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Excel sheet to size heat exchanger by Kern Method.
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HEAT EXCHANGER DESIGN CALCULATION
SHELL SIDE DATA
4000
205
264Inlet Pressure, Ps (psig) = 180
0.002
5
PHYSICAL PROPERTIES OF SHELL SIDE FLUIDINLET MEAN OUTLET
205 234.5 264
0.58 0.595 0.61
0.072 0.07 0.068
41.2 40.6 40Viscosity (cp) 0.284 0.2605 0.237
TUBE SIDE DATA
590
620
250
65
0.005
5
PHYSICAL PROPERTIES OF TUBE SIDE FLUIDINLET MEAN OUTLET
620 435 250
0.76 0.6615 0.563
0.045 0.055 0.065
42 46.3 50.6Viscosity (cp) 0.4 1.3 2.2
CALCULATIONS
Mass Flowrate, ms (lb/hr) =
Inlet Temperature, T1 (oF) =
Outlet Temperature, T2 (oF) =
Fouling Allowance, fs (hrft2oF/Btu) =
Allowable Pressure Drop, dPs (psi) =
Temperature (oF)
Sp. Heat (Btu/lboF)
k (Btuft/hrft2oF)
Density (lb/ft3)
Mass Flowrate, mt (lb/hr) =
Inlet Temperature, t1 (oF) =
Outlet Temperature, t2 (oF) =
Inlet Pressure, Pt (psig) =
Fouling Allowance, ft (hrft2oF/Btu) =
Allowable Pressure Drop, dPt (psi) =
Temperature (oF)
Sp. Heat (Btu/lboF)
k (Btuft/hrft2oF)
Density (lb/ft3)
HEAT DUTY
140420
144405.4
LMTD
150.3673 0.736501
R = 6.27118644 S = 0.142169
0.7365 From Fig. 12.19
110.7455
ESTIMATE LAYOUT
Material use for Shell = Carbon SteelMaterial use for Tubes = Carbon Steel
Tube Outer Diameter (in) = 0.75 Shell pass = 1Tube Length (ft) = 8 Tube pass = 2Pitch (in) = 1
Tube Inner Diameter (in) = 0.5837 From Table 12.3
ESTIMATE OVERALL HEAT TRANSFER COEFFICIENT
6.78
NUMBER OF TUBES
187.0135
1.570795
Number of Tubes = 119.0566= 119
Number of Tubes per pass = 59
0.001858
0.109638
QS (Btu/hr) =
Qt (Btu/hr) =
LMTD (oF) =
FT =
Corrected LMTD (oF) =
Uo (Btu/hrft2oF) =
Ao (ft2) =
Area of One tube (ft2) =
Tube cross-section area (ft2) =
So, Area per pass (ft2) =
0.00354
Tube Side Velocity (ft/s) = 0.032286
BUNDLE & SHELL DIAMETER
0.156 2.291 From Table 12.4
Bundle Diameter (in) = 13.58975
Bundle-Shell Clearence (in) = 2 From Fig. 12.10
Shell Diameter (in) = 12
TUBE SIDE HEAT TRANSFER COEFFICIENT
Reynolds Number = 83.20359Prandtl Number = 37.8378
Length Diameter Ratio = 164.468
0.07 From Fig. 12.23
Nusselt Number = 19.31771
21.84288
BAFFLE SPACING & SHELL SIDE VELOCITY
Baffle Spacing (in) = 2.8
0.058333
0.027367
Shell Side Velocity (ft/s) = 0.469153
SHELL SIDE HEAT TRANSFER COEFFICIENT
Equivalent Diameter (in) = 0.945621
Reynolds Number = 8571.481Prandtl Number = 5.358485
Volumetric Flowrate (ft3/s) =
K1 = n1 =
Jh Factor =
hi (Btu/hrft2oF) =
As (ft2) =
Volumetric Flowrate (ft3/s) =
0.015 From Fig.12.29
198.7437
CALCULATED OVERALL HEAT TRANSFER COEFFICIENT
30 From Table 2-3Ken Arnold Vol:2
13.78507
TUBESIDE PRESSURE DROP
Pt =
L (m) = 2.439024 jf = 0.095di (m) = 0.01483 Np = 2
741.263v (m/s)= 0.009843
Pt = 9.15667798 Pa0.00132843 psi
SHELL SIDE PRESSURE DROP
Ps =
L (m) = 2.439024 jf = 0.05
0.071138 Ds (in) = 0.304878
650.006 de (in) = 0.024025v (m/s)= 0.143035
Ps = 1157.19465 Pa0.16788316 psi
Jh Factor =
hs (Btu/hrft2oF) =
kw (Btu/hrftoF) =
Uo (Btu/hrft2oF) =
Np x (8 x jf x (L/di) + 2.5)(ρ x v2/2)
ρ (Kg/m3) =
8 x jf x (Ds/de) x (L/lB) x (ρ x v2/2)
lB (m) =
ρ (Kg/m3) =
INPUT BOXES
HEAT EXCHANGER DESIGN CALCULATION
SHELL SIDE DATA
4000
205
264Inlet Pressure, Ps (psig) = 180
0.002
5
PHYSICAL PROPERTIES OF SHELL SIDE FLUIDINLET MEAN OUTLET
205 234.5 264
0.58 0.595 0.61
0.072 0.07 0.068
41.2 40.6 40Viscosity (cp) 0.284 0.2605 0.237
TUBE SIDE DATA
590
620
250
65
0.005
5
PHYSICAL PROPERTIES OF TUBE SIDE FLUIDINLET MEAN OUTLET
620 435 250
0.76 0.6615 0.563
0.045 0.055 0.065
42 46.3 50.6Viscosity (cp) 0.4 1.3 2.2
CALCULATIONS
HEAT DUTY
140420
Mass Flowrate, ms (lb/hr) =
Inlet Temperature, T1 (oF) =
Outlet Temperature, T2 (oF) =
Fouling Allowance, fs (hrft2oF/Btu) =
Allowable Pressure Drop, dPs (psi) =
Temperature (oF)
Sp. Heat (Btu/lboF)
k (Btuft/hrft2oF)
Density (lb/ft3)
Mass Flowrate, mt (lb/hr) =
Inlet Temperature, t1 (oF) =
Outlet Temperature, t2 (oF) =
Inlet Pressure, Pt (psig) =
Fouling Allowance, ft (hrft2oF/Btu) =
Allowable Pressure Drop, dPt (psi) =
Temperature (oF)
Sp. Heat (Btu/lboF)
k (Btuft/hrft2oF)
Density (lb/ft3)
QS (Btu/hr) =
144405.4
LMTD
150.3673
R = 6.271186 S = 0.142169
0.7365 From Fig. 12.19
169
ESTIMATE LAYOUT
Material use for Shell = Carbon SteelMaterial use for Tubes = Carbon Steel
Tube Outer Diameter (in) = 0.75 Shell pass = 1Tube Length (ft) = 8 Tube pass = 2Pitch (in) = 1
Tube Inner Diameter (in) = 0.5837 From Table 12.3
ESTIMATE OVERALL HEAT TRANSFER COEFFICIENT
6.78
NUMBER OF TUBES
122.5498
1.570795
Number of Tubes = 78.01769= 78
Number of Tubes per pass = 39
0.001858
0.072472
0.00354
Tube Side Velocity (ft/s) = 0.048842
BUNDLE & SHELL DIAMETER
Qt (Btu/hr) =
LMTD (oF) =
FT =
Corrected LMTD (oF) =
Uo (Btu/hrft2oF) =
Ao (ft2) =
Area of One tube (ft2) =
Tube cross-section area (ft2) =
So, Area per pass (ft2) =
Volumetric Flowrate (ft3/s) =
0.156 2.291 From Table 12.4
Bundle Diameter (in) = 11.30151
Bundle-Shell Clearence (in) = 2 From Fig. 12.10
Shell Diameter (in) = 12
TUBE SIDE HEAT TRANSFER COEFFICIENT
Reynolds Number = 125.8721Prandtl Number = 37.8378
Length Diameter Ratio = 164.468
0.07 From Fig. 12.23
Nusselt Number = 29.22423
33.04436
BAFFLE SPACING & SHELL SIDE VELOCITY
Baffle Spacing (in) = 2.8
0.058333
0.027367
Shell Side Velocity (ft/s) = 0.469153
SHELL SIDE HEAT TRANSFER COEFFICIENT
Equivalent Diameter (in) = 0.945621
Reynolds Number = 8571.481Prandtl Number = 5.358485
0.015 From Fig.12.29
198.7437
CALCULATED OVERALL HEAT TRANSFER COEFFICIENT
30 From Table 2-3Ken Arnold Vol:2
K1 = n1 =
Jh Factor =
hi (Btu/hrft2oF) =
As (ft2) =
Volumetric Flowrate (ft3/s) =
Jh Factor =
hs (Btu/hrft2oF) =
kw (Btu/hrftoF) =
19.01084
TUBESIDE PRESSURE DROP
Pt =
L (m) = 2.439024 jf = 0.095di (m) = 0.01483 Np = 2
741.263v (m/s)= 0.014891
Pt = 20.95621 Pa0.00304 psi
SHELL SIDE PRESSURE DROP
Ps =
L (m) = 2.439024 jf = 0.05
0.071138 Ds (in) = 0.304878
650.006 de (in) = 0.024025v (m/s)= 0.143035
Ps = 1157.195 Pa0.167883 psi
Uo (Btu/hrft2oF) =
Np x (8 x jf x (L/di) + 2.5)(ρ x v2/2)
ρ (Kg/m3) =
8 x jf x (Ds/de) x (L/lB) x (ρ x v2/2)
lB (m) =
ρ (Kg/m3) =
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