bcd5-190-42-rpt-4-101-00-rev. d
TRANSCRIPT
PetroChina International Jabung Ltd.
Betara Complex Development Job No. : BCD – 471 – CA
PROCESS
HYSYS SIMULATION REPORT
FEED for WB-SB Non Associated Gas Early Facilities WB-GRF
DocumentBCD5-190-42-RPT-4-101-00
Revision DCONTRACTOR DOCUMENT REVIEW
FOR CONFORMANCE WITH SPECIFICATIONS AND DESIGN DRAWINGS Review Code
A Accepted as it is or with minor comments
B Accepted as noted - Resubmittal required
C Not Accepted
D Information Only
THIS REVIEW DOES NOT RELIEVE THE CONTRACTOR/VENDOR
OF ANY CONTRACTUAL OBLIGATION, INCLUDING THE
RESPONSIBILITY FOR ENGINEERING AND DETAIL DESIGN.
PetroChina International Jabung Ltd.Date By
D Re-Issued For Approval 15-Aug-13 AEN DJ JH -
C Issued For Approval 4-June-13 AEN DJ JH -
B Issued For Review 7-May-13 AEN DJ JH -
A For Discipline Coordination 2-May-13 AEN DJ JH -
Rev. Description Date PreparedBy
Checked By
ReviewedBy
Approved By
TABULATION OF REVISED PAGES
PAGE REVISIONS PAGE REVISIONS
A B C D 0 1 2 3 A B C D 0 1 2 31 522 533 544 555 X X 566 577 X 588 X 599 X 6010 6111 6212 6313 6414 6515 6616 6717 6818 6919 7020 7121 7222 7323 7424 7525 7626 7727 7828 7929 8030 8131 8232 8333 8434 8535 8636 8737 8838 8939 9040 9141 ATTACHMENT APPENDIX42 1 X X43 244 345 446 547 648 749 850 9
51 10
Sign Date
Prepared by AENChecked by DJApproval by JH
Doc/DWG No.: document.docx Rev. No: D
No. Para./Section Items Explanation/Reason
1 Sec 1 Update Introduction Implemented
2 Sec 4Process Description & Fig. 4.1
Implemented
3 Sec 5Pressure drop control valve and metering
Implemented :Attachment -2 : Hydraulic calculation
3Procedure Project Progress Reporting
Table of ContentsSection Title Page
1.0 INTRODUCTION..............................................................................................52.0 OBJECTIVE......................................................................................................53.0 REFERENCE DOCUMENT..............................................................................54.0 PROCESS DESCRIPTION...............................................................................55.0 SIMULATION BASIS AND ASSUMPTION......................................................8
5.1 Operating Pressure.........................................................................................85.2 Production Rates............................................................................................95.3 Simulation Cases............................................................................................95.4 Feed Stream Composition.............................................................................95.5 Simulation Assumption................................................................................10
6.0 RESULTS.......................................................................................................116.1 Product Composition...................................................................................116.2 Equipment Design Data................................................................................136.3 Hydrate Formation Prediction.....................................................................14
7.0 ATTACHMENT...............................................................................................14
4Procedure Project Progress Reporting
1.0 INTRODUCTION
The existing WB GRF Facility is designed for handling and processing the wellfluids
from oil wells. The incoming wellfluids is separated into a single phase where the
separated gas, called as associated gas, is delivered directly to BGP/CPS via 12”/10”
trunk-lines.
PetroChina International Jabung Ltd, called as PCI, now intends to upgrade the
existing WB Facility to handle wellfluids from non associated gas wells. The gas and
liquid from non associated gas wells will be separated and measured before
combined and delivered to BGP/CPS through existing 12’’/10” trunk-line. It is
expected that trunk-line pressure of 850 psig will be at WB Facility.
Initially when the reservoir pressure is high, It is possible that the gas and liquid will
flow to BGP/CPS on its own pressure. In future, when the wells pressure declines,
gas compression and liquid pumps shall be installed to meet the pipeline back
pressure.
2.0 OBJECTIVE
This Process Simulation Report is intended to present the data sources, simulation
methodology & basis, and summary of the process simulation for the development of
WB Facility in regard additional equipment for gas well treatment.
3.0 REFERENCE DOCUMENT
Following documents were used as reference for this simulation:
1. Process Design Basis (BCD5-190-42-DBM-4-101-00).
2. Scope of Work for BCD4-471-WOR-017 ( BCD3-195-40-SOW-4-001-00)
4.0 PROCESS DESCRIPTION
By having new gas wells in the area of WB Facility, it is understood that the existing
facility should be modified in order to measure the volumetric rates of each fluid, and to
drive whenever the well pressure decline.
The wellfluids from gas wells are directed to (3-phase) Production Separator via
trunklines and manifold. The mixed gas, liquid and water are separated into a single
5Procedure Project Progress Reporting
D
WB- SB
195-V-200Production Separator
TurbineMeter
195-E-200A/B/C195-K-200A/B/C
195-V-201 A/B/C
195-V-202A/B/C
195-V-203A/B/C
195-K-200 A/B/C
195-E-201A/B/C
3 x 50%s
2 x 100%s
195-P-200 A/B
PCV
LCV
To Produced Water System
phase. During high pressure case, the outlet gas and liquid are measured
independently, then combined & routed to BGP/CPS via 12”/10” Trunk-lines, water
shall be routed to separate produced water handling system and connection for it shall
be kept. The Production Separator is operated higher than expected export pressure of
850 psig.
During low pressure case, it is scheduled to operate the Production Separator at 150
psig as the Lowest Pressure Operating could be implemented. Since the export
pressure of 850 is kept constant then additional equipment, such as compressor and
pump, are required to drive the separated gas and liquid respectively. Again, the
pressurized gas and liquid are combined and routed to BGP/CPS via 12”/10” trunk-
lines.
Systematically, a simple process schematic is provided below.
Notes :
6Procedure Project Progress Reporting
D
: Hig
h Presssur
e Operatin
g Cas
e
Figure 4.1 Process Schematic
7Procedure Project Progress Reporting
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
5.0 SIMULATION BASIS AND ASSUMPTION
5.1 Operating Pressure
Based on the given production profile of gas wells, it is intended to deliver naturally
the well fluids from WB Facility to BGP/CPS via 12”/10” trunk-lines by keeping the
export pressure of 850 psig. This could be implemented during initial operation where
the reservoir pressure is still high. This mode operation is called as “High Pressure
Operating” case. The operating pressure at Production Separator is set at 875 psig
with pressure drop of valves and metering as follow;
a. Pressure Control Valve
The pressure drop across PCV should be defined to keep the export pressure at
850 psig. From hydraulic calculation (see attachment 2) the pressure drop of
PCV is 18 psi
b. Liquid Control Valve
To keep the export pressure at 850 psig, the LCV pressure drop should also be
defined. From hydraulic calculation (see attachment 2) the pressure drop of LCV
is 14 psi
c. Gas Metering
From calculation (see attachment 2) pressure drop across gas metering package
during high pressure operating case is 1.93 psi
d. Liquid Metering
The pressure drop at Turbine Meter is 6 psi (taken from vendor data)
The decline reservoir pressure is called as “Low Pressure Operating” case, it is
intended to operate the Production Separator at 150 psig. Since the export pressure
is kept at 850 psig, additional compression and pumping systems are added where
gas and liquid phase are comingled and delivered to BGP/CPS via 12”/10” trunk-
lines. Due to higher gas flow rate during low pressure operating case, the pressure
drop across gas metering package is changed to 2.96 psi (see attachment 2). The
same pressure drop on control valves are implemented since control valve will do the
throttling fuction.
The simulation uses HYSYS V7.2 with Peng-Robinson Equation of State.
Doc: document.docx document.docxdocument.docx Page 8 27302601-JulNovMay-09 13
D
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
5.2 Production Rates
The estimated production rates for High and Low Pressure Operating Cases are
taken from Company’s process simulation results. The followings are feed rates to
Production Separator at “High and Low Operating Pressure” cases ;
Table 5-1 Feed Rates
Description Gas
(MMscfd)Condensate(Std BPD)
Water(Std BPD) (Note 1)
Remarks
High Pressure
Operating case10.80 635.6 3800
The total molar
flow is equal to
39.62 MMscfd
Low Pressure
Operating case31.35 1401.74 3800
The total molar
flow is equal to
61.33 MMscfd
Note 1. Maximum water flow rate is used (see attachment 3)
5.3 Simulation Cases
Simulation cases for “WB-SB Non Associated Gas Development Facilities Production
Separator and Gas Metering System” are as follows:
Case 1: “High Pressure Operating” case where the Production Separator is
operated at 875 psig.
Case 2: “Low Pressure Operating” case where the Production Separator is
operated at 150 psig.
5.4 Feed Stream Composition
The wellfluids compositions for “High and Low Pressure Operating” cases are taken
from Company’s process simulation results as the inlet of Production Separator.
Refer to Table 5-2 for details.
Doc: document.docx document.docxdocument.docx Page 9 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
Table 5-2 Feed Stream Composition
ComponentsHigh Pressure
Operating CaseLow Pressure
Operating Case(Mole Fraction) (Mole Fraction)
CO2 0.0017 0.0056
Nitrogen 0.0062 0.0084
Methane 0.1991 0.3598
Ethane 0.0305 0.0558
Propane 0.0305 0.0568
i-Butane 0.0057 0.0110
n-Butane 0.0078 0.0149
i-Pentane 0.0028 0.0051
n-Pentane 0.0024 0.0040
Hexane 0.0025 0.0035
Heptane 0.0024 0.0043
Octane 0.0020 0.0034
Nonane 0.0007 0.0012
Decane 0.0004 0.0006
n-C11 0.0001 0.0002
n-C12 0.0001 0.0001
n-C13 0.0001 0.0000
H2O 0.7052 0.4653
6.1 Simulation Assumption
Some assumption are taken to generate the simulation :
1. Pressure drop in Separator is assumed 5 psi
2. The future Compressor Package are assumed as follow;
a. The Air Cooler pressure drop is 10 psi
b. The temperature outlet of Air Cooler is 110 0F
c. The Compressor polytropic efficiency is 70%.
3. Ambient temperature is assumed 73 – 95 0F
Doc: document.docx document.docxdocument.docx Page 10 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
7.0 RESULTS
7.1 Product Composition
Based on the simulation results, the product compositions for export to BGP/CPS are
as follow ;
Table 6-3 Product Composition for High Pressure Operating Case
ComponentsGas Phase Liquid Phase Combined Gas +
Liquid Phase(Mole Fraction) (Mole Fraction) (Mole Fraction)
CO2 0.0056 0.0028 0.0054
Nitrogen 0.0221 0.0030 0.0208
Methane 0.7085 0.2029 0.6730
Ethane 0.1044 0.0874 0.1032
Propane 0.0974 0.1799 0.1032
i-Butane 0.0166 0.0541 0.0192
n-Butane 0.0219 0.0885 0.0265
i-Pentane 0.0067 0.0475 0.0095
n-Pentane 0.0053 0.0446 0.0080
Hexane 0.0040 0.0687 0.0085
Heptane 0.0024 0.0834 0.0081
Octane 0.0000 0.0000 0.0000
Nonane 0.0012 0.0799 0.0067
Decane 0.0003 0.0323 0.0025
n-C11 0.0001 0.0162 0.0012
n-C12 0.0000 0.0042 0.0003
n-C13 0.0000 0.0028 0.0002
H2O 0.0036 0.0020 0.0035
Doc: document.docx document.docxdocument.docx Page 11 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
Table 6-4 Product Composition for Low Pressure Operating Case
ComponentsGas Phase Liquid Phase Combined Gas
+ Liquid Phase(Mole Fraction) (Mole Fraction) (Mole Fraction)
CO2 0.0108 0.0017 0.0104
Nitrogen 0.0165 0.0003 0.0157
Methane 0.7014 0.0432 0.6718
Ethane 0.1074 0.0372 0.1042
Propane 0.1049 0.1311 0.1061
i-Butane 0.0186 0.0589 0.0205
n-Butane 0.0240 0.1074 0.0278
i-Pentane 0.0065 0.0732 0.0095
n-Pentane 0.0045 0.0684 0.0074
Hexane 0.0021 0.1006 0.0065
Heptane 0.0010 0.1559 0.0080
Octane 0.0003 0.1360 0.0064
Nonane 0.0000 0.0503 0.0023
Decane 0.0000 0.0243 0.0011
n-C11 0.0000 0.0067 0.0003
n-C12 0.0000 0.0044 0.0002
n-C13 0.0000 0.0000 0.0000
H2O 0.0018 0.0004 0.0018
Doc: document.docx document.docxdocument.docx Page 12 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
7.2 Equipment Design Data
Table 6-3 shows the summary of equipment data from HYSYS simulation.
Table 6-5 Equipment Design Data
EquipmentCase 1 Case 2
High Operating Pressure
Low Operating Pressure
Production Separator (195-V-200)- Liquid Flow Rate, Actual BPD
635.58 1381.85
- Gas Flow Rate, MMSCFD
10.77 31.38
- Water Flow Rate, BPD
3800 3800
- Operating Pressure, psig
870 150
- Operating Temperature,°F
145 66.02
Pump (195-P-200 A/B)- Flow Rate, Actual BPD
- 1381.85
- Suction Pressure, psig - 145- Discharge Pressure, psig
- 870
- Power, hp - 33.6
Compressor 195-K- 200 A/B/C (1st Stage)- Gas Flow Rate, MMSCFD
- 15.69
- Suction Pressure, psig - 126.9- Discharge Pressure, psig
- 340
- Pressure Ratio - 2. 60
- Power, hp - 1030
Compressor 195-K- 201 A/B/C (2nd Stage)- Gas Flow Rate, MMSCFD
- 15.69
- Suction Pressure, psig - 325- Discharge Pressure, psig
- 868
- Pressure Ratio 2. 60
- Power, hp - 1069
Doc: document.docx document.docxdocument.docx Page 13 27302601-JulNovMay-09 13
D
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
EquipmentCase 1 Case 2
High Operating Pressure
Low Operating Pressure
Air Cooler 195-E-200 A/B/C (1st Stage)- Duty, MMBTU/hr - -3.60
Air Cooler 195-E-201 A/B/C (2nd Stage)- Duty, MMBTU/hr - -3.45
8.1 Hydrate Formation Prediction
This HYSYS simulation is also used to determine the hydrate formation in gas lines.
Table 6-4 shows the summary of hydrate simulation results.
Table 6-6 Hydrate Formation
No. Line From To Remarks
1 195202 195-V-200 195-PV-200 Will Not Form
2 195203 195-PV-200 195-V-201 Will Not Form
3 195203A2/B2 195-V-201 195-K-200(1st
Stage) Will Not Form
4 195203A3/B3 195-K-200 (1st
Stage)195-E-200 (1st
Stage) Will Not Form
5 195203A4/B4 195-E-200 195-V-202 Will Not Form
6 195203A5/B5 195-V-202 195-K-200(2nd
Stage) Will Not Form
7 195203A6/B6 195-K-200(2nd
Stage)195-E-201 (2nd
Stage) Will Not Form
8 195203A7/B7 195-E-201 195-V-203 Will Not Form
9 195204 195-V-203 Gas Metering Will Not Form
10 195205 Gas Metering BGP/CPS Trunk-lines Will Not Form
Doc: document.docx document.docxdocument.docx Page 14 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
9.0 ATTACHMENT
Attachment – 1 : HYSYS Simulation
Attachment – 2 : Hydraulic Calculation
Attachment – 3 : WB-SB Water Production Forecast
Doc: document.docx document.docxdocument.docx Page 15 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
10.0 INTRODUCTION
Doc: document.docx document.docxdocument.docx Page 16 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
11.0 PROCESS SIMULATION HAS BEEN PERFORMED FOR THE WEST BETARA (WB) FLARE ASSOCIATED GAS RECOVERY FACILITIES USING HYSYS 200V7.06.5. THE WB FLARE ASSOCIATED GAS RECOVERY FACILITIES WILL CONTAIN PROCESS FACILITIES AND PIPELINES FOR USE ASTO PRODUCE AND TRANSPORT LIFT GAS TO WB WELLS AND ASSOCIATED GAS TO FOR TRANSMISSION THE EXISTING BGP/CPS VIA NEW GAS GATHERING FACILITIES.
12.0 THE ASSOCIATED GAS AT WB IS PRODUCED FROM THE PRODUCTION SEPARATOR, WHERE OIL AND GAS SEPARATION OCCURS. GAS FROM THE PRODUCTION SEPARATOR WILL BE ROUTED TO THE ASSOCIATED AND LIFT GAS COMPRESSORS AND CONDENSATE WILL BE SENT TO THE EXISTING GAS BOOT.
13.0 VAPOR FROM THE EXISTING GAS BOOT WILL BE RECOVERED AND INTRODUCED TO VAPOR RECOVERY UNIT (VRU) COMPRESSOR TO BOOST UP THE PRESSURE AND THEN SENT TO THE ASSOCIATED GAS AND LIFT GAS COMPRESSORS.
14.0 A PART OF ASSOCIATED GAS FROM WB PRODUCTION SEPARATOR WILL ALSO BE INTRODUCED TO WB LIFT GAS COMPRESSOR FOR REINJECTION TO THE WELLS AS LIFT GAS.
15.0 ASSOCIATED GAS COMPRESSOR COMPRESSES THE GAS FROM 100 PSIG UP TO THE REQUIRED PRESSURE FOR FINAL TERMINATION IN BGP/CPS.
16.0 OBJECTIVE
17.0 THE OBJECTIVES OF THIS SIMULATION OF THE FLARE GAS RECOVERY FACILITIES ARE ARE AS FOLLOWS:
18.0 TO IDENTIFY PRESSURE AND TEMPERATURE PROFILE ALONG THE FACILITIES.
19.0 TO DETERMINE MAXIMUM OPERATING PRESSURE AS INPUT TO DETERMINE PIPELINE DESIGN PRESSURE.
Doc: document.docx document.docxdocument.docx Page 17 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
20.0 TO ESTIMATE REQUIRED COMPRESSOR POWER.
21.0 TO GENERATE HEAT AND MATERIAL BALANCE FOR PROCESS DESIGN.
22.0 TO ESTABLISH GAS/LIQUID FLOW RATES FOR LINE SIZING CALCULATION.
23.0 TO GENERATE THERMODYNAMIC PROPERTIES FOR USE IN VARIOUS EQUIPMENT/INSTRUMENT SIZING.
24.0 TO PROVIDE BASE CASE FOR OTHER SIMULATIONS/STUDIES.
25.0 REFERENCE DOCUMENT
26.0 FOLLOWING DOCUMENTS ARE WERE USED AS REFERENCE FOR THIS SIMULATION:
27.0 PROJECT DESIGN CRITERIA (BCD4-000-42-CRT-4-012-00).
28.0 PROCESS DESIGN BASIS (BCD4-000-42-DBM-4-001-00).
29.0 DATA SHEET FOR SWB ASSOCIATED GAS COMPRESSOR PACKAGE (BCD4-185195-4243-DS-4-K-100-00).
30.0 DATA SHEET FOR SWB VRU COMPRESSOR PACKAGE (BCD4-185195-4243-DS-4-K-101-00).
31.0 DATA SHEET FOR SWB LIFT GAS COMPRESSOR PACKAGE (BCD4-185195-4243-DS-4-K-102-00).
32.0 SWB/WB PIPELINE HYDRAULIC SIMULATION REPORT (BCD4-190-42-REPT-4-004-00).
33.0 PFD OF WB GAS RECOVERY FACILITY.
34.0 P&ID OF WB GAS RECOVERY FACILITY.
35.0 PRELIMINARY DATA FROM EAST ASIA ENERGY (VENDOR OF AG AND LG COMPRESSORS).
Doc: document.docx document.docxdocument.docx Page 18 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
36.0 PRELIMINARY DATA FROM MEMBRANE TECHNOLOGY AND RESEARCH INC. (VENDOR OF FUEL GAS CONDITIONING PACKAGE).
37.0 BASIS AND ASSUMPTION
38.0 THE FOLLOWING BASIS AND ASSUMPTIONS HAVE BEEN MADE BY USING INFORMATION SUPPLIED BY COMPANYPCI.
39.0 BASIS
40.0 BASIS FOR THIS SIMULATION ARE AS FOLLOWDESCRIBED AS FOLLOWING:
41.0 FEED GAS COMPOSITION AND CONDITIONS BASED ON STREAM AT THE INLET PRODUCTION SEPARATOR.
42.0 COMPRESSOR SUCTION / DISCHARGE PRESSURE BASED ON SWB/WB PIPELINE HYDRAULIC SIMULATION REPORT [6]COMPRESSOR PACKAGE DATASHEET.
43.0 THE SIMULATION USES HYSYS 200V6.57.0 WITH PENG-ROBINSON EQUATION OF STATE.
44.0 SIMULATION CASES
45.0 TWO CASES ARE WERE CARRIED OUT IN THIS SIMULATION:
46.0 CASE 1: WITHOUT INJECTION OF 1,000 BBL/DAY FREE WATER AT THE INLET PRODUCTION SEPARATOR.
47.0 CASE 2: WITH INJECTION OF 1,000 BBL/DAY FREE WATER AT THE INLET PRODUCTION SEPARATOR.
48.0 PROCESS FLOW SCHEME
49.0 THE SIMULATION FLOW FOR THE FLARE GAS RECOVERY FACILITIES IS WAS BASED ON THE FLOW SCHEMATIC, WHICH HAS BEEN EXTRACTED FROM THE PFD AS THE FOLLOWING:
Doc: document.docx document.docxdocument.docx Page 19 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
50.0 1X100% RECIPROCATING COMPRESSOR WITH TWO (2) STAGES WILL BE INSTALLED FOR WBAS WB ASSOCIATED GAS COMPRESSOR.
51.0 1X100% WB LIFT GAS COMPRESSOR WITH THREE (3) STAGES WILL COMPRESSES THE LIFT GAS. THE LIFT GAS WILL RETURN TO WB WELLS AND SEND TO WB TRUNKLINE.
52.0 TWO (2) STAGES VRU COMPRESSOR TO BE INSTALLED TO COMPRESS THE VAPOR OUTLET FROM GAS BOOT (194-T-100) FROM 0.31 PSIG TO 105 PSIG. RECOVERED GAS FROM VRU COMPRESSOR DISCHARGE WILL BE SENT TO 1ST STAGE ASSOCIATED GAS AND LIFT GAS COMPRESSOR SUCTION SCRUBBERS (194195-V-100).
53.0 THE BOOSTED GAS AND THE ASSOCIATED GAS FROM THE PRODUCTION SEPARATOR IS MIXED AND INTRODUCED TO THE ASSOCIATED GAS COMPRESSOR. THE ASSOCIATED GAS COMPRESSOR COMPRESSES THE MIXED GAS AND SENDS IT TO CPS VIA WB TRUNKLINE.
54.0 FEED STREAM COMPOSITION
55.0 COMPOSITION OF THE FLUID ENTERING WB PRODUCTION SEPARATOR IS TAKEN FROM PROCESS DESIGN BASIS (BCD4-000-42-DBM-4-001-00). TABLE 4-1 BELOW SHOWS THE FLUID COMPOSITION ENTERING THE PRODUCTION SEPARATOR. THE FLUID COMPOSITION IS BASED ON THE SATURATED GAS WITH WATER.
56.0
57.0
58.0
59.0
60.0
61.0
Doc: document.docx document.docxdocument.docx Page 20 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
62.0
63.0 TABLE 4-1
64.0 FEED STREAM COMPOSITION
65.0
Doc: document.docx document.docxdocument.docx Page 21 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
66.0 FLUID COMPOSITION TO PRODUCTION
SEPARATOR
67.0 COMPONENT 68.0 MOLE %
69.0 CO2 70.0 2.12632.2020
71.0 H2S 72.0 0.00000.0000
73.0 NITROGEN 74.0 0.88850.9201
75.0 METHANE 76.0 36.934738.2497
77.0 ETHANE 78.0 6.96507.2130
79.0 PROPANE 80.0 8.16298.4535
81.0 I-BUTANE 82.0 1.77911.8425
83.0 N-BUTANE 84.0 2.20392.2824
85.0 I-PENTANE 86.0 0.84770.8779
87.0 N-PENTANE 88.0 0.66220.6858
89.0 N-HEXANE 90.0 0.67870.7029
91.0 N-HEPTANE 92.0 0.71170.7370
93.0 N-OCTANE 94.0 0.78060.8083
95.0 N-NONANE 96.0 0.50430.5222
Doc: document.docx document.docxdocument.docx Page 22 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
97.0 N-DECANE 98.0 0.40020.4145
99.0 N-C11 100.0 0.31380.3250
101.0 N-C12 102.0 0.23200.2402
103.0 N-C13 104.0 0.24170.2503
105.0 N-C14 106.0 0.21460.2222
107.0 N-C15 108.0 0.26350.2729
109.0 N-C16 110.0 0.15270.1582
111.0 N-C17 112.0 0.12050.1248
113.0 N-C18 114.0 0.14890.1542
115.0 N-C19 116.0 0.08440.0874
117.0 N-C20 118.0 0.79710.8255
119.0 H2O 120.0 33.785031.4275
121.0 TOTAL 122.0 100
Doc: document.docx document.docxdocument.docx Page 23 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
123.0 SOURCE: PROCESS DESIGN BASIS (BCD4-000-42-DBM-4-001-00)
124.0COMPRESSOR TYPE AND EFFICIENCY
125.0ALL COMPRESSORS ARE ASSUMED TO BE RECIPROCATING TYPE AND SIMULATED WITH THE ASSUMED EXPECTED EFFICIENCY OF 90%.
126.0PRODUCTION SEPARATOR OPERATING PRESSURE
127.0SWB PRODUCTION SEPARATOR OPERATING PRESSURE = 100 PSIG.
128.0LIFT GAS FLOW AND PRESSURE
129.0TOTAL LIFT GAS REQUIRED FOR WB (17 WELLS) IS 10.2 MMSCFD. IT IS ASSUMED ASSUMED 50% OF THE WELLS WILL REQUIRED GAS LIFT AT THE SAME TIME SO THAT THE LIFT GAS REQUIREMENT WOULD BE 5.1 MMSCFD. THE LIFT GAS COMPRESSORS ARE DESIGNED TO ACCOMMODATE 7 MMSCFD OF GAS LIFT GAS COMPRESSORSAND THE DISCHARGE PRESSURE IS TAKEN AS 1260 PSIG CONSIDERING INJECTION PRESSURE 1200 PSI AT CASING HEAD.
130.0FUEL GAS CONDITIONING PROCESS
131.0THE FUEL GAS CONDITIONING PROCESS WAS SIMULATED BY USING THE PRELIMINARY DATA FROM VENDOR OF FUEL GAS CONDITIONING PACKAGE. A MEMBRANE SYSTEM IS CONSIDERED TO BE USED IN THIS PROCESS. A COMPONENT SPLITTER WAS ASSUMED TO BE USED AS A MEMBRANE IN THIS SIMULATION. THE COMPONENT SPLIT FRACTION OF PERMEATE GAS AND CONDITIONED GAS WAS TAKEN FROM H&MB GIVEN BY THE VENDOR OF FUEL GAS CONDITIONING PACKAGE. ATTACHMENT 5 SHOWS THE H&MB FOR THE FUEL GAS CONDITIONING PACKAGE.
132.0
133.0RESULT AND DISCUSSION
134.0IMPACT OF INJECTING FREE WATER AT INLET OF PRODUCTION SEPARATOR
Doc: document.docx document.docxdocument.docx Page 24 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
135.0FREE WATER OF 1,000 BBL/DAY IS INJECTED AT THE INLET OF THE PRODUCTION SEPARATOR TO OBSERVE THE IMPACT ON THE ASSOCIATED GAS COMPRESSOR SUCTION COMPOSITION. THE SIMULATION HAS SHOWN THAT THERE IS NO SIGNIFICANT EFFECT OF INJECTING FREE WATER BECAUSE THE ASSOCIATED GAS IS ALREADY ON NEARLY AT WATER SATURATED CONDITION AND MOST OF THE WATER HAS BEEN KNOCKED OUT AT THE PRODUCTION SEPARATOR. TABLE 5-1 BELOW SHOWS THE COMPARISON OF INLET ASSOCIATED GAS COMPRESSOR COMPOSITION ON BOTH CASES.
136.0
137.0TABLE 5-1
138.0INLET COMPRESSOR COMPOSITION
139.0
Doc: document.docx document.docxdocument.docx Page 25 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
140.0 COMPOSITION OF INLET ASSOCIATED GAS
COMPRESSOR
141.0 142.0 CASE 1 143.0 CASE 2
144.0 COMPONE
NT 145.0 MOLE % 146.0 MOLE %
147.0 CO2 148.0 3.6183.512 149.0 3.6133.507
150.0 H2S 151.0 0.0000.000 152.0 0.0000.000
153.0 NITROGEN 154.0 1.3181.462 155.0 1.3181.462
156.0 METHANE157.0 59.70260.8
41158.0 59.69560.8
42
159.0 ETHANE160.0 11.82811.5
25161.0 11.82511.5
25
162.0 PROPANE163.0 14.00613.3
90164.0 14.00113.3
90
165.0 I-BUTANE 166.0 2.9312.761 167.0 2.9312.761
168.0 N-BUTANE 169.0 3.4883.285 170.0 3.4903.285
171.0 I-PENTANE 172.0 1.0651.017 173.0 1.0671.017
174.0 N-PENTANE 175.0 0.7470.720 176.0 0.7500.720
177.0 N-HEXANE 178.0 0.3760.392 179.0 0.3780.392
Doc: document.docx document.docxdocument.docx Page 26 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
140.0 COMPOSITION OF INLET ASSOCIATED GAS
COMPRESSOR
141.0 142.0 CASE 1 143.0 CASE 2
144.0 COMPONE
NT 145.0 MOLE % 146.0 MOLE %
180.0 N-HEPTANE 181.0 0.1470.170 182.0 0.1490.170
183.0 N-OCTANE 184.0 0.0550.069 185.0 0.0560.069
186.0 N-NONANE 187.0 0.0130.017 188.0 0.0130.017
189.0 N-DECANE 190.0 0.0040.005 191.0 0.0040.005
192.0 N-C11 193.0 0.0010.001 194.0 0.0010.001
195.0 N-C12 196.0 0.0000.000 197.0 0.0000.000
198.0 N-C13 199.0 0.0000.000 200.0 0.0000.000
201.0 N-C14 202.0 0.0000.000 203.0 0.0000.000
204.0 N-C15 205.0 0.0000.000 206.0 0.0000.000
207.0 N-C16 208.0 0.0000.000 209.0 0.0000.000
210.0 N-C17 211.0 0.0000.000 212.0 0.0000.000
213.0 N-C18 214.0 0.0000.000 215.0 0.0000.000
Doc: document.docx document.docxdocument.docx Page 27 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
140.0 COMPOSITION OF INLET ASSOCIATED GAS
COMPRESSOR
141.0 142.0 CASE 1 143.0 CASE 2
144.0 COMPONE
NT 145.0 MOLE % 146.0 MOLE %
216.0 N-C19 217.0 0.0000.000 218.0 0.0000.000
219.0 N-C20 220.0 0.0000.000 221.0 0.0000.000
222.0 H2O 223.0 0.7010.833 224.0 0.7100.838
225.0 TOTAL 226.0 100 227.0 100
Doc: document.docx document.docxdocument.docx Page 28 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
228.0
229.0COMPRESSORS DATA
230.0
231.0TABLE 5-2 SHOWS THE SUMMARY OF COMPRESSOR DATA RESULTING FROM HYSYS SIMULATION BY ASSUMING COMPRESSOR EFFICIENCY OF AT 90%. ALL OF THE DATA STILL NEEDARE SUBJECT TO BE CONFIRMEDATION BY FROM COMPRESSOR VENDORMANUFACTURER.
232.0TABLE 5-2
233.0COMPRESSORS DATA
234.0
Doc: document.docx document.docxdocument.docx Page 29 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
235.0 T
A
G
N
O
.
236.0 TA
G
N
A
M
E
237.0 TYPE 238.0 GAS FLOW
(MMSCFD)
239.0 PRESSURE (PSIG) 240.0 C
O
M
P
RA
TI
O
241.0 POWER (HP)
246.0 SUC
TION
247.0 DISC
HARG
E
253.0 CAS
E 1
254.0 CAS
E 2
255.0 256.0 258.0 CAS
E 1
259.0 CAS
E 2
260.0 195-K-100
261.0
262.0 WB ASSOCIATED GAS COMPRESSOR
263.0 (1ST
STAGE)
264.0
265.0 RECIP.
266.0 9.309.79
267.0 9.309.79
268.0 85.0087.3
269.0 263.10277.4
270.0 2.792.86
271.0 522.80578.9
272.0 523.10579
274.0
275.0 W
277.0 279.0 9.839 84
281.0 9.839 84 (NO
282.0 253.10264.
283.0 860.00824.
284.0 3.273.
285.0 614.70570.
286.0 614.70570
Doc: document.docx document.docxdocument.docx Page 30 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
B ASSOCIATED GAS COMPRESSOR
276.0 (2N
D STAGE)
278.0 RECIP.
280.0 (NOTE 1)
TE 1)
4 5 01 1
Doc: document.docx document.docxdocument.docx Page 31 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
287.0 195-K-101
288.0
289.0 WB VRU COMPRESSOR (1ST
STAGE)
290.0
291.0 RECIP.VANE
292.0 0.250.2554
293.0 0.250.2554
294.0 1.000.3
295.0 33.3027.67
296.0 3.062.82
297.0 14.9814.27
298.0 14.9614.27
300.0
301.0 WB VRU COMPRESSOR (2N
D STAG
302.0
303.0
304.0 RECIPVANE
305.0
306.0 0.25 0.2791 (NOTE 1)
307.0 0.250.2791 (NOTE 1)
308.0 31.3014.67
309.0 105.00105
310.0 2.604.08
311.0 13.0420.63
312.0 13.0120.63
Doc: document.docx document.docxdocument.docx Page 32 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
E)
Doc: document.docx document.docxdocument.docx Page 33 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
313.0 195-K-102
314.0
315.0 WB LIFT GAS COMPRESSOR (1ST
STAGE)
316.0
317.0 RECIP.
318.0 7.005.1
319.0 7.005.1
320.0 85.0077.3
321.0 213.10227.5
322.0 2.282.63
323.0 315.40276.5
324.0 315.60276.5
326.0
327.0
328.0 WB LIFT GAS COMPRESSOR
329.0
330.0
331.0 RECIP.
332.0 4.9837.17
333.0 (NOTE 12)
334.0 4.9837.17 (NOTE 12)
335.0 203.10214.5
336.0 586.60850
337.0 2.763.77
338.0 395.10366.1
339.0 395.10366.1
Doc: document.docx document.docxdocument.docx Page 34 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
(2N
D STAGE)
341.0
342.0 WB LIFT GAS COMPRESSOR (3R
D STAGE)
343.0
344.0
345.0 RECIP.
346.0
347.0 4.7386.98
348.0 (NOTE 32)
349.0 4.7386.98 (NOTE 32)
350.0 576.60837
351.0 1260.001260
352.0 2.161.50
353.0 259.6083.61
354.0 259.5083.6
Doc: document.docx document.docxdocument.docx Page 35 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
355.0
356.0 NOTE:
357.0 INCLUDING RECYCLE FLOW FROM DISCHARGE KO DRUM / SCRUBBER.
358.0 GAS FLOW DECREASE BECAUSE OF 0.31 MMSCFD FUEL GAS SUPPLY.
359.0 DECREASING GAS FLOW DUE TO CONDENSATION AT 195-E-1044 (LIFT GAS COMPRESSOR AFTER INTER COOLER-2ND 2ND STAGE).
360.0
361.0
362.0
363.0FLARE ASSOCIATED GAS RECOVERY RATE
364.0THE ASSOCIATED GAS RECOVERY RATE FROM WB ASSOCIATED GAS RECOVERY FACILITIES IS SHOWN IN TABLE 5-3 BELOW.
365.0TABLE 5-3
366.0WB ASSOCIATED GAS RECOVERY RATE
367.0
Doc: document.docx document.docxdocument.docx Page 36 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
368.0
369.0 FLOWRATE
371.0 GAS
372.0 CONDE
NSATE
373.0 W
AT
E
R
375.0 (MM
SCF
D) 376.0 (BPD)
377.0 (B
P
D)
378.0 C
A
S
E
1
379.0 7.363 380.0 97.730
381.0 0.164
382.0 C
A
S
E
2
383.0 7.359 384.0 97.780
385.0 0.164
Doc: document.docx document.docxdocument.docx Page 37 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
386.0
387.0THIS ASSOCIATED GAS WAS TAKEN FROM OUTLET OF THE ASSOCIATED GAS COMPRESSOR KO DRUM EXCLUDING THE 3.497 MMSFCFD FUEL GAS SUPPLY FOR PRODUCING 0.6 MMSCFD OF CONDITIONED FUEL GAS. THE REMAINING GAS FROM OUTLET OF THE LIFT GAS COMPRESSOR KO DRUM WHICH WAS NOT INJECTED TO WELL HAS ALREADY INCLUDED IN THIS ASSOCIATED GAS RATE.
388.0THE PRESSURE DROP OF LIFT GAS ACROSS 195-PCV-115 FROM 1260 PSIG TO 850 PSIG WILL CAUSE A LIQUID CONDENSATION IN THE GAS STREAM. THEREFORE, LIQUID PRESENT IN THE GAS STREAM TO WB TRUNKLINE.
389.0AS PER SIMULATION RESULT, THE FLARE GAS RECOVERY RATE FROM WB ASSOCIATED GAS FACILITIES IS AS FOLLOWS:
390.0GAS CASE 1 = 9.335 MMSCFD (CASE 1 AND CASE 2)
391.0CONDENSATECASE 2 = 9.334 MMSCFD 0 BPD (CASE 1 AND CASE 2)
392.0WATER = 0 BPD (CASE 1 AND CASE 2)
393.0
394.0
395.0
396.0
397.0
398.0
399.0THE ASSOCIATED GAS COMPOSITION TO WB TRUNKLINE IS SHOWN IN TABLE 5-3 4 BELOW.
Doc: document.docx document.docxdocument.docx Page 38 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
400.0
401.0TABLE 5-34
402.0WB ASSOCIATED GAS COMPOSITION
403.0
Doc: document.docx document.docxdocument.docx Page 39 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
404.0 GAS COMPOSITION TO WB TRUNKLINE
405.0 406.0 CASE 1 407.0 CASE 2
408.0 COMPONENT
409.0 MOLE %
410.0 MOLE %
411.0 CO2 412.0 3.6723.561
413.0 3.6683.556
414.0 H2S 415.0 0.0000.000
416.0 0.0000.000
417.0 NITROGEN
418.0 1.3451.485
419.0 1.3451.485
420.0 METHANE
421.0 60.79461.776
422.0 60.79861.779
423.0 ETHANE 424.0 11.94411.656
425.0 11.94311.657
426.0 PROPANE
427.0 13.89913.413
428.0 13.89713.414
429.0 I-BUTANE
430.0 2.8402.718
431.0 2.8402.718
432.0 N-BUTANE
433.0 3.3363.198
434.0 3.3373.199
435.0 I-PENTAN
436.0 0.9590.937
437.0 0.9600.937
Doc: document.docx document.docxdocument.docx Page 40 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
404.0 GAS COMPOSITION TO WB TRUNKLINE
405.0 406.0 CASE 1 407.0 CASE 2
408.0 COMPONENT
409.0 MOLE %
410.0 MOLE %
E
438.0 N-PENTANE
439.0 0.6530.645
440.0 0.6540.646
441.0 N-HEXANE
442.0 0.2570.278
443.0 0.2570.278
444.0 N-HEPTANE
445.0 0.0600.069
446.0 0.0600.069
447.0 N-OCTANE
448.0 0.0100.010
449.0 0.0100.010
450.0 N-NONANE
451.0 0.0010.001
452.0 0.0010.001
453.0 N-DECANE
454.0 0.0000.000
455.0 0.0000.000
456.0 N-C11 457.0 0.0000.000
458.0 0.0000.000
Doc: document.docx document.docxdocument.docx Page 41 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
404.0 GAS COMPOSITION TO WB TRUNKLINE
405.0 406.0 CASE 1 407.0 CASE 2
408.0 COMPONENT
409.0 MOLE %
410.0 MOLE %
459.0 N-C12 460.0 0.0000.000
461.0 0.0000.000
462.0 N-C13 463.0 0.0000.000
464.0 0.0000.000
465.0 N-C14 466.0 0.0000.000
467.0 0.0000.000
468.0 N-C15 469.0 0.0000.000
470.0 0.0000.000
471.0 N-C16 472.0 0.0000.000
473.0 0.0000.000
474.0 N-C17 475.0 0.0000.000
476.0 0.0000.000
477.0 N-C18 478.0 0.0000.000
479.0 0.0000.000
480.0 N-C19 481.0 0.0000.000
482.0 0.0000.000
483.0 N-C20 484.0 0.0000.000
485.0 0.0000.000
486.0 H2O 487.0 0.23 488.0 0.23
Doc: document.docx document.docxdocument.docx Page 42 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
404.0 GAS COMPOSITION TO WB TRUNKLINE
405.0 406.0 CASE 1 407.0 CASE 2
408.0 COMPONENT
409.0 MOLE %
410.0 MOLE %
00.251 00.251
489.0 TOTAL 490.0 100 491.0 100
Doc: document.docx document.docxdocument.docx Page 43 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
492.0
493.0
494.0HYDRATE FORMATION PREDICTION
495.0THIS HYSYS SIMULATION WAS ALSO USED TO DETERMINE THE HYDRATE FORMATION OF THE COMPRESSOR SUCTION PRESSURE CONTROL RECYCLE LINES ON AG, LG AND VRU COMPRESSORS PACKAGE. TABLE 5-5 BELOW SHOWS THE SUMMARY OF HYDRATE FORMATION PREDICTION.
496.0
497.0TABLE 5-5
498.0SUMMARY OF HYDRATE FORMATION PREDICTION
499.0
Doc: document.docx document.docxdocument.docx Page 44 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
500.0 N
O
.
501.0 LI
N
E
502.0 F
R
O
M
503.0 T
O
504.0 UPSTREAM 505.0 DOWNSTRE
AM
506.0 HYDRATE
FORMATION
507.0 REM
ARKS
520.0 P
(P
SI
G)
521.0 T
(O
F
)
522.0 P
(
P
S
I
G
)
523.0 T
(O
F
)
524.0 T
(O
F
)
525.0 P
(
P
S
I
G
)
527.0
528.0 1
529.0 AG RECYCLE
530.0 195-V-102
531.0 195-V-100
532.0 850.0
533.0 120.0
534.0 85.0
535.0 43.4
536.0 38.0
537.0 136.5
538.0 WILL NOT FORM
539.0
540.0 2
541.0 LG RECYCLE
542.0 195-V-108
543.0 195-V-105
544.0 1250.0
545.0 120.0
546.0 85.0
547.0 19.6
548.0 37.8 549.0 -
550.0 WILL FORM
551.0
552.0 3
553.0 VRU RECYCLE
554.0 195-V-109
555.0 195-V-103
556.0 95.0
557.0 120.0
558.0 1.0
559.0 105.3
560.0 -4.0 561.0 -
562.0 WILL NOT FORM
Doc: document.docx document.docxdocument.docx Page 45 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
563.0
564.0FROM TABLE 5-5 ABOVE, IT CAN BE CONCLUDED THAT HYDRATE FORMATION WILL POSSIBILITY OCCURS ON LG RECYCLE DUE TO DRAMATIC DECREASE ON THE PRESSURE FROM UPSTREAM TO DOWNSTREAM WHICH WILL ALSO CAUSE THE CHANGE OF THE TEMPERATURE.
565.0TO OVERCOME THE HYDRATE FORMATION ISSUE, CONTRACTOR PROPOSES TO MODIFY THE TAPPING POINT OF THE LG COMPRESSOR SUCTION PRESSURE CONTROL RECYCLE LINES USING HOT RECYCLE LINE. THE TAPPING POINT WILL BE MODIFIED FROM DISCHARGE KO DRUM (AFTER FINAL STAGE COOLER) TO DISCHARGE FINAL STAGE COMPRESSOR (BEFORE FINAL STAGE COOLER).
566.0TABLE 5-6 BELOW SHOWS THE SUMMARY OF HYDRATE FORMATION PREDICTION AFTER MODIFYING THE COMPRESSOR SUCTION PRESSURE CONTROL RECYCLE TAPPING POINT.
567.0
568.0TABLE 5-6
569.0SUMMARY OF HYDRATE FORMATION PREDICTION USING HOT RECYCLE
570.0
Doc: document.docx document.docxdocument.docx Page 46 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
571.0 N
O
.
572.0 LI
N
E
573.0 F
R
O
M
574.0 T
O
575.0 UPSTREAM 576.0 DOWNSTRE
AM
577.0 HYDRATE
FORMATION
578.0 REM
ARKS
591.0 P
(P
SI
G)
592.0 T
(O
F
)
593.0 P
(
P
S
I
G
)
594.0 T
(O
F
)
595.0 T
(O
F
)
596.0 P
(
P
S
I
G
)
598.0
599.0 1
600.0 AG RECYCLE
601.0 195-V-108
602.0 195-V-100
603.0 850.0
604.0 120.0
605.0 85.0
606.0 43.4
607.0 38.0
608.0 136.5
609.0 WILL NOT FORM
610.0
611.0 2
612.0 LG RECYCLE
613.0 195-K-102 (3R
D STAGE)
614.0 185-V-105
615.0 1260.0
616.0 217.3
617.0 85.0
618.0 141.7
619.0 37.8 620.0 -
621.0 WILL NOT FORM
622.0
623.0 3
624.0 VRU RECYCLE
625.0 185-V-109
626.0 185-V-103
627.0 95.0
628.0 120.0
629.0 1.0
630.0 105.3
631.0 -4.0 632.0 -
633.0 WILL NOT FORM
Doc: document.docx document.docxdocument.docx Page 47 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
634.0
635.0FROM TABLE 5-6 ABOVE, IT WAS PREDICTED THAT HYDRATE FORMATION WILL NOT OCCURS ON LG COMPRESSOR SUCTION PRESSURE RECYCLE LINES AFTER MODIFYING THE TAPPING POINT. COMPRESSOR PACKAGE VENDOR SHALL BE REQUIRED TO STUDY THIS HYDRATE FORMATION IN MORE DETAIL.
636.0COOLER DUTY REQUIREMENT AT 100% RECYCLE
637.0SIMULATION FOR 100% RECYCLE WAS PERFORMED TO CHECK THE COOLER DUTY REQUIREMENT IN ORDER TO MEET THE ALLOWABLE LIMIT OF DISCHARGE TEMPERATURE WHICH WAS SET AT 120 OF.
638.0TABLE 5-7 BELOW SHOWS THE COMPARISON OF COOLER DUTY REQUIREMENT AT 0% AND 100% RECYCLES. THE SIMULATION WAS PERFORMED BASED ON CASE 2 DESIGN CONDITION AFTER MODIFYING THE TAPPING POINT OF THE AG AND LG COMPRESSORS SUCTION PRESSURE CONTROL RECYCLE USING HOT RECYCLE LINE.
639.0TABLE 5-7
640.0COMPARISON OF COOLER DUTY REQUIREMENT AT 0% AND 100% RECYCLE
641.0
Doc: document.docx document.docxdocument.docx Page 48 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
642.0 T
A
G
N
O
.
643.0 TAG NAME 644.0 DUTY
(BTU/HR)
645.0 DEVI
ATIO
N OF
DUTY
646.0 TEMPERATURE (OF) 647.0 REM
ARK
S652.0 INLET 653.0
654.0 OU
TL
ET
658.0 0 659.0 100
%
661.0 0
%
662.0 1
0
0
%
665.0
666.0 195-E-100
667.0 AG COMP. INTER COOLER
668.0 -
669.0 -3.17E+06 670.0 163%
671.0 206.5
672.0 330.7 673.0 120 674.0 HOT
RECYCLE675.0
676.0 195-E-101
677.0 AG COMP. AFTER COOLER
678.0 -679.0 0.00
E+00
680.0 -100%
681.0 242.9 682.0 - 683.0 -
685.0
686.0 195-E-10
687.0 VRU COMP. INTER COOLER
688.0 - 689.0 -3.44E+04
690.0 53% 691.0 160.8
692.0 184.0
693.0 120 694.0 COLD RECYCLE
Doc: document.docx document.docxdocument.docx Page 49 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
642.0 T
A
G
N
O
.
643.0 TAG NAME 644.0 DUTY
(BTU/HR)
645.0 DEVI
ATIO
N OF
DUTY
646.0 TEMPERATURE (OF) 647.0 REM
ARK
S652.0 INLET 653.0
654.0 OU
TL
ET
658.0 0 659.0 100
%
661.0 0
%
662.0 1
0
0
%
6
695.0
696.0 195-E-107
697.0 VRU COMP. AFTER COOLER
698.0 -
699.0 -3.87E+04 700.0 -34%
701.0 188.2
702.0 190.6 703.0 120
705.0
706.0 195-E-103
707.0 LG COMP. INTER COOLER (1ST STAGE)
708.0 -
709.0 -1.20E+06 710.0 83%
711.0 184.7
712.0 235.7 713.0 120
714.0 HOT RECYCLE
715.0
716.0 195-E-1
717.0 LG COMP. INTER COOLER (2ND STAGE)
718.0 - 719.0 -1.34E+06
720.0 -5% 721.0 226.7
722.0 222.3
723.0 120
Doc: document.docx document.docxdocument.docx Page 50 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
642.0 T
A
G
N
O
.
643.0 TAG NAME 644.0 DUTY
(BTU/HR)
645.0 DEVI
ATIO
N OF
DUTY
646.0 TEMPERATURE (OF) 647.0 REM
ARK
S652.0 INLET 653.0
654.0 OU
TL
ET
658.0 0 659.0 100
%
661.0 0
%
662.0 1
0
0
%
04
725.0
726.0 195-E-105
727.0 LG COMP. AFTER COOLER (3RD STAGE)
728.0 -729.0 0.00
E+00
730.0 -100%
731.0 217.3 732.0 - 733.0 -
735.0
Gas Composition to WB Trunkline Case 1 Case 2Component Mole % Mole %
CO2 3.561 3.556
H2S 0.000 0.000Nitrogen 1.485 1.485Methane 61.772 61.774Ethane 11.656 11.656Propane 13.414 13.415i-Butane 2.719 2.719n-Butane 3.199 3.200i-Pentane 0.937 0.938n-Pentane 0.646 0.646n-Hexane 0.278 0.278n-Heptane 0.069 0.069n-Octane 0.010 0.010n-Nonane 0.001 0.001n-Decane 0.000 0.000
Doc: document.docx document.docxdocument.docx Page 51 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
n-C11 0.000 0.000n-C12 0.000 0.000n-C13 0.000 0.000n-C14 0.000 0.000n-C15 0.000 0.000n-C16 0.000 0.000n-C17 0.000 0.000n-C18 0.000 0.000n-C19 0.000 0.000n-C20 0.000 0.000H2O 0.252 0.252Total 100 100
ATTACHMENT -1HYSYS SIMULATION
Doc: document.docx document.docxdocument.docx Page 52 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
ATTACHMENT -2HYDRAULIC CALCULATION
Doc: document.docx document.docxdocument.docx Page 53 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
ATTACHMENT -3WB-SB Production Forecast
736.0ATTACHMENTS
Attachment – 1 : HYSYS Simulation Process Flow Diagram (Case 1)
Attachment – 2 : HYSYS Simulation Process Flow Diagram (Case 2)
Attachment – 2 3 : Stream Data (Case 1)
Attachment – 4 : Stream Data (Case 2)
Attachment – 5 : H&MB Fuel Gas Conditioning Package
Doc: document.docx document.docxdocument.docx Page 54 27302601-JulNovMay-09 13
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
ATTACHMENT 1
HYSYS SIMULATION PROCESS FLOW DIAGRAM (CASE 1)
Doc: document.docx document.docxdocument.docx Page 55 4/28/2023273026
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
ATTACHMENT 2
HYSYS SIMULATION PROCESS FLOW DIAGRAM (CASE 2)
Doc: document.docx document.docxdocument.docx Page 56 4/28/2023273026
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
ATTACHMENT 32
STREAM DATA (CASE 1)
Doc: document.docx document.docxdocument.docx Page 57 4/28/2023273026
PetroChina International Jabung Ltd. Study ReportWB-SB Non Associated Gas Recovery
Simulation
ATTACHMENT 4
STREAM DATA (CASE 2)
Doc: document.docx document.docxdocument.docx Page 58 4/28/2023273026