bcd5-190-42-rpt-4-101-00-rev. d

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


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


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 :


D

: Hig

h Presssur

e Operatin

g Cas

e

Figure 4.1 Process Schematic


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 27302601-JulNovMay-09 13

D


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.



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



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


engineer.process, 04/30/13,


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


engineer.process, 04/30/13,


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


D


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


5 195203A4/B4 195-E-200 195-V-202 Will Not Form

6 195203A5/B5 195-V-202 195-K-200(2nd


7 195203A6/B6 195-K-200(2nd

Stage)195-E-201 (2nd


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



Simulation

9.0 ATTACHMENT

Attachment – 1 : HYSYS Simulation

Attachment – 2 : Hydraulic Calculation

Attachment – 3 : WB-SB Water Production Forecast



Simulation

10.0 INTRODUCTION



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.



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).



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:



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



Simulation

62.0

63.0 TABLE 4-1

64.0 FEED STREAM COMPOSITION

65.0



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



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



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



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



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



Simulation


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



Simulation


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



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



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



Simulation

B ASSOCIATED GAS COMPRESSOR

276.0 (2N

D STAGE)

278.0 RECIP.

280.0 (NOTE 1)

TE 1)

4 5 01 1



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



Simulation

E)



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



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



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



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



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.



Simulation

400.0

401.0TABLE 5-34

402.0WB ASSOCIATED GAS COMPOSITION

403.0



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



Simulation


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



Simulation


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



Simulation


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



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



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



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



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



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



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



Simulation

642.0 T

A

G

N

O

.


(BTU/HR)

645.0 DEVI

ATIO

N OF

DUTY


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



Simulation

642.0 T

A

G

N

O

.


(BTU/HR)

645.0 DEVI

ATIO

N OF

DUTY


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



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



Simulation

ATTACHMENT -2HYDRAULIC CALCULATION



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



Simulation

ATTACHMENT 1

HYSYS SIMULATION PROCESS FLOW DIAGRAM (CASE 1)

Doc: document.docx document.docxdocument.docx 4/28/2023273026


Simulation

ATTACHMENT 2

HYSYS SIMULATION PROCESS FLOW DIAGRAM (CASE 2)



Simulation

ATTACHMENT 32

STREAM DATA (CASE 1)



Simulation

ATTACHMENT 4

STREAM DATA (CASE 2)



Simulation

ATTACHMENT 5

H&MB FUEL GAS CODITIONING PACKAGE


bcd5-190-42-rpt-4-101-00-rev. d

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