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Lampiran 1: Perhitungan Nilai RD Dan Pressure Drop Desain

This document contains calculations for determining the design heat transfer coefficient (Ud) and pressure drop (ΔP) of a heat exchanger. It includes calculations of mass flow rates, heat duties, temperatures, heat transfer coefficients, clean overall coefficient, dirt factor and pressure drops for both the shell and tube sides.

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Adiyat Adi
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85 views21 pages

Lampiran 1: Perhitungan Nilai RD Dan Pressure Drop Desain

This document contains calculations for determining the design heat transfer coefficient (Ud) and pressure drop (ΔP) of a heat exchanger. It includes calculations of mass flow rates, heat duties, temperatures, heat transfer coefficients, clean overall coefficient, dirt factor and pressure drops for both the shell and tube sides.

Uploaded by

Adiyat Adi
Copyright
© © All Rights Reserved
We take content rights seriously. If you suspect this is your content, claim it here.
Available Formats
Download as DOC, PDF, TXT or read online on Scribd
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LAMPIRAN 1

Perhitungan Nilai Rd dan Pressure drop Desain

1. Komposisi
a.
Acid gas
Density : 1,036 kg/m3
Mass Rate : 9979 kg/hr
Berat Molekul : 32,03 kg/kmol
Specific Gravity :1
b.
Steam
Mass Rate : 903 kg/hr
Berat molekul : 18,02 kg/kmol
Specific Gravity : 0,998

Mass Rate Total = 10882 kg/hr


2. Data tiap arus
a.
Shell Side (cold fluid)
Komponene : Steam
Vapour : 187 kg/hr
Liquid : 716 kg/hr
Temperatur 1(t1) : 130oC
Temperatur 2 (t2) : 210 oC
: 80
b.
Tube side (hot fluid)
Komponene : acid gas
Vapour : 7977 kg/hr
Liquid : 2002 kg/hr
Temperatur 1(T1) : 300,6oC
Temperatur 2 (T2) : 175 oC
: 125,6 oC

3. Duty
Cp cold : 1,032 Kcal/kgoC
Cp Hot : 0,282 Kcal/kg oC
Panas latent : 497,5 kcal/kg
a.
Q cold
Q Sensible = m x Cp x T
Q latent =mx
Q cold = 67640,160 kcal/h
= 78665,50608 W
b.
Q hot
Q Sensible = m x Cp x T
Q hot = 282538,9584 kcal/h

xiii
= 2507747 W
4. DataSheet Heat Exchanger
a.
Number of shell pass =1
b.
Number of tube pass =1
c.
Baffle Spacing = 60,96 mm
d.
Jumlah Baffle =4
e.
Number of Tube/Shell = 35
f.
ID Shell = 304,8 mm
g.
Length Tube = 3000 mm
h.
OD Tube = 25,4 mm
i.
Thickness = 2,108 mm
j.
ID Tube = 21,1836 mm
k.
Tube Pitch (Pt) = 31,8 mm
l.
BWG = 14
m.
Flow Area = 0,546 in2 = 0,000352257 m2
5. Log Mean Temperature Difference

= 65,1622454 oC

6. Caloric Temperature
= 0,497
o
API = (141,5/1)-131,5
= 10
Kc = 1 (figure 17, Kern)
Fc = 0,4 (figure 17, Kern)
Tc = T2 + Fc(T1-T2) = 225,24 oC
tc = t1 + Fc(t2-t1) = 162 oC
7. Flow Area Shell
ID Shell = 0,3048 m
C = Pt - OD tube
= 0,0064 m
B = 0,06096 m
Pt = 0,0318 m
ID C ' B
as = 0,00374 m2
Pt
8. Mass Rate Shell
m
Gs = 191469,784 kg/m2hr
as
9. Bilangan reynold shell
= 0,146 cp
= 0,5256 kg/m hr
De = 0,025146 m

De Gs
N Re = 9160,386583

xiv
10. Menentukan nilai Jh dari figure 28 Kern
jH = 45
11. Menghitung nilai ho
o
API = 10
k = 446,68 kcal/m.hr.oC
= 0,324 kg/m hr
k(c/k)1/3 = 5,713 BTU/hr (ft2) (oF/ft)
= 16,733 W/m2 (oC/m)
1
ho k c 3
jH
s De k

ho = 29943,663 W/m2 oC
12. Menghitung flow area tube
N t a 't
at = 0,0123 m2
n
13. Mass rate tube
m
Gt = 647010,7132 kg/m2hr
at

14. NRe tube


= 0,022 cp
= 0,0792 kg/ m hr
ID tube = 21,1836 mm
= 0,02118 m

ID Gt
N Re

NRe = 173055,7594

15. jH = 230 (figure 24, Kern)

16. Menghitung hio


o
API = 10,284
= 0,0792 kg/m hr
k(c/k)1/3 = 4,6591 BTU/hr (ft2) (oF/ft)
= 13,6464 W/m2 (oC/m)
1
hi k c 3
jH
t ID k

hi = 148165,4112 W/m2 oC
IDTube
hio hi
ODTube
hio = 123569,9529 W/m2 oC

17. Tube Wall Temperature (tW)

xv
s t 1
ho
s
tw tc (Tc tc)
ho hio
s t
= 174,3353 oC

18. Clean Overall Coefficient Uc


hio ho
Uc
hio ho
= 24102,98903 W/m2 oC

19. Design Overall Coefficient UD


OD Tube = 0,0254 m
A Tube = 2667 m2
A Shell = 60,295 m2
Q
UD
A t
UD Shell = 19,8150 W/m2 oC
UD Tube = 14,4300 W/m2 oC

20. Dirt Factor (RD)


Uc Ud
Rd
UcxUd
Rd Shell = 0,0504 m2.oC/W
= 0,0057 m2.hr.oC/kcal
Rd Tube = 0,0693 m2.oC/W
= 0,0081 m2.hr.oC/kcal

21. Pressure Drop


a.
Shell Side
NRe = 9160,386583
L =3m
B = 60,96 m
IDs = 0,3048 m
De = 0,025146 m
Gs = 191469,784 kg/m2 hr
= 53,1861 kg/m2 s

xvi
f = e0,576 0,19 ln(Nre)
= 0,31433
L
f Gs 1 1 IDs
Ps B
2 De s

= 255,987 Pa
= 0,00261 kg/cm2

b.
Tube Side
V = 173,4799 m/s
L =3m
OD = 0,0254 m
No. Pass =1
Nre = 173055
f = (1,58ln(Nre)- 3,28)-2
= 0,0040
L Np
Pt 2 f 2 Np s V 2
IDs
= 530,0114 Pa
= 0,00540 kg/cm2

LAMPIRAN 2

Perhitungan Nilai Rd dan Pressure drop aktual

1. Komposisi
a.
Acid gas
Density : 1,036 kg/m3
Mass Rate : 2994,7 kg/hr
Berat Molekul : 32,03 kg/kmol
Specific Gravity :1
b.
Steam
Mass Rate : 270,9 kg/hr
Berat molekul : 18,02 kg/kmol
Specific Gravity : 0,998

2. Data tiap arus

xvii
a.
Shell Side (cold fluid)
Komponene : Steam
Vapour : 56,1 kg/hr
Liquid : 214,8 kg/hr
Temperatur 1(t1) : 130oC
Temperatur 2 (t2) : 210 oC
: 80
b.
Tube side (hot fluid)
Komponene : acid gas
Vapour : 2393,1 kg/hr
Liquid : 600,6 kg/hr
Temperatur 1(T1) : 300,6oC
Temperatur 2 (T2) : 175 oC
: 125,6 oC

3. Duty
Cp cold : 1,032 Kcal/kgoC
Cp Hot : 0,282 Kcal/kg oC
Panas latent : 497,5 kcal/kg
a.
Q cold
Q Sensible = m x Cp x T
Q latent =mx
Q cold = 6087,614 kcal/h
= 7079,895547 W
b.
Q hot
Q Sensible = m x Cp x T
Q hot = 25428,50626 kcal/h
= 225697,2764 W
4. DataSheet Heat Exchanger
a.
Number of shell pass =1
b.
Number of tube pass =1
c.
Baffle Spacing = 60,96 mm
d.
Jumlah Baffle =4
e.
Number of Tube/Shell = 35
f.
ID Shell = 304,8 mm
g.
Length Tube = 3000 mm
h.
OD Tube = 25,4 mm
i.
Thickness = 2,108 mm
j.
ID Tube = 21,1836 mm
k.
Tube Pitch (Pt) = 31,8 mm
l.
BWG = 14
m.
Flow Area = 0,546 in2 = 0,000352257 m2
5. Log Mean Temperature Difference

xviii
= 65,1622454 oC

6. Caloric Temperature
= 0,497
o
API = (141,5/1)-131,5
= 10
Kc = 1 (figure 17, Kern)
Fc = 0,4 (figure 17, Kern)
Tc = T2 + Fc(T1-T2) = 225,24 oC
tc = t1 + Fc(t2-t1) = 162 oC
7. Flow Area Shell
ID Shell = 0,3048 m
C = Pt - OD tube
= 0,0064 m
B = 0,06096 m
Pt = 0,03 m
ID C ' B
as = 0,00374 m2
Pt
8. Mass Rate Shell
m
Gs = 57440,93519 kg/m2hr
as
9. Bilangan reynold shell
= 0,146 cp
= 0,5256 kg/m hr
De = 0,025146 m

De Gs
N Re = 2748,115975

10. Menentukan nilai Jh dari figure 28 Kern
jH = 23
11. Menghitung nilai ho
o
API = 10
k = 446,68 kcal/m.hr.oC
= 0,324 kg/m hr
k(c/k)1/3 = 5,713 BTU/hr (ft2) (oF/ft)
= 16,733 W/m2 (oC/m)
1
ho k c 3
jH
s De k

ho = 29943,663 W/m2 oC
12. Menghitung flow area tube
N t a 't
at = 0,0123 m2
n

xix
13. Mass rate tube
m
Gt = 194103,214 kg/m2hr
at

14. NRe tube


= 0,022 cp
= 0,0792 kg/ m hr
ID tube = 21,1836 mm
= 0,02118 m

ID Gt
N Re

NRe = 51916,7278

15. jH = 19 (figure 24, Kern)

16. Menghitung hio


o
API = 10,284
= 0,0792 kg/m hr
k(c/k)1/3 = 4,6591 BTU/hr (ft2) (oF/ft)
= 13,6464 W/m2 (oC/m)
1
hi k c 3
jH
t ID k

hi = 12239,75136 W/m2 oC
IDTube
hio hi
ODTube
hio = 10207,95263 W/m2 oC

17. Tube Wall Temperature (tW)


s t 1
ho
s
tw tc (Tc tc)
ho hio
s t
= 245,0256534 oC

18. Clean Overall Coefficient Uc


hio ho
Uc
hio ho
= 6123,588802 W/m2 oC

19. Design Overall Coefficient UD


OD Tube = 0,0254 m

xx
A Tube = 2667 m2
A Shell = 60,295 m2
Q
UD
A t
UD Shell = 5,9444 W/m2 oC
UD Tube = 4,3289 W/m2 oC

20. Dirt Factor (RD)


Uc Ud
Rd
UcxUd
Rd Shell = 0,1681 m2.oC/W
= 0,0195 m2.hr.oC/kcal
Rd Tube = 0,2308 m2.oC/W
= 0,0268 m2.hr.oC/kcal

21. Pressure Drop


a.
Shell Side
NRe = 2748,115975
L =3m
B = 60,96 m
IDs = 0,3048 m
De = 0,025146 m
Gs = 57440,93519 kg/m2 hr
= 15,9558 kg/m2 s
f = e0,576 0,19 ln(Nre)
= 0,3951
L
f Gs 1 1 IDs
Ps B
2 De s

= 28,9606 Pa
= 0,00029 kg/cm2

b.
Tube Side
V = 52,0440 m/s
L =3m
OD = 0,0254 m
No. Pass =1

xxi
Nre = 51916,72782
f = (1,58ln(Nre)- 3,28)-2
= 0,0052
L Np
Pt 2 f 2 Np s V 2
IDs
= 173,9960 Pa
= 0,001773 kg/cm2

xxii
DATA SPESIFIKASI ALAT 94-E-402

xxiii
APPENDIX

xxiv
xxv
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xxviii
xxix
xxx
xxxi
xxxii
xxxiii

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