TITIS SAMPURNA Moree Per ect With Us Mor
Job No 9801
Doc No 9801-PRO-DBM-001
PROYEK PEMANFAATAN PEMANFAAT AN GAS SERDANG - BERINGIN
Page 1 of 7
AIR
PROCESS DESIGN BASIS
0
06-06-2001
Issued for Design
ABI
JHN
DAG
B
08-05-2001
Issued for Approval
ABI
JHN
DAG
A
06-04-2001
Issued for Review
ABI
JHN
DAG
Rev
Date
Description
Prep¶d
Chk¶d
App¶d
Total or partial reproduction and/or utilization of this document areforbidden areforbidden Without prior written authorization of the owner
P
YE
.
LP
3..
3..3
P
3..
P
IV.
P
l
.
k
V.
l
. .
k
m
ii
L
Pl
i
o
i
n
}
m
I
................................ ................................ ................................ .........
m
k
................................ ................................ ................................ .................
z
k
................................ ................................ ................................ .............
j
k
S
}
Lim
i
o
im
m
k
ESI
|
E I
................................ ................................ ................................ .................
n
z
o
o
l
l
k
k
SE
................................ ................................ ................................ ..............
j
ii
I
................................ ................................ ................................ ....................
m
n
S
m
}
ESS
LP
o
S
o
................................ ................................ ................................ ....
m
k
................................ ................................ ................................ ...... k
{
{
{
{
ILI Y ................................ ................................ ................................ ............................... 7
~
k
ELE P
o
I
o
S
o
k
o
EX
m
P
.
I l
3..
n
k
l
PE
I I Y................................ ................................ ................................ ...................... 7
k
Document No Revision
|
~
1
S
E
P RO-DB
j
|
-001
|
ELIVE Y ................................ ................................ ................... 7
k
Date Page
06/06/01
Sheet 3
P
I.
YE
I
PE
I
S
I
SE
E I
I
This process design basis def ines the general minimum technical requirements of the process detail engineering applicable f or the Air Ser dang ± Beringin Gas Project. This project consist of two sub-system : 1.
Sub-system I : -
Gas Compressor Station Air Ser dang (SKG ASD) 20
-
Gas Compressor Station Beringin (SKG BRG) 10
-
Gas Dehydration Unit Air Ser dang (DHP ASD) 20
-
Gas Dehydration Unit Beringin (DHP Beringin )
-
Gas Pipeline Transmission ´ 32.4 km f rom SKG ASD to SKG BRG
-
Gas Pipeline Transmission 10´ 2 .5 km f rom SKG BRG to LPG Plant Limau Timur
-
CO2 Removal Plant Limau Timur (CO2 L T) 30
2.
SCFD capacity
SCFD capacity
SCFD capacity
SCFD capacity
Sub-system II : -
LPG Extraction Plant Limau Timur (LPG L T) 30 storage 600 Ton Capacity.
-
LPG Storage Tank and Loading System Pulau Layang Plaju 1000 Ton capacity
OVER ALL
Document No Revision
1
01-P RO-DB
-001
SCFD Feeding capacity with
PROCESS SCHE E
Date Page
06/06/01
Sheet 4
P
II.
YE
PE
E E
S
I
SE
E I
I
L
ª
¬
«
«
«
«
®
°
¯
As minimum, the most recent edition or revision of the f ollowing industry standar ds and codes shall be use d or ref e rred to in the design, material selection, f abrication, installation, inspection, testing, mar king and shipment of the mechanical equipment. API RP 14C
Analysis, Design, Installation and Testing of Basic Sur f ace Saf ety System f or Off shore Production Platf orms
API RP 14E
Design and Installation of Off shore Production Platf orm Piping System (particularly f or line -sizing criteria)
API RP 2000
Venting
API RP 520
Sizing, Selection, and Installation of Pressure Relieving Devices in Ref ineries
API RP 521
Pressure Relief and Depressurizing System
API RP 50 ±
anagement of Process Hazar ds
²
API Spec 12J
Atmospheric and Low Pressure Tanks
Oil
and Gas Separators
GPA 2172
Publication f or calculation of gross heating value, relative density and compressibility f actor f or natural gas mixtures f rom compositional analysis
API RP 551
Process
API RP 554
Process Instrumentation and Control
²
easurement Instrumentation
-
Indonesia Government Regulation No. 11/1979
-
Engineering Data Book Gas Processors Suppliers Association (GPSA).
Document No Revision
1
01-P RO-DB
-001
Date Page
06/06/01
Sheet 5
P
´
³
III.
Ç
.
È
3..1
YE
À
Ä
µ
PE
ESI VE
·
¹
¶
Á
·
º
·
Å
É
»
·
¸
S
·
I
³
SE
P IL S P Y & Ã
Â
Ä
LL S
Ä
Ã
Ë
SYS E
Ì
¾
·
¸
Å
Æ
½
E I ³
I
»
¸
¸
Å
À
Æ
Ê
» ¼
³
Á
E E Â
Å
É
L
Å
Æ
Å
À
Design Lif e and Conditions Overall
3..2
·
¸
equipment both in Sub-System I and Sub-System II shall be designed f or 20 Years.
Site Environmental Data -
Site Elevation SKG ASD SKG BRG LPG L T
: : +/ - 150 f t above : +/- 150 f t above : +/ - 150 f t above
y y
Í
y
-
Ambient Temperature Plant Saf ety
o
o
Í
Í
Í
SL SL SL o
: 80 F to 100 F (90 F Normal) :
Process Plant has many hazar d s that need to be considered in the design of the f acilities. Process design shall consider various hazar d s including but not limited to: Handling and disposal of process f luids and chemicals
y
Noise levels in excess of 85dB (A) Hot sur f aces in excess of 6 0°C (140°F)
y y
3..3
Climatology -
Wind Condition Wind Direction Wind Velocity Rain f all Average Rainf all per years Average Number of rainy days Average Number raining in hours aximum rainf all daily Humidity Relative Humidity y y
-
y
: 1640 mm : 109 days : 2 hours : 2 inch/hr
y
: min 60 % - maximum 95 %
y y y
Í
-
-
: : NE (North-East) : 19.2 f t/s
Air Pressure Average Air pressure yearly y
3..4
Earthquake Consideration
3..5
Environmental Requirement
: 1009.2 mbar
: Yes, apply zone 1 (0.100)
CONTR ACTOR shall comply with all Indonesian laws, rules and regulations.
Document No Revision
9801- P RO-DB 1
¿
-001
Date Page
06/06/01
Sheet 6
P
Ï
Î
YE
PE
Ð
Ò
Ô
Ñ
Ò
Ò
Õ
Ò
Ó
Ö
S
Ò
Ó
Ò
I
SE
Î
Ö ×
Î
E I
Ù
Ò
Ó
Ø
Î
Ö
Ó
I
Ó
As a minimum CONTR ACTOR shall meet the f ollowing pollution limits or the Indonesian Law values if more stringent: AIR E ISSION LI ITS (Continuous 24 Hour Average Emission Limits) Û
Û
Ref erence
f or Indonesian Emission Standar ds shall be the latest version. Peraturan enteri Negara Lingkungan Hidup Nomor 4 tahun 2000 (Water pollution: Indonesia Government Regulation (permen Negara Lingkungan Hidup No. 4 tahun 2007)) Air Polution: Keputusan enteri Negara Lingkungan Hidup No. 129, Tahun 2000 tentang baku mutu Emisi Sumber Tidak Bergerak
y
Ü
y
Ü
Ref erence
f or Indonesian Saf ety Standar ds shall be the last version Saf ety: Indonesia Government regulation No. 11/1979 & Pertamina saf ety Regulation Noise: Indonesia Government Code No. SE-01/ EN 1978 Storage Tank: Indonesia Government Regulation No. 11/1979
y y
Ü
y
Ketentuan umum Pemadam Kebakaran Api dan Keselamatan (KUPAK) Peraturan Khusus Depnaker
5.
Ý
3..1
S
I
à
Þ
ß
SE
á
à
á
â
ã
ß
Feed Gas Flow rate Prof ile
YE
LP
à
á
ä
å
æ
ä
å
ß
2002
5
5
2003
5
5
2004
5
5
2005
5
5
2006
5
5
2007
5
5
2008
5
5
2009
5
5
2010
5
5
2011
5
5
Total
3..2
P
ß
10
Gas Composition
ç
è
é
P
è
ã
E
ê
ã
æ
Car bon Dioxide
Document No Revision
9801- P RO-DB 1
P
ä
ß
å
(% m l ) ì
ë
N/A
Ú
-001
LP
ä
ß
å
(%m l ) ì
ë
N/A
Date Page
06/06/01
Sheet 7
P
î
í
YE
ï
PE
ñ
ð
ó
ñ
ñ
ô
ñ
ò
õ
ñ
ò
S
ñ
I
í
SE
õ ö
ø
ñ
í
ò
÷
E I í
õ
ò
I
ò
Nitrogen
N/A
N/A
ethane
N/A
N/A
Ethane
N/A
N/A
Propane
N/A
N/A
i -Butane
N/A
N/A
n-Butane
N/A
N/A
i -Pentane
N/A
N/A
n-Pentane
N/A
N/A
n-Hexane (+)
N/A
N/A
Total
N/A
N/A
Water Content Inlet (lb/mmscf )
N/A
N/A
ú
Water Content Inlet (mix) lb/mmscf
100
Water Content Outlet (lb/mmscf )
3..3
7
Pressure
¡
V i û
û
ü
l
LP
þ
ý
Inlet Pressure (psig) Outlet
3..4
Pressure (psig)
û
30
850
800
800
¡
û
û
ü
l
LP
þ
ý
o
Inlet Temperature ( F) Outlet
o
Temperature ( F)
£
3..1
3..3
û
P
û
ÿ
ÿ
130
130
120
120
PIPELI E ´
¢
3..2
û
ÿ
Temperature
V i
5.
P
ÿ
¤
Gas Flow Rate ú
ú
: 20
aximum Operating Pressure
ú
ú
SCFD
: 800 psig
inimum Receiving Pressure (ASD BRG) : 700 psig
Document No Revision
9801- P RO-DB 1
ù
-001
Date Page
06/06/01
Sheet 8
P
¦
¥
3..4 3..5
YE
PE
§
©
¨
©
©
©
S
©
©
I
¥
SE
¥
E I
©
¥
: 120 F
P
!
"
E
P
#
"
$
&
%
S
1
'
(% m l ) )
(
Car bon Dioxide
N/A
Nitrogen
N/A
ethane
N/A
Ethane
N/A
Propane
N/A
i -Butane
N/A
n-Butane
N/A
i -Pentane
N/A
n-Pentane
N/A
n-Hexane (+)
N/A
Water Content Inlet (lb/mmscf )
N/A
Water Content Inlet (mix) lb/mmscf
100
Water Content Outlet (lb/mmscf )
3..1
Gas Composition
0
I
o
aximum Operating Temperature
5.
%
2
E I 3
"
%
I
7
"
Feed Gas Flow rate Prof ile
YE
LP
4
Document No Revision
3
&
'
$
P
&
2002
10
10
2003
10
10
2004
10
10
2005
10
10
2006
10
10
2007
10
10
2008
10
10
2009
10
10
9801- P RO-DB 1
-001
'
%
%
Date Page
06/06/01
Sheet 9
P
6
5
YE
7
PE
9
A
8
9
9
B
9
@
C
S
9
@
YE
9
I
5
SE
C D
5
@
E
LP
H
I
E I
F
9
5
Q
C
@
I
@
R
S
10
10
2011
10
10
20
U
P
V
U
E
W
X
W
S
P
Q
(% m l )
LP
`
R
P
Y
Q
P
R
(%m l ) `
Y
Car bon Dioxide
N/A
N/A
Nitrogen
N/A
N/A
ethane
N/A
N/A
Ethane
N/A
N/A
Propane
N/A
N/A
i -Butane
N/A
N/A
n-Butane
N/A
N/A
i -Pentane
N/A
N/A
n-Pentane
N/A
N/A
n-Hexane (+)
N/A
N/A
Total
N/A
N/A
Water Content Inlet (lb/mmscf )
N/A
N/A
a
Water Content Inlet (mix) lb/mmscf
100
Water Content Outlet (lb/mmscf )
7
Pressure
V i Q
Q
b
l
LP
`
c
Inlet Pressure (psig) Outlet
3..4
R
Gas Composition
T
3..3
Q
P
2010
Total
3..2
P
P
Pressure (psig)
Q
R
S
P
Q
R
P
P
30
70
700
700
Temperature
Document No Revision
9801- P RO-DB 1
G
-001
Date Page
06/06/01 Sheet 10
P
e
d
YE
f
PE
h
g
p
h
h
q
h
i
r
S
h
i
V i w
I
d
SE
r s
i
t
o
Inlet Temperature ( F) Outlet
5.
3..1 3..2 3..3 3..4 3..5
o
Temperature ( F)
PIPELI E
d
LP
y
E I
u
h
d
l
w
x
h
r
i
w
i
P
w
130
130
120
120
³
Gas Flow Rate
I
: 30
aximum Operating Pressure
SCFD
: 800 psig
inimum Receiving Pressure (ASD BRG) : 65 0 psig o
aximum Operating Temperature
: 120 F
Gas Composition
P
E
P
w
(% m l )
Car bon Dioxide
N/A
Nitrogen
N/A
ethane
N/A
Ethane
N/A
Propane
N/A
i -Butane
N/A
n-Butane
N/A
i -Pentane
N/A
n-Pentane
N/A
n-Hexane (+)
N/A
Water Content Inlet (lb/mmscf )
N/A
Water Content Inlet (mix) lb/mmscf
100
Water Content Outlet (lb/mmscf )
Document No Revision
9801- P RO-DB 1
v
7
-001
Date Page
06/06/01 Sheet 11
P
5.
j
YE
k
PE
n
l
m
3..1
E
S
V L
o
l
I
SE
E I
I
I
Gas Specif ication The design of Amine CO2 Removal capacity is 31.4 SCFD and f eed gas composition shown Table ± 1 is obtained f rom Titis Sampurna specif ication
LE ±
k
k
l
o
P
l
E
m
3..2
l
|
z
|
}
Car bon Dioxide
ii
j
{
~
|
P SI I
k
l
o
l
l
o
l
LE %)
13.46
H2S
0.00
N2
1.04
ethane
(
63.82
Ethane
8.20
Propane
9.36
i-Butane
1.08
n-Butane
1.74
i-Pentane
0.42
n-Pentane
0.36
n-Hexane +
0.38
H2O
0.14
Total
100
Design Basis ITE
:
Amine CO2 Gas Removal Package
LOCATION :
Limau Timur, South Sumatera
AREA CLASSIFICATION :
CL. 1. Div.2. Group C/D area in accor dance to API-RP 500
DESIGN AX. WIND PRESSURE :
300 kgf/sqm (please consider the shape f actor (k) of the equipment)
EARTHQUAKE CONSIDER ATION :
Yes. Apply zone 1 (0.100)
SKID FOUND ATION :
Concrete Slab
Document No Revision
9801- P RO-DB 1
-001
Date Page
06/06/01 Sheet 12
P
YE
PE
S
I
SE
E I
I
TREATING FLUID :
Ucarsol AP 810, concentration 45% wt. in water
AX. ACID GAS LO ADING :
0.498
mole CO2/mole Amine
380 V AC, 3-phase, 50 Hz, u/t max. 200 kW drivers above 200 kW gas-engine to be applied.
ELECTRICAL SUPPLY :
220 V AC, 1-phase, 50 Hz INSTRU ENT POWE R :
Air supply 80-100 psig
FUEL GAS :
Natural gas (water saturated) @ plant inlet conditions approximate 1050 btu/scf
UNIT PROCESS GUAR ANTEE BY VENDOR:
CO2 content < 5.4 %mole, under all inlet conditions (3-cases)
INLET GAS PROPERTIES Case 1
Case 2
Case 3
29.75
30.93
31.4
Specif ic Gravity
0.88
0.87
0.86
Operating
Pressure, psia
665
665
665
Operating
Temperature, F
90
90
90
CO2 & H2S
CO2 & H2S
CO2 & H2S
Total Flow Rate,
SCFD
Contaminants:
Design Case, %mole 13.46
CO2 H2S N2 C1 C2 C3 iC4 nC4 iC5 nC5 C6+ H2O
OUTLET
0 1.04 63.82 8.2 9.36 1.08 1.74 0.42 0.36 0.38 0.14 100
GAS PROPERTIES
Delivery Pressure
Document No Revision
665 psia
aximum CO2 content
<5.4 %mole max
aximum Liquid Carryover in Gas Stream
0.1
9801- P RO-DB 1
-001
(assuming no f oaming)
Date Page
06/06/01 Sheet 13
P
5.
YE
PE
LP
S
EX
I
I
SE
E I
I
The Hydrocar bon Liquids Recovery Unit (HRU) will be manuf actured to f orm part of the Limau Timur Gas Plant f or the South Sumatera Gas Utilization Project. The HRU will be designed to extract the optimum amount of natural gas liquids by separation and ref rigeration system to produce 192 TPD of commercial grade LPG, 27 SCFD of pipeline quality natural gas, and 1316 bbls/day of hydrocar bon condensate.
3..1
Inlet Condition Gas Phase
-
Total Flow Rate,
SCFD
Case 1
Case 2
Case 3
27.22
28.26
28.66
Operating
Pressure, psia
665
665
665
Operating
Temperature, F
120
120
120
Composition, %mole
CO2
5.45
5.22
5.15
H2S
0.00
0.00
0.00
N2
1.15
1.31
1.40
C1
69.84
71.79
72.92
C2
8.98
8.22
7.79
C3
10.24
9.23
8.60
iC4
1.18
1.10
1.05
nC4
1.90
1.84
1.79
iC5
0.46
0.45
0.45
nC5
0.39
0.39
0.40
C6+
0.41
0.45
0.45
H2O
saturated
saturated
Saturated
91.02
58.86
51.44
25,899
16,890
14,728
665
665
665
90
90
90
Tabl
3.7.
as
ii
ª
«
¬
«
¬
Condensate Phase
-
Condensate Flow, USGP ®
®
@ 60 F
ass f low, lb/hr
Pressure, psia Temperature, F
Composition, %mole
CO2
6.56
7.10
6.45
H2S
0.00
0.00
0.00
N2
0.10
0.13
0.12
C1
16.10
17.75
16.26
C2
7.6
6.57
6.52
C3
22.57
12.82
19.12
iC4
5.14
5.33
4.67
Document No Revision
9801- P RO-DB 1
-001
Date Page
06/06/01 Sheet 14
P
°
¯
YE
±
PE
³
µ
²
TAN
³
AS AI
¶
SE
¯
ANG
·
¯
E INGIN
¹
¸
¯
nC4
10.86
11.65
10.43
iC5
5.15
5.72
5.21
nC5
5.39
6.19
5.77
C6+
20.44
25.62
25.35
H2O
0.10
0.10
0.10
Case 1
Case 2
Case 3
26.02
27.29
27.50
600
600
600
Tabl »
3..2
³
´
3.7. ¼
»
»
»
½
¾
¿
À
Á
¾
Á
sate
¿
À
Á
¾
iti
À
Á
Product Specif ication
Gas Flow Rate,
Â
Â
SCFD
Pressure, psig Temperature, F
120
max
120
max
120
max
Btu/scf
950
min
950
min
950
min
LPG Flow,
TPD
191
143
137
120
max
120
max
120
max
Ethane content, %volume
0.2
min
0.2
min
0.2
min
C3/C4 Content, % volume
97.5
Pentane plus, % volume
2.00 max
2.00 max
2.00 max
Flow, bbls/day
1.316
1.275
1.130
Vapor Pressure @100 F, psia
8
Vapor Pressure @100 F, psig
max
97.5
max
97.5
max
Stabilized Condensate
3..3
max
8
max
8
max
Product Storage -
-
Storage at Limau Timur LPG
:
Pressurized cylinder
Capacity
:
To cover 3 days on spec LPG Production
Volume
:
3x
Condensate
:
Atmospheric Tank ± 1 Nos
Capacity
:
Volume
:
Ã
Ä
Ä
metric tones LPG
days production
Ã
1
x 3000 std bbls
Storage at Pulau Layang LPG
Document No Revision
:
9801- P RO-DB 1
º
-001
Pressurized Sphere
Date Page
06/06/01 Sheet 15
P
Æ
Å
YE
3..4
PE
Ç
ANFAATAN GAS AI
È
SE
Å
ANG
É
Å
Ë
Ê
E INGIN Å
Capacity
:
To cover 5 days on spec LPG Production
Volume
:
1
x 1000 metric tones LPG
Product Loading At Lmau Timur LPG Plant
-
LPG Product Transportation
:
By Truck 8 & 15
Loading Time
:
0.5 - 1
Í
T
Hours
Condensate Product
P
:
By Truck, 15000 liter
Loading Time
:
0.5 - 1
hours
At Pulau Layang
-
IV.
Transportation
Î
Transportation
:
By LPG Tanker
Loading Time
:
Hold Hours
Ï
ESS
Ð
ESIGN
5.1
Gas
5.1
LPG Plant Limau Timur
Ð
Ò
m
Ñ
Ó
Ô
essor Station
The process design case is def ined based on the f eed gas throughput given in attached document based on the design case, process simulation has been per f ormed utilizing HYSYS sof tware. All product streams quantities are based on an Inlet gas volume of maximum 28.66 with a gas composition as shown in Table 3.7.1 (excluding water).
Í
Í
SCFD
The resulting specif ication products f rom these quantities at the Fractionation Plant are as f ollows: LPG
:
190
Condensate
:
1500
Í
etric tonnes/day
Barrel/day
LPG extraction plant consist of : -
Liquef action with propane ref rigerant chiller
Document No Revision
9801- P RO-DB 1
Ì
-001
Date Page
06/06/01 Sheet 16
P
Ö
Õ
YE
×
PE
ANFAATAN GAS AI
Ø
Õ
SE
Ù
Õ
ANG
Û
Ú
E INGIN Õ
Fractionation with Low Temperature Separator (Demetanizer), Deetanizer Column, and Debutanizer Column.
-
To ensure that no hydrate f ormed during the process of liquef action then used Ethylene Glycol ( EG) as a hydrate inhibitor
Ý
ono
Ý
V.
Þ
TILIT Y
This section describes the utility needs and availability at Pemanf aatan Gas Air Ser dang Beringin Project f or both sub-system. All required utilities must be self provided and this also includes f or disposal of waste products. Utilities f or this plant will be self provided by the utility in both Sub -system.
ß
.1
ELE TRI IT Y à
à
Electric power f or all users at the both sub-system will be provided by gas engine driven generators. The engines will be reciprocating type with minimum 10 % operating horse power margin over the generator maximum demand case. The f eed to the engines will be f uel gas. At start-up plant f uel gas will be provided f rom a upstream of plant af ter inlet separator at each sub-system The power generation system comprises of: Normal Condition: 2 Nos (2 x 100%) gas engines of rating (ref er to load list) kW / 400 V, 50 Hz
á
. â
PRODUCT STORE LPG Production will be stored in LPG Storage vessel. LPG storage should be able to store the on-spec LPG product f or three (3) days, whereas the off -spec product will be stored in others storage ( off -spec LPG storage). Condesate production will be stored in Condensate Storage Tank. condensate storage should be able to store the on-spec condensate product f or seven (7) days. LPG product will be transf er by LPG truck line to Pulau Layang LPG Storage in Palembang. LPG Storage in Pulau Layang should be able to store the LPG product f or seven (7) days. From Pulau Layang, LPG product will be delivered by LPG Tanker. Condensate product will be transf er to Pertamina by truck line or by Pipeline. The specif ication of Loading of LPG and condensate be described below : -
LI AU TI UR ã
y
y
Document No Revision
ã
LPG Transportation : By LPG Truck 8 Loading Time : 0.5 ± 1 hours
ä
T & 15
ä
T
Condensate Transportation : by Truck 15000 liters or by pipeline
9801- P RO-DB 1
Ü
-001
Date Page
06/06/01 Sheet 17
PRO YE
å
-
PE
æ
ANFAATAN GAS AIR
SE RDANG
è
ç
ERINGIN
PULAU LA YANG Transportation : By LPG Tanker Loading Time : 4 hours
Document No Revision
9801- P RO-DB 1
é
-001
Date Page
06/06/01 Sheet 18
