[°C]
[°C]
[kg/m³
]
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
0.06
6
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
0.06
7
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overall
Efficien
cy
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
Overall
Heat
Transfer
Coefficie
nt
U
1481.2
1345.8
135.4
90.9
12.5
11.3
11.9
37.53
2077.10
[%]
1
60.2
54.8
17.5
22.4
44.00
0
4.0
90
4.00
4.183
4.182
57.495
984.5
19.963
998.2
5.3
4.8
2
60.3
55.0
17.5
22.3
44.00
0
4.0
90
3.88
4.183
4.182
57.622
984.4
19.948
998.2
5.3
4.8
0.06
6
0.06
5
1455.3
1297.3
157.9
89.1
12.4
11.2
11.8
37.67
2033.01
3
60.4
55.1
17.5
22.4
43.00
0
4.0
90
3.91
4.183
4.182
57.783
984.3
19.962
998.2
5.3
5.0
0.06
6
0.06
5
1463.5
1349.0
114.5
92.2
12.3
11.5
11.9
37.82
2036.55
4
60.7
55.2
17.5
22.3
44.00
0
4.0
90
4.36
4.183
4.182
57.945
984.2
19.915
998.2
5.4
4.9
0.06
5
0.07
3
1480.1
1476.0
4.1
99.7
12.6
11.3
11.9
38.03
2048.37
5
60.9
55.4
17.5
22.5
44.00
0
4.0
90
3.81
4.183
4.182
58.137
984.1
20.01
998.2
5.5
4.9
0.06
6
0.06
3
1494.4
1304.7
189.8
87.3
12.6
11.4
12.0
38.13
2062.93
6
61.0
55.5
17.5
22.4
43.00
0
4.0
90
4.17
4.183
4.182
58.265
984.1
19.962
998.2
5.5
5.0
0.06
6
0.06
9
1513.1
1438.9
74.2
95.1
12.6
11.4
12.0
38.30
2079.07
7
61.0
55.7
17.5
22.5
44.00
0
4.0
90
4.10
4.183
4.182
58.343
984.0
20.01
998.2
5.4
4.9
0.06
5
0.06
8
1455.8
1406.0
49.8
96.6
12.4
11.3
11.8
38.33
1998.81
8
61.3
55.8
17.5
22.5
44.00
0
4.1
90
4.07
4.184
4.182
58.554
983.9
19.993
998.2
5.5
5.0
0.06
7
0.06
8
1562.7
1422.0
140.8
91.0
12.6
11.5
12.1
38.56
2132.90
9
61.6
55.9
17.5
22.4
44.00
0
4.0
90
4.17
4.184
4.182
58.732
983.8
19.946
998.2
5.7
4.9
0.06
5
0.06
9
1549.1
1429.9
119.1
92.3
12.8
11.2
12.0
38.78
2102.05
10
61.7
56.1
17.5
22.5
43.00
0
4.1
90
3.88
4.184
4.182
58.875
983.8
19.993
998.2
5.6
5.0
0.06
7
0.06
5
1568.7
1357.0
211.7
86.5
12.6
11.4
12.0
38.88
2123.43
11
61.8
56.2
17.5
22.6
44.00
0
4.0
90
3.88
4.184
4.182
59.019
983.7
20.024
998.2
5.6
5.1
0.06
5
0.06
5
1520.0
1373.7
146.3
90.4
12.7
11.5
12.1
38.99
2051.47
12
62.2
56.4
17.5
22.5
43.00
0
4.0
90
4.07
4.184
4.182
59.278
983.6
20.008
998.2
5.8
5.1
0.06
6
0.06
8
1593.7
1430.7
162.9
89.8
12.9
11.3
12.1
39.27
2135.97
13
62.1
56.4
17.5
22.6
43.00
0
4.1
90
4.00
4.184
4.182
59.276
983.6
20.055
998.2
5.7
5.1
0.06
7
0.06
7
1587.3
1433.2
154.1
90.3
12.7
11.5
12.1
39.22
2129.96
14
62.2
56.5
17.5
22.5
43.00
0
4.0
90
3.97
4.184
4.182
59.357
983.5
19.977
998.2
5.7
5.0
0.06
5
0.06
6
1569.2
1378.5
190.7
87.8
12.8
11.2
12.0
39.38
2097.21
15
62.3
56.6
17.5
22.4
43.00
0
4.0
90
3.85
4.184
4.182
59.438
983.5
19.962
998.2
5.8
5.0
0.06
6
0.06
4
1596.6
1327.0
269.6
83.1
12.9
11.1
12.0
39.47
2128.72
16
62.6
56.7
17.6
22.3
43.00
0
4.0
90
4.21
4.184
4.182
59.631
983.4
19.918
998.2
5.8
4.7
0.06
5
0.07
0
1600.4
1369.7
230.7
85.6
13.0
10.4
11.7
39.71
2121.12
17
62.4
56.6
17.5
22.5
43.00
0
4.0
90
4.07
4.184
4.182
59.502
983.5
20.008
998.2
5.8
5.1
0.06
5
0.06
8
1580.5
1430.7
149.8
90.5
12.9
11.3
12.1
39.49
2106.34
18
62.7
56.8
17.4
22.6
43.00
0
4.0
90
3.85
4.184
4.182
59.727
983.3
20.023
998.2
5.8
5.1
0.06
6
0.06
4
1613.8
1377.3
236.5
85.3
12.9
11.4
12.2
39.70
2139.25
19
62.7
57.0
17.4
22.6
43.00
0
4.0
90
4.00
4.184
4.182
59.837
983.3
20.038
998.2
5.8
5.2
0.06
6
0.06
7
1595.1
1442.3
152.7
90.4
12.7
11.4
12.1
39.80
2109.38
20
61.0
55.6
17.4
22.4
43.00
0
4.0
90
4.10
4.183
4.182
58.279
984.1
19.945
998.2
5.4
5.0
0.06
6
0.06
8
1470.7
1425.3
45.4
96.9
12.3
11.5
11.9
38.33
2019.22
21
59.4
54.3
17.4
22.3
43.00
0
4.0
90
4.23
4.183
4.182
56.884
984.8
19.852
998.2
5.1
4.8
0.06
5
0.07
0
1391.3
1413.8
-22.5
101.6
12.2
11.4
11.8
37.03
1977.33
vi
Group E
Table 7: Raw data parallel current base case tube and shell.
Sampl
e
Numb
er
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
Densit
y
Hot
Fluid
Cold fluid
Average
Temperatu
re
[°C]
[kg/m³
]
Densit
y
Cold
Fluid
Tho
t
Tcol
d
[°C]
[°C]
[kg/m³
]
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
0.06
7
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
0.06
7
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overall
Efficien
cy
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
Overall
Heat
Transfer
Coefficie
nt
U
1159.3
1053.3
105.9
90.9
13.0
11.8
12.4
28.07
2173.47
[%]
1
49.5
45.4
17.5
21.3
44.00
0
4.0
90
4.00
4.180
4.182
47.445
989.2
19.372
998.3
4.2
3.8
2
49.7
45.5
17.4
21.3
44.00
0
4.0
90
4.10
4.180
4.182
47.587
989.1
19.356
998.3
4.2
3.8
0.06
7
0.06
8
1167.8
1089.0
78.8
93.3
13.0
11.8
12.4
28.23
2177.11
3
50.0
45.7
17.5
21.3
44.00
0
4.0
90
4.17
4.180
4.182
47.824
989.0
19.404
998.3
4.3
3.8
0.06
6
0.06
9
1180.6
1096.7
83.9
92.9
13.2
11.6
12.4
28.42
2186.31
4
50.2
45.9
17.5
21.3
44.00
0
4.0
90
4.17
4.180
4.182
48.045
988.9
19.388
998.3
4.2
3.8
0.06
6
0.06
9
1161.8
1106.2
55.6
95.2
12.9
11.7
12.3
28.66
2133.77
5
50.7
46.4
17.4
21.4
44.00
0
4.0
90
4.07
4.180
4.182
48.532
988.7
19.418
998.3
4.3
3.9
0.06
6
0.06
8
1184.6
1115.3
69.3
94.2
13.0
11.8
12.4
29.11
2141.42
6
50.8
46.6
17.5
21.4
44.00
0
4.0
90
4.00
4.180
4.182
48.689
988.6
19.45
998.3
4.2
3.9
0.06
6
0.06
7
1166.2
1096.5
69.7
94.0
12.7
11.8
12.3
29.24
2099.20
7
51.1
46.8
17.5
21.5
45.00
0
4.0
90
4.17
4.180
4.182
48.94
988.5
19.481
998.3
4.4
4.0
0.06
6
0.06
9
1199.2
1160.2
39.0
96.7
13.0
11.9
12.4
29.46
2142.41
8
51.2
46.9
17.5
21.5
44.00
0
4.0
90
4.07
4.180
4.182
49.066
988.4
19.481
998.3
4.3
4.0
0.06
6
0.06
8
1181.0
1132.3
48.7
95.9
12.7
11.9
12.3
29.59
2101.01
9
51.4
47.1
17.4
21.4
44.00
0
4.0
90
4.07
4.180
4.182
49.239
988.4
19.449
998.3
4.3
4.0
0.06
6
0.06
8
1188.6
1132.9
55.7
95.3
12.7
11.8
12.3
29.79
2099.85
10
51.6
47.2
17.4
21.4
44.00
0
4.0
90
4.10
4.180
4.182
49.396
988.3
19.449
998.3
4.4
4.0
0.06
7
0.06
8
1235.5
1142.1
93.3
92.4
13.0
11.7
12.4
29.95
2171.32
Densit
y
Hot
Fluid
Cold fluid
Average
Temperatu
re
[°C]
Densit
y
Cold
Fluid
Tho
t
Tcol
d
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
[°C]
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
0.03
3
Overall
Efficien
cy
[°C]
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
0.06
6
Overall
Heat
Transfer
Coefficie
nt
U
916.0
884.6
31.5
96.6
10.2
19.4
14.8
27.90
1728.15
Table 8: Raw data parallel current slower cold water case tube and shell.
Sampl
e
Numb
er
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
[kg/m³
]
[kg/m³
]
[%]
1
50.2
46.9
17.5
23.8
44.00
0
4.0
44
2.00
4.180
4.181
48.584
988.7
20.66
998.1
3.3
6.4
2
49.8
46.6
17.5
23.6
44.00
0
4.0
44
2.00
4.180
4.181
48.175
988.8
20.552
998.1
3.2
6.1
0.06
6
0.03
3
883.5
845.5
38.0
95.7
10.0
18.8
14.4
27.60
1684.89
3
49.2
46.2
17.5
23.6
44.00
0
4.0
44
2.00
4.180
4.181
47.7
989.0
20.553
998.1
3.1
6.0
0.06
6
0.03
3
849.6
836.6
13.0
98.5
9.7
19.0
14.4
27.12
1648.68
4
48.9
45.9
17.5
23.4
44.00
0
4.0
44
2.04
4.180
4.181
47.415
989.2
20.474
998.1
3.0
5.9
0.06
6
0.03
4
832.7
841.1
-8.4
101.0
9.6
18.8
14.2
26.91
1628.29
5
48.7
45.7
17.5
23.4
44.00
0
4.0
44
2.09
4.180
4.181
47.208
989.3
20.458
998.1
3.1
6.0
0.06
7
0.03
5
851.0
865.9
-14.9
101.7
9.8
19.0
14.4
26.72
1675.93
6
48.6
45.5
17.5
23.3
45.00
0
4.0
44
2.04
4.180
4.181
47.034
989.3
20.38
998.1
3.1
5.8
0.06
6
0.03
4
850.9
823.8
27.1
96.8
9.9
18.6
14.3
26.63
1681.60
7
48.5
45.4
17.5
23.3
44.00
0
4.0
44
2.00
4.180
4.181
46.939
989.4
20.428
998.1
3.1
5.8
0.06
7
0.03
3
860.3
811.0
49.4
94.3
10.0
18.8
14.4
26.49
1709.52
8
48.5
45.5
17.5
23.3
44.00
0
4.0
44
2.06
4.180
4.181
47.002
989.4
20.412
998.1
3.1
5.8
0.06
6
0.03
4
850.9
830.0
20.9
97.5
10.0
18.7
14.3
26.57
1685.76
9
48.7
45.6
17.5
23.3
45.00
0
4.0
44
2.04
4.180
4.181
47.145
989.3
20.413
998.1
3.1
5.7
0.06
5
0.03
4
853.1
814.4
38.7
95.5
10.0
18.4
14.2
26.71
1681.03
10
48.9
45.8
17.5
23.4
44.00
0
4.0
44
2.04
4.180
4.181
47.319
989.2
20.443
998.1
3.1
5.9
0.06
6
0.03
4
850.3
832.3
18.0
97.9
9.9
18.7
14.3
26.85
1666.63
vii
Group E
Table 9: Raw data parallel current slower hot water case tube and shell.
Sampl
e
Numb
er
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
Densit
y
Hot
Fluid
Cold fluid
Average
Temperatu
re
[°C]
[kg/m³
]
Densit
y
Cold
Fluid
Tho
t
Tcol
d
[°C]
[°C]
[kg/m³
]
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
0.03
4
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
0.06
7
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overall
Efficien
cy
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
Overall
Heat
Transfer
Coefficie
nt
U
824.1
795.8
28.3
96.6
17.2
8.4
12.8
29.67
1461.93
[%]
1
51.5
45.6
17.4
20.3
26.00
0
2.0
90
4.00
4.180
4.182
48.539
988.7
18.844
998.4
5.8
2.9
2
51.8
45.7
17.4
20.3
26.00
0
2.0
90
4.00
4.180
4.182
48.726
988.6
18.844
998.4
6.1
2.9
0.03
3
0.06
7
848.7
814.1
34.6
95.9
17.7
8.5
13.1
29.85
1496.21
3
52.1
46.1
17.4
20.3
26.00
0
2.0
90
3.81
4.180
4.182
49.073
988.4
18.811
998.4
6.0
2.9
0.03
2
0.06
3
804.9
774.3
30.6
96.2
17.2
8.4
12.8
30.24
1401.06
4
52.2
46.3
17.4
20.4
26.00
0
2.0
90
4.07
4.180
4.182
49.23
988.4
18.893
998.4
6.0
3.0
0.03
3
0.06
8
829.5
836.9
-7.5
100.9
17.1
8.5
12.8
30.31
1440.20
5
52.2
46.2
17.4
20.2
26.00
0
2.0
90
4.39
4.180
4.182
49.167
988.4
18.811
998.4
6.0
2.9
0.03
2
0.07
3
813.1
873.1
-60.0
107.4
17.3
8.2
12.8
30.33
1411.01
6
52.1
45.9
17.4
20.2
25.00
0
2.1
90
4.39
4.180
4.182
48.993
988.5
18.795
998.5
6.1
2.8
0.03
4
0.07
3
877.4
863.1
14.3
98.4
17.7
8.1
12.9
30.17
1530.63
7
51.6
45.5
17.4
20.1
25.00
0
2.0
90
4.31
4.180
4.182
48.538
988.7
18.762
998.5
6.0
2.8
0.03
3
0.07
2
820.5
827.2
-6.8
100.8
17.7
8.1
12.9
29.75
1451.66
8
51.1
45.2
17.5
20.1
25.00
0
2.0
90
4.57
4.180
4.182
48.114
988.9
18.795
998.5
5.9
2.6
0.03
3
0.07
6
820.1
835.4
-15.2
101.9
17.5
7.8
12.7
29.29
1473.74
9
50.5
44.7
17.5
20.1
25.00
0
1.9
90
4.31
4.180
4.182
47.564
989.1
18.795
998.5
5.8
2.6
0.03
2
0.07
2
769.2
787.8
-18.6
102.4
17.6
8.0
12.8
28.74
1408.56
10
49.8
44.2
17.5
20.1
25.00
0
2.0
90
4.26
4.180
4.182
47.046
989.3
18.795
998.5
5.6
2.6
0.03
3
0.07
1
779.8
759.3
20.5
97.4
17.3
7.9
12.6
28.22
1454.18
Densit
y
Hot
Fluid
Cold fluid
Average
Temperatu
re
[°C]
Densit
y
Cold
Fluid
Tho
t
Tcol
d
Heat
Power
emitte
d
Qe
[W]
Heat
Power
absorbe
d
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Temp
Efficien
cy
of hot
fluid
[%]
Temp
Efficien
cy
of cold
fluid
[%]
Mean
Temp
Efficien
cy
[%]
LMT
D
[°C]
Cold
Mas
s
Flo
w
Rate
qmc
[kg/s
]
0.07
2
Overall
Efficien
cy
[°C]
Hot
Mas
s
Flo
w
Rate
qmh
[kg/s
]
0.06
6
Overall
Heat
Transfer
Coefficie
nt
U
1534.0
1524.9
9.1
99.4
13.2
12.0
12.6
36.95
2185.17
Table 10: Raw data parallel current hotter inlet temperature case tube and shell.
Sampl
e
Numb
er
Tem
p
T1
Tem
p
T2
Tem
p
T3
Tem
p
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pump
Settin
g
[%]
Hot
Water
Flowra
te
Fhot
[l/min]
Cold
Wate
r
Valve
Settin
g
[%]
Cold
Water
Flowra
te
Fcold
[l/min]
Specifi
c Heat
Hot
Fluid
Cph
[kJ/kg
K]
Specifi
c Heat
Cold
Fluid
Cpc
[kJ/kg
K]
Hot fluid
Average
Temperatu
re
[°C]
[kg/m³
]
[kg/m³
]
[%]
1
59.7
54.1
17.4
22.5
43.00
0
4.0
79
4.31
4.183
4.182
56.94
984.7
19.992
998.2
5.6
5.1
2
60.1
54.5
17.5
22.7
43.00
0
4.0
79
4.17
4.183
4.182
57.293
984.6
20.086
998.2
5.7
5.2
0.06
6
0.06
9
1575.0
1510.8
64.2
95.9
13.3
12.2
12.8
37.21
2227.87
3
60.2
54.6
17.5
22.7
43.00
0
4.0
76
4.07
4.183
4.182
57.372
984.5
20.086
998.2
5.6
5.2
0.06
6
0.06
8
1533.1
1474.6
58.5
96.2
13.1
12.2
12.7
37.29
2164.06
4
60.4
54.7
17.5
22.9
43.00
0
4.1
75
4.00
4.183
4.181
57.565
984.4
20.194
998.2
5.7
5.4
0.06
7
0.06
7
1582.4
1510.9
71.5
95.5
13.2
12.6
12.9
37.37
2228.59
5
60.5
54.9
17.5
22.9
43.00
0
4.0
75
4.10
4.183
4.181
57.676
984.4
20.179
998.2
5.6
5.4
0.06
6
0.06
8
1547.4
1539.8
7.7
99.5
13.1
12.5
12.8
37.50
2171.91
6
60.7
55.1
17.4
22.9
43.00
0
4.0
75
4.17
4.183
4.181
57.9
984.3
20.193
998.2
5.6
5.5
0.06
5
0.06
9
1517.2
1592.3
-75.1
104.9
12.9
12.7
12.8
37.71
2117.72
7
60.9
55.1
17.4
22.8
43.00
0
4.0
75
4.00
4.183
4.181
58.014
984.2
20.147
998.2
5.8
5.4
0.06
6
0.06
7
1579.8
1502.8
77.1
95.1
13.3
12.4
12.8
37.87
2195.79
8
60.5
54.9
17.5
22.9
43.00
0
4.0
75
3.87
4.183
4.181
57.66
984.4
20.211
998.2
5.6
5.4
0.06
6
0.06
4
1543.9
1452.2
91.8
94.1
13.1
12.6
12.8
37.45
2169.84
9
60.6
54.9
17.5
22.8
43.00
0
4.0
75
3.94
4.183
4.181
57.773
984.3
20.18
998.2
5.7
5.3
0.06
5
0.06
5
1532.3
1459.7
72.5
95.3
13.1
12.4
12.7
37.59
2145.20
10
60.4
54.7
17.5
22.8
43.00
0
4.0
75
4.07
4.183
4.181
57.549
984.4
20.163
998.2
5.7
5.4
0.06
6
0.06
8
1562.6
1518.5
44.2
97.2
13.3
12.5
12.9
37.39
2199.83
viii
Group E
Table 11: Raw data counter current base case plate.
Sampl
e
Numb
er
Te
mp
T1
Te
mp
T2
Te
mp
T3
Te
mp
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pum
p
Setti
ng
[%]
Hot
Water
Flowr
ate
Fhot
[l/min]
Cold
Wate
r
Valv
e
Setti
ng
[%]
Cold
Water
Flowr
ate
Fcold
[l/min]
Speci
fic
Heat
Hot
Fluid
Cph
[kJ/k
g K]
Speci
fic
Heat
Cold
Fluid
Cpc
[kJ/k
g K]
Hot Fluid
Average
Temperat
ure
[%]
Densi
ty
Hot
Fluid
1
49.7
33.3
33.4
18.2
28
1.5
35
1.47
4.178
4.179
41.508
991.6
25.793
996.8
16.
3
15.1
Hot
Mas
s
Flo
w
Rat
e
qm
h
[kg/
s]
0.02
5
2
49.8
33.4
33.4
18.2
28
1.5
35
1.43
4.179
4.179
41.604
991.6
25.809
996.8
16.
4
15.2
0.02
5
0.02
4
1696.
60
######
##
3208.
10
-89.1
100.1
16.3
91
-92.9
3.6
3
50.4
33.6
33.7
18.2
28
1.4
35
1.43
4.179
4.179
41.989
991.4
25.94
996.8
16.
8
15.5
0.02
3
0.02
4
1641.
80
######
##
3179.
33
-93.6
100.5
16.7
03
-92.7
3.9
4
50.4
33.6
33.7
18.2
28
1.5
35
1.43
4.179
4.179
41.989
991.4
25.923
996.8
16.
7
15.5
0.02
5
0.02
4
1728.
86
######
##
3269.
82
-89.1
100.3
16.6
71
-93.1
3.6
5
50.1
33.6
33.6
18.2
28
1.5
35
1.43
4.179
4.179
41.862
991.5
25.906
996.8
16.
5
15.5
0.02
5
0.02
4
1709.
22
######
##
3246.
93
-90.0
100.3
16.4
81
-94.0
3.2
6
50.2
33.5
33.6
18.1
28
1.4
35
1.38
4.179
4.179
41.861
991.5
25.873
996.8
16.
7
15.5
0.02
3
0.02
3
1629.
53
######
##
3110.
19
-90.9
100.5
16.5
77
-93.4
3.6
7
50.0
33.5
33.5
18.1
28
1.5
35
1.43
4.179
4.179
41.733
991.5
25.807
996.8
16.
5
15.4
0.02
5
0.02
4
1709.
57
######
##
3234.
46
-89.2
100.1
16.5
17
-93.0
3.6
8
49.9
33.5
33.5
18.1
28
1.5
35
1.38
4.179
4.179
41.733
991.5
25.807
996.8
16.
4
15.4
0.02
5
0.02
3
1696.
25
######
##
3164.
39
-86.6
99.7
16.4
53
-93.3
3.2
9
49.9
33.4
33.5
18.1
28
1.4
35
1.43
4.179
4.179
41.684
991.6
25.807
996.8
16.
5
15.4
0.02
3
0.02
4
1614.
23
######
##
3139.
11
-94.5
100.3
16.4
53
-93.3
3.5
10
50.0
33.5
33.5
18.1
28
1.4
35
1.38
4.179
4.179
41.733
991.5
25.791
996.8
16.
5
15.3
0.02
4
0.02
3
1641.
60
######
##
3106.
61
-89.2
99.7
16.5
18
-92.8
3.5
Cold
Water
Flowr
ate
Fcold
[l/min
]
[kg/m
³]
Cold
Fluid
Average
Temperat
ure
[%]
Densi
ty
Cold
Fluid
[kg/m
³]
Th
ot
Tcol
d
[°C
]
[°C]
Col
d
Mas
s
Flo
w
Rat
e
qmc
[kg/
s]
0.02
4
Heat
Powe
r
emitt
ed
Qe
[W]
Heat
Power
absorb
ed
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overall
Efficie
ncy
1690.
19
######
##
3229.
01
-91.0
100.1
[%]
Temp
Efficie
ncy
for hot
fluid
[%]
Temp
Efficie
ncy
for cold
fluid
[%]
Mean
Temp
Efficie
ncy
[%]
16.3
29
-92.6
3.8
LMT
D
Overall
Heat
Transfe
r
Coeffici
ent
U
0.000
6
0.000
7
0.002
7
0.001
7
0.001
7
0.002
7
0.000
7
0.001
4
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
4.8
#######
#
0.001
7
0.001
4
0.0
0.000
4.8
#######
#
Table 12: Raw data counter current slower cold water case plate.
Samp
le
Num
ber
Te
mp
T1
Te
mp
T2
Te
mp
T3
Te
mp
T4
1
49.1
39.8
42.7
18.3
Hot
Wat
er
Pum
p
Setti
ng
[%]
27
[°C]
[°C]
[°C]
[°C]
Hot
Water
Flowr
ate
Fhot
[l/min
]
1.4
Cold
Wat
er
Valv
e
Setti
ng
[%]
12
Speci
fic
Heat
Cold
Fluid
Cpc
[kJ/k
g K]
4.178
Hot
Fluid
Average
Tempera
ture
[%]
Dens
ity
Hot
Fluid
0.52
Speci
fic
Heat
Hot
Fluid
Cph
[kJ/k
g K]
4.179
Cold
Fluid
Average
Tempera
ture
[%]
Dens
ity
Cold
Fluid
44.437
990.4
30.507
2
49.4
40.0
43.0
18.4
27
1.4
12
0.49
4.179
4.178
44.693
990.3
30.673
995.4
9.5
24.6
0.023
0.008
924.9
6
840.17
1765.
13
-90.8
146.7
6.45
3
-381.3
-117.3
-0.0971
3
49.7
40.2
43.4
18.4
27
1.4
12
0.50
4.179
4.178
44.949
990.2
30.889
995.4
9.4
25.0
0.023
0.008
918.4
5
868.58
1787.
02
-94.6
149.8
6.27
9
-397.6
-123.9
-0.1
4
50.1
40.5
43.8
18.4
27
1.3
12
0.50
4.179
4.178
45.317
990.1
31.138
995.3
9.6
25.4
0.022
0.008
880.4
0
883.43
1763.
83
-100.3
152.7
6.26
2
-405.5
-126.4
-0.1042
5
50.4
40.8
44.1
18.5
27
1.4
12
0.50
4.179
4.178
45.589
990.0
31.321
995.2
9.7
25.6
0.023
0.008
942.8
0
891.34
1834.
14
-94.5
153.7
6.28
31
-407.8
-127.1
-0.1057
6
50.7
40.9
44.4
18.5
27
1.4
12
0.49
4.179
4.178
45.813
989.9
31.471
995.2
9.8
25.9
0.023
0.008
955.0
7
882.65
1837.
73
-92.4
155.1
6.30
53
-410.0
-127.5
-0.1081
7
50.8
41.1
44.6
18.6
27
1.4
12
0.49
4.179
4.178
45.957
989.8
31.604
995.2
9.7
26.1
0.023
0.008
945.5
5
889.35
1834.
89
-94.1
157.0
6.16
92
-422.3
-132.7
-0.1091
8
51.0
41.2
44.7
18.6
27
1.3
12
0.49
4.179
4.178
46.101
989.7
31.671
995.1
9.8
26.1
0.022
0.008
900.2
7
891.54
1791.
81
-99.0
156.2
6.26
13
-417.1
-130.5
-0.1087
9
51.0
41.3
44.8
18.6
27
1.4
12
0.49
4.179
4.178
46.133
989.7
31.688
995.1
9.7
26.1
0.023
0.008
942.2
4
892.66
1834.
90
-94.7
155.8
6.19
63
-422.0
-133.1
-0.1068
10
51.0
41.3
44.8
18.6
27
1.4
12
0.49
4.179
4.178
46.149
989.7
31.721
995.1
9.7
26.1
0.023
0.008
945.3
5
892.60
1837.
95
-94.4
156.3
6.19
51
-422.1
-132.9
-0.1078
[kg/
m³]
Th
ot
Tco
ld
[°C
]
[°C]
995.5
9.3
[kg/
m³]
ix
Hot
Mass
Flow
Rate
qmh
[kg/s]
Cold
Mass
Flow
Rate
qmc
[kg/s]
Heat
Powe
r
emitt
ed
Qe
[W]
Heat
Power
absor
bed
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overal
l
Efficie
ncy
[%]
Temp
Efficie
ncy
for hot
fluid
[%]
24.3
0.023
0.009
912.7
1
878.26
1790.
98
-96.2
145.3
Temp
Efficie
ncy
for
cold
fluid
[%]
Mean
Temp
Efficie
ncy
[%]
6.43
19
-378.4
-116.6
-0.0946
L
M
T
D
Overall
Heat
Transfer
Coefficient
U
0
.
0
0
.
0
0
.
0
0
.
0
0
.
0
0
.
0
0
.
0
0
.
0
0
.
0
0
.
0
0.000
0.000
0.000
0.000
0.000
0.000
0.000
0.000
0.000
0.000
Group E
Table 13: Raw data counter current slower hot water case plate.
Sampl
e
Numb
er
Te
mp
T1
Te
mp
T2
Te
mp
T3
Te
mp
T4
[°C]
[°C]
[°C]
[°C]
Hot
Wate
r
Pum
p
Setti
ng
[%]
Hot
Water
Flowr
ate
Fhot
[l/min]
Cold
Wate
r
Valv
e
Setti
ng
[%]
Cold
Water
Flowr
ate
Fcold
[l/min]
Speci
fic
Heat
Hot
Fluid
Cph
[kJ/k
g K]
Speci
fic
Heat
Cold
Fluid
Cpc
[kJ/k
g K]
Hot Fluid
Average
Temperat
ure
[%]
Densi
ty
Hot
Fluid
[kg/m
³]
Cold
Fluid
Average
Temperat
ure
[%]
Densi
ty
Cold
Fluid
[kg/m
³]
Th
ot
Tcol
d
[°C
]
[°C]
Hot
Mas
s
Flo
w
Rat
e
qm
h
[kg/
s]
0.00
8
Col
d
Mas
s
Flo
w
Rat
e
qmc
[kg/
s]
0.02
3
Heat
Powe
r
emitt
ed
Qe
[W]
Heat
Power
absorb
ed
Qa
[W]
Heat
Powe
r
lost
Qf
[W]
Overall
Efficie
ncy
856.8
1
625.71
1482.
52
-73.0
104.3
[%]
Temp
Efficie
ncy
for hot
fluid
[%]
Temp
Efficie
ncy
for cold
fluid
[%]
Mean
Temp
Efficie
ncy
[%]
25.1
78
-26.0
39.2
1
49.8
23.6
24.7
18.1
13
0.5
35
1.38
4.178
4.181
36.713
993.4
21.397
997.9
26.
3
-6.5
2
49.9
23.0
24.3
18.1
13
0.5
35
1.38
4.178
4.181
36.466
993.5
21.201
998.0
26.
9
-6.2
0.00
8
0.02
3
908.5
6
594.88
1503.
44
-65.5
105.1
25.6
31
-24.2
40.4
3
50.2
22.9
24.2
18.1
13
0.5
35
1.38
4.178
4.181
36.56
993.5
21.186
998.0
27.
3
-6.1
0.00
8
0.02
3
889.6
9
585.36
1475.
05
-65.8
105.1
25.9
51
-23.6
40.8
4
51.1
23.0
24.4
18.1
13
0.5
35
1.38
4.178
4.181
37.024
993.3
21.266
997.9
28.
1
-6.3
0.00
8
0.02
3
946.0
2
607.29
1553.
32
-64.2
105.4
26.6
18
-23.8
40.8
5
51.8
23.1
24.5
18.1
13
0.5
36
1.38
4.178
4.181
37.439
993.2
21.332
997.9
28.
8
-6.4
0.00
8
0.02
3
969.4
8
613.30
1582.
78
-63.3
105.4
27.2
86
-23.5
41.0
6
52.9
23.2
24.8
18.1
13
0.5
36
1.43
4.178
4.181
38.047
992.9
21.445
997.9
29.
8
-6.6
0.00
8
0.02
4
1003.
59
659.56
1663.
15
-65.7
105.7
28.1
75
-23.5
41.1
7
53.9
23.2
24.9
18.1
13
0.5
36
1.43
4.178
4.181
38.542
992.8
21.494
997.9
30.
7
-6.7
0.00
8
0.02
4
1034.
56
669.23
1703.
79
-64.7
105.7
29.0
35
-23.2
41.3
8
54.6
23.3
25.1
18.1
13
0.5
36
1.38
4.178
4.181
38.942
992.6
21.608
997.9
31.
2
-7.0
0.00
8
0.02
3
1018.
61
666.05
1684.
66
-65.4
106.0
29.4
78
-23.6
41.2
9
55.1
23.5
25.2
18.1
13
0.5
36
1.39
4.178
4.181
39.295
992.5
21.689
997.9
31.
7
-7.1
0.00
8
0.02
3
1067.
36
690.34
1757.
71
-64.7
106.0
29.8
9
-23.8
41.1
10
55.1
23.5
25.2
18.1
13
0.5
36
1.43
4.178
4.181
39.295
992.5
21.689
997.9
31.
6
-7.1
0.00
8
0.02
4
1116.
73
707.90
1824.
63
-63.4
105.9
29.8
58
-23.8
41.0
x
View publication stats
LMT
D
Overall
Heat
Transfe
r
Coeffici
ent
U
0.034
1
0.041
3
0.041
0.0
0.000
0.0
0.000
0.0
0.000
0.043
8
0.043
8
0.046
1
0.046
7
0.048
4
0.048
5
0.047
7
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000
0.0
0.000