Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-404 Fluid Name Sodium Chloride

1.132 Flow (M), Kg/s 33.2

-13 Temp. in, °C -9

-13 Temp. out, °C -10

Av. Density 903 r, Kg/m3

1050

Av. Viscosity 0.158 m, mNs/m2

2.300

Av. Heat Capacity 1.250 cp, kJ/kg°C 4.36

Heat Exchanged 145 Q, kW 145

Av. Thermal Conductivity 0.0376 k, W/m°C 0.5800

Fouling Resistance 0.0004 R,m² °C/W 0.0004

LMTD 3.5 °C

Corrected LMTD 3.5 °C

Step 2. Input tubing OD, BWG and Tube OD 0.0125 m

length (can be trial and error). BWG 16

Tube ID, d = 0.00925 m

Tube Length, L = 2 m

Area of one tube = 0.079 m²

0.00007 m²

page number 648 Bundle diameter = 0.417758 m

Shell diameter = 0.430258 m

7382

5.24

216

page number 665 j h 0.0032

40.80hi = 165.86 W/m² °C

Step 6. Shell side heat transfer

coefficient

Nusselt number =

Step 3. Start configuring the exchanger. Begin with the assumed overall heat transfer

coefficient to this point:

Length / ID =

Step 1. Input flows, conditions and properties data for shellside and tubeside

Prandtl No. =

No. of passes =

Segmental baffle cut 25% page number 673 jh =

The values in this block will keep on changing

Step. 4 Bundle and Shell

diameter

Step. 5 Tube side heat

transfer coefficient

Tubeside Reynolds No., NRe =

Cross sectional area of tube =

Evaporator

Cooling of 23% sodium chloride solution

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8

9

10Ustart = 1000.00 W/m² °C 11

Then the required transfer A = 41.714 m2

12

531 13

4 14

134 132.85 15

0.00900 m² 16

0.001254 m³/s

0.139284 m/s

Tube Pitch = 0.015625 m

Pattern = Tri.

0.237 m

0.020363 m²

0.008876 m

0.031660 m³/s

1.55 m/s

6,300

17

0.0070

114

ho = 7,444 W/m² °C

R1 = 0.00013

R2 = 0.00040 For 2 tube passes

R3 = 0.000042

R4 = 0.0087

Overall heat transfer coefficient = 107.9 W/m² °C

Step 6. Shell side heat transfer

coefficient

Area of Shell =

Equivalent Diameter, de =

Prandtl No. =

Volumetric flowrate =

Baffle Spacing =

Shellside Reynolds No., NRe =

Volumetric flow =

Av. Velocity =

Step 3. Start configuring the exchanger. Begin with the assumed overall heat transfer

coefficient to this point:

Number of tubes required =

No. of passes =

Shellside velocity =

Nusselt number =

Segmental baffle cut 25% page number 673 jh =

-

MAS

Area of tubes per pass =

Tubes per pass =

BWG/Tube Wall Thicknesses

0.165

0.148 0.017

0.134 0.014

0.120 0.014

0.109 0.011

0.095 0.014

0.083 0.012

0.072 0.011

0.065 0.007

For 2 t.p For 4 t.p For 6 t.p

k1 0.249 0.175 0.0743

n1 2.207 2.285 2.499

Clearance 0.0125 page number 646

page number 649

page number 649

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Project: Project No.:

Item No.: - Service: By:

Tube Side Shell

R-22 Fluid Name Water Over all heat transfer Coefficient, Uo =

168.5 Flow (M), lb/h 11,014.1

5 Temp. in, oF 86

5 Temp. out, oF 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 r, lb/ft3

62.42

Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 cp, Btu/lb·oF 1.003

Heat Exchanged 48,000 Q, Btu/h 44,188

Av. Thermal Conductivity 0.0049 k, Btu/h·ft·oF 0.3351

Fouling Resistance 0.0040 R, ft2·h·

oF/Btu 0.004 Step 4. Select tube arrangement

Prandtl No. 0.87 cpm/k 13.78 and estimate shell diameter

Corrected MTD 79.0oF

Corrected MTD 79.0oF

Step 2. Input tubing OD, BWG and Tube OD 0.5000 in. Equivalent Diameter, de (see table) =

length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.

Tube Length, L = 2 ft.

Flow area per tube, at = 0.108 in.2

Effective transfer area per tube = 0.262 ft2

Step 3. Estimate the number of Tubes/pass = 66 Check: % difference, Ucalc. vs Uassum. =

tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3

Av. velocity, fps = 1.18

Tubeside Reynolds No., NRe = 4,025

Tubeside Friction Factor, f = 0.027

DP per pass, psi = 0.00021

Nusselt number, Nr = 7.04

Inside Film Coefficient, hi = 11

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

Evaporator -

Water cooler MAS

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point:

Shell and Tube Heat Exchanger Design Spreadsheet

Date/Time: 4-Mar-14 8:33 BWG/Tube Wall Thicknesses

8 0.165

9 0.148 0.017

10 0.134 0.014Ustart = 10 Btu/h·ft

2·oF 11 0.120 0.014

Over all heat transfer Coefficient, Uo = 9.7 Btu/h·ft2·oF 12 0.109 0.011

Then the required transfer A = 63 ft2

13 0.095 0.014

Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011

Total tube count = 132 16 0.065 0.007

Tubeside DP (incl. returns) = 5.802 psi

Actual effective transfer area, A = 35 ft2

MTD Correction Factors

R = ( T1 - T2 ) / ( t2 - t1 ) = #DIV/0!

Step 4. Select tube arrangement Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. S = ( t2 - t1 ) / ( T1 - t1 ) = 0.000

Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. ( R2 + 1 )

½ = #DIV/0!

Number of Baffles = 4 3.80

Flow Area across Bundle, as = 0.064 ft2

( 1 - S ) / ( 1 - RS ) = #DIV/0!

Equivalent Diameter, de (see table) = 7.5 in.

Mass Velocity, Gs = 171,820 lb/h·ft2 2 - S ( R + 1 - ( R

2 + 1 )

½ ) = #DIV/0!

Shellside Reynolds No., NRe = 56,431

Shellside Friction Factor = 0.00153 2 - S ( R + 1 + ( R2 + 1 )

½ ) = #DIV/0!

Shellside DP = 0.357 psi

Outside Transfer Factor, jh = 139.7 FT = #DIV/0!

Outside Film Coefficient, ho = 179

Calculated Uo = 9.7

Check: % difference, Ucalc. vs Uassum. = 0.0%

Uclean = 10.5

Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

adjust tube length, number of tubes per pass, number of passes, and/or shell

baffle spacing. Remember to reset shell diameter from tube count tables, as

required.

-

MAS

Step 5. Start configuring the exchanger. Begin with the total calculated transfer coefficient to

this point: