[xls] · web viewshell id from tube count tables corrected mtd select baffle spacing number of...

Shell and Tube Heat Exchanger Design SpreadsheetProject: Evaporator Project No.: Item No.: - Service: Cooling of 23% sodium chloride solution By:

Tube Side ShellR-404 Fluid Name Sodium Chloride1.132 Flow (M), Kg/s 33.2

-13 -9 No. of passes =-13 -10

Av. Density 903 1050Av. Viscosity 0.158 2.300

Av. Heat Capacity 1.250 4.36Heat Exchanged 145 Q, kW 145

Av. Thermal Conductivity 0.0376 0.5800Fouling Resistance 0.0004 0.0004

LMTD 3.5Corrected LMTD 3.5

Tube OD 0.0125 m length (can be trial and error). BWG 16

Tube ID, d = 0.00925 mTube Length, L = 2 m

Area of one tube = 0.079Cross sectional area of tube = 0.00007

page number 648 Bundle diameter = 0.417758 mShell diameter = 0.430258 m

7382Prandtl No. = 5.24Length / ID = 216

page number 665 0.0032Nusselt number = 40.80

165.86

The values in this block will keep on changing

Step 1. Input flows, conditions and properties data for shellside and tubeside Step 3. Start configuring the exchanger. Begin with the assumed overall heat transfer coefficient to this point:

Temp. in, °CTemp. out, °C

r, Kg/m3

m, mNs/m2

cp, kJ/kg°C

k, W/m°CR,m² °C/W Step 6. Shell side heat transfer

coefficient

°C°C

Step 2. Input tubing OD, BWG and

Segmental baffle cut 25% page number 673 jh =

m²m²

Step. 4 Bundle and Shell diameter

Step. 5 Tube side heat transfer coefficient

Tubeside Reynolds No., NRe =

j h

hi = W/m² °C

Shell and Tube Heat Exchanger Design Spreadsheet-

MAS Date/Time: 6-May-23 13:00 BWG/Tube Wall Thicknesses89

101000.00 11

Then the required transfer A = 41.714 12Number of tubes required = 531 13

No. of passes = 4 14Tubes per pass = 134 132.85 15

Area of tubes per pass = 0.00900 16Volumetric flow = 0.001254

Av. Velocity = 0.139284 m/s

Tube Pitch = 0.015625 mPattern = Tri.

Baffle Spacing = 0.237 mArea of Shell = 0.020363

0.008876 mVolumetric flowrate = 0.031660

Shellside velocity = 1.55 m/s6,300

Prandtl No. = 170.0070

Nusselt number = 1147,444

R1 = 0.00013R2 = 0.00040 For 2 tube passesR3 = 0.000042

R4 = 0.0087Overall heat transfer coefficient = 107.9

Step 3. Start configuring the exchanger. Begin with the assumed overall heat transfer coefficient to this point:

Ustart = W/m² °Cm2

m²m³/s

Step 6. Shell side heat transfer coefficient

m²Equivalent Diameter, de =

m³/s

Shellside Reynolds No., NRe =

Segmental baffle cut 25% page number 673 jh =

ho = W/m² °C

W/m² °C

BWG/Tube Wall Thicknesses0.1650.148 0.0170.134 0.0140.120 0.0140.109 0.0110.095 0.0140.083 0.0120.072 0.0110.065 0.007

For 2 t.p For 4 t.p For 6 t.p0.249 0.175 0.0743 page number 6492.207 2.285 2.499 page number 649

Clearance 0.0125 page number 646

k1

n1

Shell and Tube Heat Exchanger Design SpreadsheetProject: Evaporator Project No.: -Item No.: - Service: Water cooler By: MAS

Tube Side ShellR-22 Fluid Name Water168.5 Flow (M), lb/h 11,014.1

5 865 82 Reset tubes/pass (Step 3), then no. of passes =

Av. Density 0.8053 62.42Av. Viscosity 0.011 m, cP 1.903

Av. Heat Capacity 0.163 1.003Heat Exchanged 48,000 Q, Btu/h 44,188


Prandtl No. 0.87 13.78 and estimate shell diameterCorrected MTD 79.0Corrected MTD 79.0

Tube OD 0.5000 in. length (can be trial and error). BWG 16

Tube ID, d = 0.370 in.Tube Length, L = 2 ft.

0.108Effective transfer area per tube = 0.262

Tubes/pass = 66 tubes per tube pass. lb/h per tube = 3

lb/h per tube per pass = 1.3Av. velocity, fps = 1.18

4,025Tubeside Friction Factor, f = 0.027

0.00021 adjust tube length, number of tubes per pass, number of passes, and/or shellNusselt number, Nr = 7.04 baffle spacing. Remember to reset shell diameter from tube count tables, as

11 required.

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:

Over all heat transfer Coefficient, Uo =

Temp. in, oFTemp. out, oF

r, lb/ft3

cp, Btu/lb·oF

k, Btu/h·ft·oF R, ft2·h·oF/Btu Step 4. Select tube arrangement

cpm/koFoF

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

Flow area per tube, at = in.2

ft2

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

Tubeside Reynolds No., NRe =Step 6. Check tubeside velocity and DP, shellside DP. If too high or too low,

DP per pass, psi =

Inside Film Coefficient, hi =


MAS Date/Time: 6-May-23 13:00 BWG/Tube Wall Thicknesses8 0.1659 0.148 0.017

10 0.134 0.01410 11 0.120 0.0149.7 12 0.109 0.011

Then the required transfer A = 63 13 0.095 0.014Number of tubes required = 239 14 0.083 0.012

Reset tubes/pass (Step 3), then no. of passes = 2 15 0.072 0.011Total tube count = 132 16 0.065 0.007

5.802 psi Actual effective transfer area, A = 35 MTD Correction Factors

#DIV/0!Tube Pitch 0.65 in.

and estimate shell diameter Pattern Tri. 0.000Shell ID from Tube Count Tables 8 in.

Select Baffle Spacing 5 in. #DIV/0!Number of Baffles = 4 3.80

0.064 ( 1 - S ) / ( 1 - RS ) = #DIV/0!7.5 in.

171,820 #DIV/0!56,431

Shellside Friction Factor = 0.00153 #DIV/0!0.357 psi 139.7 #DIV/0!1799.7

0.0%10.5

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.

Start configuring the exchanger. Begin with the total calculated transfer coefficient to this point:

Ustart = Btu/h·ft2·oF

Over all heat transfer Coefficient, Uo = Btu/h·ft2·oF

ft2

Tubeside DP (incl. returns) =ft2

R = ( T1 - T2 ) / ( t2 - t1 ) = Select tube arrangement

S = ( t2 - t1 ) / ( T1 - t1 ) =

( R2 + 1 ) ½ =

Flow Area across Bundle, as = ft2

Equivalent Diameter, de (see table) =Mass Velocity, Gs = lb/h·ft2 2 - S ( R + 1 - ( R2 + 1 ) ½ ) =

Shellside Reynolds No., NRe =2 - S ( R + 1 + ( R2 + 1 ) ½ ) =

Shellside DP =Outside Transfer Factor, jh = FT =

Outside Film Coefficient, ho =Calculated Uo =

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

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















11 required.




r, lb/ft3

cp, Btu/lb·oF


cpm/koFoF



ft2



DP per pass, psi =
