Fix 17. Lampiran 2 Perhitungan Desain
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Transcript of Fix 17. Lampiran 2 Perhitungan Desain
Perhitungan Kinerja Heat Exchanger 116-C Secara Desain
Diketahui:
SHELL (COOLING WATER)
t1 = 33 oC
= 33 x 1,8
= 59,4 oF
t2 = 47 oC
= 47 x 1,8
= 84,6 oF
t2 – t1 = (84,6 – 59,4) oF........................................................................(Kern, Hal.85)
= 25,2 oF
w = 178.000 kg/hr ..........(Tabel Pengukuran Flow Cooling Water dengan Flow meter
KURITA)
= 178.000 kg/hr x 2,2046 Ib/kg
= 392418,8 Ib/hr
TUBE (SYN GAS)
T1 = 164,67 oC
= 164,67 oC x 1,8
= 296,406 oF
T2 = 63,53 oC
= 63,53 oC x 1,8
= 114,354 oF
T1 – T2 = (296,406 – 114,354) oF.............................................................(Kern, Hal.85)
= 182,052 oF
W = 35525,65 kg/hr ............(Tabel Pusri II Synthesis Loop Uprate Case Pada Rate
Operasi 100%)
W = 35525,65 kg/hr x 95,248
100 x 2,2046 Ib/kg
99
= 74598,0888 Ib/hr .......................................... (Tabel Rate Operasi Pada 95,248%)
1. PERHITUNGAN NERACA PANAS
Q = W x C x (T1-T2) = w x c x (t1-t2).......................(Persamaan 5.7 Kern, Hal. 88)
a. Pada Shell (Cooling Water)
Diketahui :
w = 178.000 kg/hr .............................(Tabel Pengukuran Flow Cooling Water)
= 178.000 kg/hr x 2,2046 Ib/kg
= 392418,8 Ib/hr
tavg = t 1+t 2
2
= (59,4+84,6)
2
= 72 oF
C = 4186 J/kg oC.............................(Tabel Pengukuran Flow Cooling Water)
= 4186 J/kg oC x 1 Kcal/ kgC4186 J /kgK
= 1 Kcal/ kg oC = 1 BTU/Ib oF
Maka,
Q = w x c (t2-t1) ..................................................(Persamaan 5.7 Kern, Hal. 88)
= 392418,8 Ib/hr x 1 BTU/IboF x (84,6-59,4) oF
= 9888933,6 BTU/hr
b. Pada Tube (Syn Gas)
Diketahui :
W = 35525,65 kg/hr .....................(Tabel Pusri II Synthesis Loop Uprate Case)
= 35525,65 kg/hr x 95,248
100 x 2,2046 Ib/kg
= 74598,0888 Ib/hr
Rate operasi = 95,248.........................................................(Tabel Rate Operasi)
100
Tavg = T 1+T 2
2
= (164,67+63,53)
2
= 205,38 oF
C = 3332,97 J/kg oK .................(Tabel Pusri II Synthesis Loop Uprate Case)
= 3332,97 J/kg oK x 1 Kcal/ kgC4186 J /kgK
= 0,7960 Kcal/kg oC = 0,7960 BTU/Ib oF
Maka,
Q = W x C (T1-T2) ................................................. (Persamaan 5.7 Kern, Hal. 88)
= 74598,0888 Ib/hr x 0,7960 BTU/Ib oF x (296,406 – 114,354) oF
= 10810262,08 BTU/hr
2. LMTD dan ∆t
Hot Fluida
(oF)Cold Fluida
(oF)
Difference
(oF)
T1 296,406 Higher
Temp
t1 59,4 237,006 ∆t2
T2 114,354 Lower
Temp
t2 84,6 29,754 ∆t1
182,052 Difference 25,2 207,252 (∆t2-∆t1)
(T1-T2) (t2-t1)
101
LMTD =
(T 1−t 1 )−(T 2−t 2)
ln( (T 1−t 1 )(T 2−t 2) ) ................................. (Persamaan 5.14 Kern,
Hal. 89)
=
(296,406−59,4 )−(114,354−84,6 ) F
ln( 296,406−59,4114,354−84,6 )F
= 99,8746 oF
R = T 1−T 2t 2−t 1
....................................................... (Persamaan 5.14 Kern, Hal.
149)
= (296,406−114,354)F
(84,6−59,4 ) F
= 7,2242 oF
S = t 2−t 1T 1−t 1
........................................................ (Persamaan 5.14 Kern, Hal.
149)
= 84,6−59,4 F
296,406−59,4 F
= 0,1063 oF
FT = 0,97 ........................................................................(Fig. 18 Kern Hal 828)
Sehingga,
∆t = LMTD x FT .....................................(Persamaan 7.42 Kern, Hal. 149)
= 99,8746 oF x 0,97
= 96,8783 oF
3. TEMPERATURE AVERAGE (Tavg dan tavg)
tavg = (t 1+t 2)
2
102
= (59,4+84,6 ) F
2
= 72 oF
Tavg = (T 1+T 2)
2
= (296,406+114,354 ) F
2
= 205,38 oF
4. LUAS ALIRAN (as dan at)
a. Pada Shell (Cooling Water)
Diketahui :
ID = 736 mm .................................................(Tabel Spesifikasi HE 116-C)
= 73,6 cm x 0,3937 in/cm = 28,9763 in
OD = 19 mm .................................................(Tabel Spesifikasi HE 116-C)
= 1,9 cm x 0,3937 in/cm = 0,74803 in
Tube pitch (PT) = 25mm ...............................(Tabel Spesifikasi HE 116-C)
= 2,5 cm x 0,3937in/cm = 0,9842 in
Jumlah baffles = 4 ...(Fig. Kellog Syn Gas Compressor Interstage Cooler)
Jarak baffles (B) = 3810 mm ........(Fig. Kellog Syn Gas Compressor
Interstage Cooler)
= 3810 mm/4
= 952,5 mm
= 95,25 cm x 0,3937in/cm = 37,4999 in
Tube clearance (C”) = PT –OD ................................................(Kern, 1950)
= 0,9842in – 0,74803 in
= 0,2362 in
Maka,
103
as = ID xC x B} over {144 x PT ¿ ...............................................
(Persamaan 7.1 Kern, Hal.138)
= 28,9763∈x0,2362∈x 37,4999∈ ¿144 x 0,9842∈¿¿
¿
= 1,8109 ft2
b. Pada Tube
Diketahui :
Jumlah Tube (Nt) = 254/shell.........................(Tabel Spesifikasi HE 116-C)
Jumlah Pass (n) = 2 .......................................(Tabel Spesifikasi HE 116-C)
Diameter Luar (OD) =19 mm .......................(Tabel Spesifikasi HE 116-C)
=1,9 cm x 0,3937 in/cm = 0,74803 in
BWG = 14 .....................................................(Tabel Spesifikasi HE 116-C)
Maka,
a’t= 0,268 in2........................................................(Tabel 10 Kern, Hal.843)
at = Nt x a ' t144 xn
..................................................(Persamaan 7.48 Kern,
Hal.150)
= 254/ shell x 0,268∈2
144 x 2
= 0,2363 ft3
5. KECEPATAN MASSA (Gs dan Gt)
a. Pada Shell
Diketahui : ws = 392418,8 Ib/hr
as = 1,8109 ft2
maka, Gs = wsas
.............................................(Persamaan 7.2 Kern, Hal
138)
104
= 392418,8lb /hr
1,8109 ft 2
= 216698,2164 Ib/hr ft2
b. Pada Tube
Diketahui : wt = 35525,65 Ib/hr
at = 0,2363 ft2
maka, Gt = w tat
..............................................(Persamaan 7.2 Kern, Hal
138)
¿ 35525,65 Ib /hr
0,2363 ft ²
= 150341,3034 Ib/hr ft2
6. BILANGAN REYNOLD (Re)
a. Pada Shell
Dik : tavg = 72oF
μ = 0,95 x 2,42 = 2,299 Ib/ft hr ...............(Fig.14 Kern, Hal. 823)
Ds = 0,95 in ft / 12 in = 0,0791 ft ...............(Fig.28 Kern, Hal. 845)
Res= Ds x Gs / μ ...............................(Persamaan 7.3 Kern, Hal 152)
= 0,0791 ft x 216698,2164 Ib/hr ft2 / 2,299 Ib/ft hr
= 7455,7759
b. Pada Tube
Dik : Tavg = 205,38oF
μ = 1,176 x 10-2 = 0,01176 lb/fthr ............(Fig. 15 Kern, Hal. 825)
= 0,01176 x 2,42 = 0,0284 lb/fthr
Dt = 0,584 in ............................................(Tabel.10 Kern, Hal. 843)
= 0,584 in x 1 ft/12in = 0,0486 ft
105
Ret = Dt x Gt / μ .................................(Persamaan 7.3 Kern, Hal 152)
= 0,0486 ft x 150341,3034 Ib/hr ft2 / 0,0284 Ib/ft hr
= 257274,2023
7. FAKTOR PERPINDAHAN PANAS
a. Pada Shell
Res = 7455,7759
JH = 50 ......................................................................(Fig.28 Kern, hal.838)
b. Pada Tube
Ret = 257274,2023
L = 4264mm ...............................................(Tabel Spesifikasi HE 116-C)
= 4,264 m / 0,0254 m/in = 167,8740 in x 0,0833 ft/in = 13,98 ft
D = 0,584 ft/12 = 0,0486 ft ...............................(Tabel.10 Kern, Hal.843)
L/D = 13,98 ft/0,0486 ft = 287,2602
jH = 320 ...............................................................(Fig.24 Kern, Hal.834)
8. KOEFISIEN PERPINDAHAN PANAS
a. Pada Shell
tavg = 72 oF
c = 1 BTU/lb oF ...................................................(Fig.4 Kern, Hal. 806)
k = 0,3491 BTU/hrft oF ....................................(Table.4 Kern, Hal. 800)
Maka :
(c x μ
k)1/3 ....................................................(Persamaan 6.15b Kern,
Hal.150)
= ( 1 BTU
lbFx 2,299 lb / fthr
0,3491 BTU / fthrF )1/3 = 1,8744
106
b. Pada Tube
Tavg = 205,38 oF
c = 1,3077 BTU/lb oF
k = 9,479 x 10-2 = 0,09479 BTU/hrft oF....(Tabel Spesifikasi HE 116-C)
Maka :
(c x μ
k)1/3 ....................................................(Persamaan 6.15b Kern,
Hal.150)
= ( 1,3077 BTU
lbFx0,0284 lb / fthr
0,09479 BTU / fthrF )1/3 = 0,7317
9. ho dan hio
a. Pada Shell
jH = 50 ......................................................................(Fig.28 Kern, hal.838)
k/Ds .........................................................(Persamaan 6.15b Kern, Hal.150)
= 0,3491 BTU/hrft oF/0,0791 ft
= 4,4134 BTU/hr oF
Maka :
ho = jH x kD
x ( c x μk )
1 /3
ɸs .........................(Persamaan 6.15 Kern,
Hal.122)
hoɸs
= jH x kD
x ( c x μk )
1 /3
hoɸs
= 50 x 4,4134 BTU/hr oF x 1,8744 = 413,6238 BTU/hr oF
b. Pada Tube
jH = 320 ...................................................................(Fig.24 Kern, Hal.834)
k/Dt .........................................................(Persamaan 6.15b Kern, Hal.150)
107
= 0,09479 BTU/hrft oF/0,0486 ft
=1,9504 BTU/hr oF
Maka :
hi = jH x kD
x ( c x μk )
1 /3
ɸt ..........................(Persamaan 6.15 Kern,
Hal.122)
hiɸt
= jH x kD
x ( c x μk )
1 /3
hiɸt
= 320 x 1,9504 BTU/hr oF x 0,7317
hi= 456,6744 BTU/hr oF
hio = hi x IDOD
.............................................(Persamaan 6.5 Kern, Hal.
105)
= 456,6744 BTU/hr oF x 28 , 9763∈ ¿0,74803∈¿¿
¿
= 17690,11415 BTU/hr oF
10. CLEAN OVERALL COEFICIENT, Uc
Uc = hio x hohio+ho
= 17690,11415
BTUhrF
x413,6238BTUhrF
17690,11415BTUhrF
+413,6238B TUhrF
= 404,1735 ....
(Persamaan 6.38
Kern, Hal. 121)
11. DESIGN OVERALL COEFFICIENT, UD
Diketahui: OD = ¾ in ..........................................(Tabel Spesifikasi HE 116-C)
BWG = 14 .........................................(Tabel Spesifikasi HE 116-C)
a” = 0,1963 ft2 / in ft ................................(Tabel.10 Kern, Hal.843)
L = 14 ft .............................................(Tabel Spesifikasi HE 116-C)
108
Nt = 254/shell.....................................(Tabel Spesifikasi HE 116-C)
Maka:
A = a” x L x Nt ..................................................................(Appendix Tabel.10)
= 0,1963 ft2/in ft x 14 ft x 254/shell
= 698,0428 ft2
Sehingga,
UD = Q
A x ∆ t ......................................................(Persamaan 6.11 Kern, Hal.
107)
= 10810262,08 BTU /hr
698,0428 ft ² x 96,8783 F
= 159,8555 BTU/hrft2 oF
12. FAKTOR PENGOTOR, Rd
Rd = Uc−UDUc x UD
.....................................................(Persamaan 6.13 Kern, Hal.
108)
= 404,1735 – 159,8555404,1735 x 159,8555
= 0,0037 BTU/hrft2 oF
13. PRESSURE DROP
a. Pada shell
Res = 7455,7759
f = 0,0012 ft2/in2 .................................................(Fig.29 Kern, Hal. 839)
s = 1,0 …...........................................................(Tabel.6 Kern, Hal. 808)
∆ Pt = f x Gs² x L x n
5,22 x 1010 x Ds x S x ɸs .......................(Persamaan 7.45 Kern, Hal.
148)
109
= 0,0012 ft ²/¿ ² x
(216698,2164 )2 Ibhr
f t 2 x 13,98 ft x2
5,22 x1010
x0,0791 ft x 1 x 1
= 0,3815 psi/14,7 = 0,0259 kg/cm2
b. Pada tube
Ret = 257274,2023
f = 0,0013 ft2/in2 ...................................................(Fig.29 Kern, Hal.839)
Dt = ID/12 ...............................................................................(Kern, 1950)
= 28,9763/12
= 2,4146 ft
No of crosses
N + 1 = 12L/B .....................................(Persamaan 7.43 Kern, Hal 147)
= 12 x 13,98 ft/ 37,4999 in
= 4,4736
s = ρgas
ρwater ............................................................................(Kern,
1950)
= 15,48 kg/mᶾ
1 kg/mᶾ
= 15,48 kg /mᶾ
s =15,48 kg/mᶾ62,5 kg/mᶾ
= 0,2476
∆PT = f x>² x Dt x (N+1)
5,22 x 1010 x Dt x S x ɸs ..............................(Persamaan 7.44 Kern,
Hal.147)
= 0,0013 ft ² /¿ ² x
(150341,3034 )2 Ibhr
f t 2 x 2,4146 ft x 4,4736
5,22 x1010
x0,0486 ft x0,2476 x 1
= 0,5052 psi
110
= 0,0343 kg/cm2
14. EFISIENSI KERJA HE
η = Panas yangdiserapPanas yang dilepas
x 100%
= 9888933,6
10810262,08 x 100%
= 91,47%
111