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Desing of Cooler

The document provides specifications for two fluids in a heat exchanger, including mass flow rates, temperatures, densities, heat capacities, and heat flow. Design calculations are shown for the heat transfer area, numbers of tubes, tube and shell side pressure drops and heat transfer coefficients based on the fluid properties and an assumed overall heat transfer coefficient. Key parameters calculated include a required heat transfer area of 138.86 m2 and shell side pressure drop of 78.32 kPa.

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578 views25 pages

Desing of Cooler

The document provides specifications for two fluids in a heat exchanger, including mass flow rates, temperatures, densities, heat capacities, and heat flow. Design calculations are shown for the heat transfer area, numbers of tubes, tube and shell side pressure drops and heat transfer coefficients based on the fluid properties and an assumed overall heat transfer coefficient. Key parameters calculated include a required heat transfer area of 138.86 m2 and shell side pressure drop of 78.32 kPa.

Uploaded by

meet
Copyright
© © All Rights Reserved
We take content rights seriously. If you suspect this is your content, claim it here.
Available Formats
Download as XLSX, PDF, TXT or read online on Scribd
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First Fluid

Mass flow rate of fluid, m1 45508 kg/hr


Mass Density, q1 855 kg/m3
Inlet temp T1 27 C Sp.Heat Cp11 2.892 KJ/kg. C
Outlet temp T2 50 C Sp.Heat Cp12 2.941 KJ/kg. C
Thermal conductivity of liquid λs 0.32 W/ m.C

Second Fluid
Inlet temp t1 200 C Sp.Heat Cp21 2.627 KJ/kg. C
Outlet temp t2 100 C Sp.Heat Cp22 2.243 KJ/kg. C
Mass Density of liquid q2 763.33 kg/m3 at given temp
Thermal conductivity of liquid λt 0.1046 W/ m.C
Heat Flow of fluid, Φ1 3138504.7 KJ/hr 871.8068688889 Kw

Required mass m2 2.8954064 kg/sec 10423.46306211 kg/hr 12513.6

Assume Recom heat transfer coefficient, U 0 45 W/m².˚C

Provisional heat transfer area, A 186.8030095976 m²


Tube OD, do 0.01905 m 19.05
Tube ID, di 0.015748 m 15.748
Tube length, L 3.6576 m 12
Numbers of tube, Nt 853.81
Tube pitch, Pt 23.8125 mm

Evaluation of hi
Tube side Flow area, at 0.083110042696 m²
Tube side mass velocity, Gt 41.82406707113 kg/ (m².s)
Tube side Reynold number Ret 1675.942514596
2000< Ret < 4000
Tube side velocity, ut 0.054791593506 m/s
Prandtl Number, Pr 19.74017208413
Nu 9.554630502699
Tube side heat transfer coefficient, hi 63.46293818785 W/m².˚C

Evaluation of ho
Baffle spacing, Bs 166.1664896751 mm
Shell side flow area, As 0.027611302291 m²
Shell side mass velocity, Gs 457.8237917904 kg/ (m².s)
Shell side velocity, us 0.535466423147 m/s
Shell side equivalent diameter for Triangular pitch, de 18.81044625 mm 0.01881
Shell side Reynolds number, Re 734.1747508479
Prandtl Number, Pr 106.009875
Nu 1394.200093517
Shell side heat transfer coefficient, ho 23717.88654007 W/m².˚C

Required heat transfer area, Ar 165.9607651259 m²

Shell side pressure Drop:


ΔPs 63875.23 Pa 63.87523

Tube side pressure Drop:


ΔPt 133.4676434575 Pa 0.133468
Hot Fluid
T1 200 C T2 100 C

Cold Fluid
t2 50 C t1 27 C

ΔT1 150 C ΔT2 73 C

ΔTLN 106.9183 C

Number of tube side pass, Np 2


R 4.3478 S 0.133
kg/hr
Ft 0.97 From Fig
Mean temp difference, ΔTm 103.71 C

From Table for nos. of tube pass


k1 0.156
mm n1 2.291
mm
ft Tube bundle diameter, Db 815.832 mm
Clearance between shell ID and D b 15 mm
Shell Inside diameter Ds 831 mm

0.786 Cp
Viscocity of tube side fluid, µt
0.000786 Kg/(m.s)

11.73 Cp
Viscocity of shell side fluid, µs
0.01173 Kg/(m.s)

Heat trasnfer factor, Jh 0.4 for 25% baffles cut

Recommended fouling coefficients


hod 5000 W/m².˚C
m hid 3000 W/m².˚C
Themal conductivity of tube material 50 W/m².˚C

A 0.003626239
1/Uo 0.019743
Uo 50.65134 W/m².˚C
Friction factor, Jf 0.067

Friction factor tube side, Jt 0.03

Kpa

Kpa
Tube sheet thickness
F 1.25
f 16700 psi 115142.5 kpa
p 100 bar 10000 kpa
G 889 mm

t 163.7435

t
First Fluid
Mass flow rate of fluid, m1 45508.1 kg/hr
Mass Density, q1 855 kg/m3
Inlet temp T1 27 C Sp.Heat Cp11 2.892 KJ/kg. C
Outlet temp T2 50 C Sp.Heat Cp12 2.941 KJ/kg. C
Thermal conductivity of liquid λs 0.32 W/ m.C

Second Fluid
Inlet temp t1 200 C Sp.Heat Cp21 2.627 KJ/kg. C
Outlet temp t2 100 C Sp.Heat Cp22 2.243 KJ/kg. C
Mass Density of liquid q2 763.33 kg/m3 at given temp
Thermal conductivity of liquid λt 0.1046 W/ m.C
Heat Flow of fluid, Φ1 3138511.6 KJ/hr 774 Kw

Required mass m2 2.5705746 kg/sec 9254.068415809 kg/hr 13372.5

Assume Recom heat transfer coefficient, U 0 45 W/m².˚C

Provisional heat transfer area, A 165.8458250195 m²


Tube OD, do 0.01905 m 19.05
Tube ID, di 0.015748 m 15.748
Tube length, L 3.6576 m 12
Numbers of tube, Nt 758.03
Tube pitch, Pt 23.8125 mm

Evaluation of hi
Tube side Flow area, at 0.073786036039 m²
Tube side mass velocity, Gt 50.34263300691 kg/ (m².s)
Tube side Reynold number Ret 2017.292072755
2000< Ret < 4000
Tube side velocity, ut 0.065951335604 m/s
Prandtl Number, Pr 19.74017208413
Nu 10.15738901529
Tube side heat transfer coefficient, hi 67.46652851154 W/m².˚C

Evaluation of ho
Baffle spacing, Bs 157.9078511759 mm
Shell side flow area, As 0.024934889463 m²
Shell side mass velocity, Gs 506.9659084575 kg/ (m².s)
Shell side velocity, us 0.592942582991 m/s
Shell side equivalent diameter for Triangular pitch, de 18.81044625 mm 0.01881
Shell side Reynolds number, Re 812.9799634801
Prandtl Number, Pr 106.009875
Nu 1543.851432922
Shell side heat transfer coefficient, ho 26263.72877969 W/m².˚C

Required heat transfer area, Ar 138.8696860656 m²

Shell side pressure Drop:


ΔPs 78323.72 Pa 78.32372

Tube side pressure Drop:


ΔPt 193.3727707655 Pa 0.193373
Hot Fluid
T1 200 C T2 100 C

Cold Fluid
t2 50 C t1 27 C

ΔT1 150 C ΔT2 73 C

ΔTLN 106.9183 C

Number of tube side pass, Np 2


R 4.3478 S 0.133
kg/hr
Ft 0.97 From Fig
Mean temp difference, ΔTm 103.71 C

From Table for nos. of tube pass


k1 0.156
mm n1 2.291
mm
ft Tube bundle diameter, Db 774.539 mm
Clearance between shell ID and D b 15 mm
Shell Inside diameter Ds 790 mm

0.786 Cp
Viscocity of tube side fluid, µt
0.000786 Kg/(m.s)

11.73 Cp
Viscocity of shell side fluid, µs
0.01173 Kg/(m.s)

Heat trasnfer factor, Jh 0.4 for 25% baffles cut

Recommended fouling coefficients


hod 5000 W/m².˚C
m hid 3000 W/m².˚C
Themal conductivity of tube material 50 W/m².˚C

A 0.003626239
1/Uo 0.018608
Uo 53.74148 W/m².˚C
Friction factor, Jf 0.067

Friction factor tube side, Jt 0.03

Kpa

Kpa
Tube sheet thickness
F 1.25
f 16700 psi 115142.5 kpa
p 35 bar 3500 kpa
G 864 mm

t 94.14777

t
First Fluid
Mass flow rate of fluid, m1 20398.4 kg/hr
Mass Density, q1 892.7 kg/m3
Inlet temp T1 49.92 C Sp.Heat Cp11 2.066 KJ/kg. C
Outlet temp T2 92.87 C Sp.Heat Cp12 2.222 KJ/kg. C
Thermal conductivity of liquid λs 0.17 W/ m.C

Second Fluid
Inlet temp t1 111.4 C Sp.Heat Cp21 2.039 KJ/kg. C
Outlet temp t2 55 C Sp.Heat Cp22 1.813 KJ/kg. C
Mass Density of liquid q2 862.51 kg/m3 at given temp
Thermal conductivity of liquid λt 0.1143 W/ m.C
Heat Flow of fluid, Φ1 2105572.2 KJ/hr 549 Kw

Required mass m2 4.3082612 kg/sec 15509.74028012 kg/hr 17993.7

Assume Recom heat transfer coefficient, U 0 45 W/m².˚C

Provisional heat transfer area, A 1209.720702982 m²


Tube OD, do 0.01905 m 19.05
Tube ID, di 0.015748 m 15.748
Tube length, L 6.096 m 20
Numbers of tube, Nt 3317.54
Tube pitch, Pt 25 mm

Evaluation of hi
Tube side Flow area, at 0.322928220991 m²
Tube side mass velocity, Gt 15.4778977962 kg/ (m².s)
Tube side Reynold number Ret 1339.263376344
2000< Ret < 4000
Tube side velocity, ut 0.017945180689 m/s
Prandtl Number, Pr 6.493403324584
Nu 5.194146021626
Tube side heat transfer coefficient, hi 37.69944693116 W/m².˚C

Evaluation of ho
Baffle spacing, Bs 745.1688781002 mm
Shell side flow area, As 0.264311688679 m²
Shell side mass velocity, Gs 21.43765283532 kg/ (m².s)
Shell side velocity, us 0.02401439771 m/s
Shell side equivalent diameter for Triangular pitch, de 22.67476916667 mm 0.022675
Shell side Reynolds number, Re 220.9517406891
Prandtl Number, Pr 53.47294117647
Nu 333.8521664459
Shell side heat transfer coefficient, ho 2502.99651911 W/m².˚C

Required heat transfer area, Ar 1803.316911219 m²

Shell side pressure Drop:


ΔPs 74.18 Pa 0.074185

Tube side pressure Drop:


ΔPt 26.49859634954 Pa 0.026499
Hot Fluid
T1 111.41 C T2 55 C

Cold Fluid
t2 92.87 C t1 49.92 C

ΔT1 18.54 C ΔT2 5.08 C

ΔTLN 10.39688 C

Number of tube side pass, Np 2


R 1.3134 S 0.698
kg/hr
Ft 0.97 From Fig
Mean temp difference, ΔTm 10.08 C

From Table for nos. of tube pass


k1 0.156
mm n1 2.291
mm
ft Tube bundle diameter, Db 1475.338 mm
Clearance between shell ID and D b 15 mm
Shell Inside diameter Ds 1490 mm

0.364 Cp
Viscocity of tube side fluid, µt
0.000364 Kg/(m.s)

4.4 Cp
Viscocity of shell side fluid, µs
0.0044 Kg/(m.s)

Heat trasnfer factor, Jh 0.4 for 25% baffles cut

Recommended fouling coefficients


hod 5000 W/m².˚C
m hid 3000 W/m².˚C
Themal conductivity of tube material 50 W/m².˚C

A 0.003626239
1/Uo 0.033126
Uo 30.18739 W/m².˚C
Friction factor, Jf 0.067

Friction factor tube side, Jt 0.03

Kpa

Kpa
Tube sheet thickness
F 1.25
f 16700 psi 115142.5 kpa
p 35 bar 1000 kpa
G 870 mm

t 50.67357

t
First Fluid
Mass flow rate of fluid, m1 20398.4 kg/hr
Mass Density, q1 881.42 kg/m3
Inlet temp T1 92.81 C Sp.Heat Cp11 2.222 KJ/kg. C
Outlet temp T2 112 C Sp.Heat Cp12 2.274 KJ/kg. C
Thermal conductivity of liquid λs 0.17 W/ m.C

Second Fluid
Inlet temp t1 200 C Sp.Heat Cp21 2.627 KJ/kg. C
Outlet temp t2 100 C Sp.Heat Cp22 2.243 KJ/kg. C
Mass Density of liquid q2 763.33 kg/m3 at given temp
Thermal conductivity of liquid λt 0.1046 W/ m.C
Heat Flow of fluid, Φ1 988591.73 KJ/hr 774 Kw

Required mass m2 2.5705746 kg/sec 9254.068415809 kg/hr 9254

Assume Recom heat transfer coefficient, U 0 45 W/m².˚C

Provisional heat transfer area, A 549.5888287687 m²


Tube OD, do 0.01905 m 19.05
Tube ID, di 0.015748 m 15.748
Tube length, L 6.096 m 20
Numbers of tube, Nt 1507.19
Tube pitch, Pt 25 mm

Evaluation of hi
Tube side Flow area, at 0.146709684569 m²
Tube side mass velocity, Gt 17.52137606399 kg/ (m².s)
Tube side Reynold number Ret 1031.501421517
2000< Ret < 4000
Tube side velocity, ut 0.022953868005 m/s
Prandtl Number, Pr 13.43637667304
Nu 6.057740320789
Tube side heat transfer coefficient, hi 40.23619745711 W/m².˚C

Evaluation of ho
Baffle spacing, Bs 212.102467632 mm
Shell side flow area, As 0.053535073563 m²
Shell side mass velocity, Gs 105.8413082324 kg/ (m².s)
Shell side velocity, us 0.120080447723 m/s
Shell side equivalent diameter for Triangular pitch, de 22.67476916667 mm 0.022675
Shell side Reynolds number, Re 3053.342534947
Prandtl Number, Pr 10.27348235294
Nu 2659.189112333
Shell side heat transfer coefficient, ho 19936.79167244 W/m².˚C

Required heat transfer area, Ar 760.5937979796 m²

Shell side pressure Drop:


ΔPs 4578.62 Pa 4.578618

Tube side pressure Drop:


ΔPt 38.36958928315 Pa 0.03837
Hot Fluid
T1 200 C T2 100 C

Cold Fluid
t2 112 C t1 92.81 C

ΔT1 88 C ΔT2 7.19 C

ΔTLN 32.26405 C

Number of tube side pass, Np 2


R 5.211 S 0.179
kg/hr
Ft 0.97 From Fig
Mean temp difference, ΔTm 31.30 C

From Table for nos. of tube pass


k1 0.156
mm n1 2.291
mm
ft Tube bundle diameter, Db 1045.512 mm
Clearance between shell ID and D b 15 mm
Shell Inside diameter Ds 1061 mm

0.535 Cp
Viscocity of tube side fluid, µt
0.000535 Kg/(m.s)

0.786 Cp
Viscocity of shell side fluid, µs
0.000786 Kg/(m.s)

Heat trasnfer factor, Jh 0.4 for 25% baffles cut

Recommended fouling coefficients


hod 5000 W/m².˚C
m hid 3000 W/m².˚C
Themal conductivity of tube material 50 W/m².˚C

A 0.003626239
1/Uo 0.030754
Uo 32.51604 W/m².˚C
Friction factor, Jf 0.067

Friction factor tube side, Jt 0.03

Kpa

Kpa
Tube sheet thickness
F 1.25
f 16700 psi 115142.5 kpa
p 385 bar 38500 kpa
G 1200 mm

t 433.6845

t
First Fluid
Mass flow rate of fluid, m1 5489.8 kg/hr
Mass Density, q1 286.03 kg/m3
Inlet temp T1 27 C Sp.Heat Cp11 3.235 KJ/kg. C
Outlet temp T2 112.5 C Sp.Heat Cp12 3.117 KJ/kg. C
Thermal conductivity of liquid λs 0.0942 W/ m.C

Second Fluid
Inlet temp t1 200 C Sp.Heat Cp21 2.627 KJ/kg. C
Outlet temp t2 100 C Sp.Heat Cp22 2.243 KJ/kg. C
Mass Density of liquid q2 763.33 kg/m3 at given temp
Thermal conductivity of liquid λt 0.1046 W/ m.C
Heat Flow of fluid, Φ1 1445560.4 KJ/hr 401.54455875 Kw

Required mass m2 1.333592 kg/sec 4800.931290269 kg/hr 6112

Assume Recom heat transfer coefficient, U 0 34 W/m².˚C

Provisional heat transfer area, A 152.1331277887 m²


Tube OD, do 0.01905 m 19.05
Tube ID, di 0.015748 m 15.748
Tube length, L 3.048 m 10
Numbers of tube, Nt 834.42
Tube pitch, Pt 23.8125 mm

Evaluation of hi
Tube side Flow area, at 0.081222186558 m²
Tube side mass velocity, Gt 18.77497404418 kg/ (m².s)
Tube side Reynold number Ret 16517.78163396
2000< Ret < 4000
Tube side velocity, ut 0.024596143272 m/s
Prandtl Number, Pr 1.229437367304
Nu 8.637728976944
Tube side heat transfer coefficient, hi 51.6684067582 W/m².˚C

Evaluation of ho
Baffle spacing, Bs 164.5382245525 mm
Shell side flow area, As 0.027072827339 m²
Shell side mass velocity, Gs 62.71150613586 kg/ (m².s)
Shell side velocity, us 0.219248002433 m/s
Shell side equivalent diameter for Triangular pitch, de 18.81044625 mm 0.01881
Shell side Reynolds number, Re 1500.803327513
Prandtl Number, Pr 19.74017208413
Nu 1625.664744308
Shell side heat transfer coefficient, ho 8141.094415227 W/m².˚C

Required heat transfer area, Ar 125.0439862459 m²

Shell side pressure Drop:


ΔPs 2985.41 Pa 2.985407

Tube side pressure Drop:


ΔPt 22.60546085302 Pa 0.022605
Hot Fluid
T1 200 C T2 100 C

Cold Fluid
t2 112.5 C t1 27 C

ΔT1 87.5 C ΔT2 73 C

ΔTLN 80.03119 C

Number of tube side pass, Np 2


R 1.1696 S 0.494
kg/hr
Ft 0.97 From Fig
Mean temp difference, ΔTm 77.63 C

From Table for nos. of tube pass


k1 0.156
mm n1 2.291
mm
ft Tube bundle diameter, Db 807.691 mm
Clearance between shell ID and D b 15 mm
Shell Inside diameter Ds 823 mm

0.0358 Cp
Viscocity of tube side fluid, µt
0.0000358 Kg/(m.s)

0.786 Cp
Viscocity of shell side fluid, µs
0.000786 Kg/(m.s)

Heat trasnfer factor, Jh 0.4 for 25% baffles cut

Recommended fouling coefficients


hod 5000 W/m².˚C
m hid 3000 W/m².˚C
Themal conductivity of tube material 50 W/m².˚C

A 0.003626239
1/Uo 0.024175
Uo 41.36565 W/m².˚C
Friction factor, Jf 0.067

Friction factor tube side, Jt 0.03

Kpa

Kpa
Tube sheet thickness
F 1.25
f 16700 psi 115142.5 kpa
p 100 bar 10000 kpa
G 864 mm

t 159.1388

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