Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Cooling of 23% sodium chloride solution
Step 3. Start configuring the exchanger. Beg coefficient to t
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-404 1.132
Sodium Chloride 33.2
Av. Density Av. Viscosity Av. Heat Capacity
-13 -13 903 0.158 1.250
Fluid Name Flow (M), Kg/s Temp. in, °C Temp. out, °C r, Kg/m3 2 m, mNs/m cp, kJ/kg°C
Heat Exchanged Av. Thermal Conductivity Fouling Resistance
145 0.0376 0.0004
Q, kW k, W/m°C R,m² °C/W
145 0.5800 0.0004
LMTD Corrected LMTD
Step. 4 Bundle and Shell diameter Step. 5 Tube side heat transfer coefficient
-9 -10 1050 2.300 4.36
3.5 3.5
Step 2. Input tubing OD, BWG and length (can be trial and error).
No. of
Step 6. Shell side heat transfer coefficient
°C °C
Tube OD BWG
0.0125 16
m
Tube ID, d = Tube Length, L =
0.00925 2
m m
Area of one tube = Cross sectional area of tube =
0.079 0.00007
m² m²
Bundle diameter =
0.417758
m
Shell diameter = Tubeside Reynolds No., NRe =
0.430258 7382
m
page number 648
page number 665
Prandtl No. = Length / ID = jh
5.24 216 0.0032
Nusselt number =
40.80 165.86
hi =
The values in this block will keep on changing
Project No.: By:
W/m² °C
Segmental baffle cut 25% page numbe
xchanger Design Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
Step 3. Start configuring the exchanger. Begin with the assumed overall heat transfer coefficient to this point: Ustart = 1000.00 W/m² °C Then the required transfer A = Number of tubes required = No. of passes = Tubes per pass = Area of tubes per pass = Volumetric flow = Av. Velocity =
2
41.714 531 4 134 0.00900 0.001254 0.139284
m
Tube Pitch = Pattern = Baffle Spacing = Area of Shell = Equivalent Diameter, de =
0.015625 Tri. 0.237 0.020363 0.008876
m
Volumetric flowrate = Shellside velocity = Shellside Reynolds No., NRe =
0.031660 1.55 6,300
m³/s m/s
Step 6. Shell side heat transfer coefficient
Prandtl No. = Segmental baffle cut 25% page number 673 jh =
17 0.0070
Nusselt number = ho =
114 7,444
R1 = R2 = R3 = R4 = Overall heat transfer coefficient =
132.85 m² m³/s m/s
12 13 14 15 16
m m² m
W/m² °C
0.00013 0.00040 0.000042 0.0087 107.9
BWG/Tube Wall Thicknesses 8 9 10 11
For 2 tube passes
W/m² °C
BWG/Tube Wall Thicknesses 0.165 0.148 0.134 0.120
0.017 0.014 0.014
0.109 0.095 0.083 0.072 0.065
0.011 0.014 0.012 0.011 0.007
k1 n1 Clearance
For 2 t.p For 4 t.p For 6 t.p 0.249 0.175 0.0743 2.207 2.285 2.499 0.0125
page number 649 page number 649 page number 646
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
Shell and Tube Heat Exchanger Design Spreadsheet Project: Item No.:
Evaporator -
Service:
Project No.: By:
Water cooler
Step 5. Start configuring the exchanger. Begin wit this point
Step 1. Input flows, conditions and properties data for shellside and tubeside Tube
Side
Shell
R-22
Fluid Name
Water
168.5
11,014.1
Av. Density Av. Viscosity Av. Heat Capacity
5 5 0.8053 0.011 0.163
Flow (M), lb/h Temp. in, oF Temp. out, oF r, lb/ft3 m, cP cp, Btu/lb·oF
Heat Exchanged Av. Thermal Conductivity
48,000 0.0049
Q, Btu/h k, Btu/h·ft·oF
44,188 0.3351
Fouling Resistance Prandtl No.
0.0040 0.87
R, ft2·h·oF/Btu cpm/k
0.004 13.78
Corrected MTD Corrected MTD
Step 2. Input tubing OD, BWG and length (can be trial and error).
79.0 79.0
Step 3. Estimate the number of tubes per tube pass.
Over all heat transfer Coefficie
86 82 62.42 1.903 1.003
Reset tubes/pass (Step 3), then no. of p
Step 4. Select tube arrangement and estimate shell diameter
o
F F
o
Tube OD BWG Tube ID, d =
0.5000 16 0.370
in.
Tube Length, L = Flow area per tube, at =
2 0.108 0.262
ft. in.2 ft2
Effective transfer area per tube =
Tubes/pass = lb/h per tube = lb/h per tube per pass = Av. velocity, fps = Tubeside Reynolds No., NRe = Tubeside Friction Factor, f = DP per pass, psi = Nusselt number, Nr = Inside Film Coefficient, hi =
MAS
66 3
Equivalent Diameter, de (see
in.
Check: % difference, Ucalc. vs U
1.3 1.18 4,025 0.027 0.00021 7.04 11
Step 6. Check tubeside velocity and DP, shellside D adjust tube length, number of tubes per pass, num baffle spacing. Remember to reset shell diamete required.
n Spreadsheet MAS
Date/Time:
11-Mar-14
8:40
BWG/Tube Wall Thicknesses 8 0.165 9 0.148 10 0.134 11 0.120
Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point: Ustart = 10 Btu/h·ft2·oF Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF ft2 Then the required transfer A = 63 Number of tubes required = 239 Reset tubes/pass (Step 3), then no. of passes = 2 Total tube count = 132 Tubeside DP (incl. returns) = 5.802 psi ft2 Actual effective transfer area, A = 35
elect tube arrangement mate shell diameter
Tube Pitch Pattern
0.65 Tri.
in.
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = Equivalent Diameter, de (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
8 5 4 0.064 7.5 171,820 56,431
in. in.
Shellside Friction Factor = Shellside DP =
0.00153 0.357 139.7 179 9.7 0.0% 10.5
Outside Transfer Factor, jh = Outside Film Coefficient, ho = Calculated Uo = Check: % difference, Ucalc. vs Uassum. = Uclean =
heck tubeside velocity and DP, shellside DP. If too high or too low, ube length, number of tubes per pass, number of passes, and/or shell pacing. Remember to reset shell diameter from tube count tables, as .
ft2
0.017 0.014 0.014
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
MTD Correction Factors R = ( T1 - T2 ) / ( t2 - t1 ) =
#DIV/0!
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.000
( R2 + 1 ) ½ =
#DIV/0!
( 1 - S ) / ( 1 - RS ) =
#DIV/0!
2 - S ( R + 1 - ( R2 + 1 ) ½ ) =
#DIV/0!
2 - S ( R + 1 + ( R2 + 1 ) ½ ) =
#DIV/0!
FT =
#DIV/0!
3.80
in. lb/h·ft2
psi
