Vol 1 of 1 - Plant Operation Maintenance and Safety Manual

4 A b u D h a b i G a s Industries L t d .

Abu Dhabi Gas Industries Ltd. GASCO Project No. 5221 Ethane Recovery Maximization Project

DIVISION 10 PLANT OPERATION, MAINTENANCE AND SAFETY MANUAL

Volume 1 of 1

FLUOR Contract AOWT 2004

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Operating, Maintenance and Safety Manual Addendum for the ERM Project

Approved Rev.

Date

Description

By

Chk.

Disc.

Proj.

20-Dec-04

Client Comments Incorporated

DTS

DTS

RvdV

MS

26-Sept-04

Issued for Review

DTS

DTS

RvdV

MS

GASCO

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project T A B L E OF CONTENTS

INTRODUCTION CHAPTER 1:

DESIGN BASIS

CHAPTER 2:

PROCESS DESCRIPTION

CHAPTER 3:

INITIAL START-UP

CHAPTER 4:

NORMAL START-UP

CHAPTER 5:

NORMAL OPERATION

CHAPTER 6:

NORMAL SHUTDOWN

CHAPTER 7:

EMERGENCY SHUTDOWN

CHAPTER 8:

SAFETY

CHAPTER 9:

EQUIPMENT AND DATA SHEETS

CHAPTER 10:

DRAWINGS

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

INTRODUCTION

CONTENTS

SECTION

PAGE

1.0

FOREWORD

2

2.0

PROJECT OVERVIEW

3

INTRODUCTION

Fluor Mideast, Ltd. Contract No. AOWT

1.0

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

FOREWORD This manual describes the modifications made to Unit 44 for the Ethane Recovery Maximization (ERM) Project. This manual should be read in conjunction with the existing Unit 44 Operating, Maintenance and Safety Manual and the supplement prepared for the C2 Enhancement Project (Project 1219). The information contained in this manual provides a basis for the safe start-up, normal operation, normal shutdown, and emergency shutdown for the new equipment and systems. The manual provides a description ofthe new E R M operating modes and discusses how the new systems are integrated into the existing unit. The procedures described in this manual should be considered as guidelines and may have to be adapted at site. It is the prime responsibility of the Operations personnel to interpret the instructions and where necessary adjust them to suit the conditions prevailing at any time taking into account the local conditions during the preparation and commissioning of the new E R M extension. In order to facilitate assimilation and understanding of information, the format and contents of this manual follow that of the existing Operating, Maintenance and Safety Manual.

INTRODUCTION

Fluor Mideast, Ltd. Contract No. AOWT

2.0

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

PROJECT OVERVIEW The objective of the E R M Project was to increase the ethane production from Unit 44 by at least 400 TPD based on the design feed rate, composition, and inlet conditions defined in the Design Basis Memorandum. C2 recovery is increased in Unit 44 by adding the following new equipment: • • • • • •

Cold Demethanizer (44-V-308) Cold Demethanizer Bottoms Pumps (44-P-302A/B) 2 Feed Chiller (44-E-318) Debutanizer Trim Condenser (44-E-406) N G L Subcooler (44-E-407) Propane Refrigeration Package (44-ME-201) nd

The new Refrigeration Package includes a two-stage Refrigeration Compressor (44-C-202) with an electric motor driver. An existing air cooler purchased for a previous project is used as the Refrigerant Condenser (44-E-203) for the new system. The package also includes two K O drums (44-V-206/207) and two subcooling exchangers (44-E-204/5).

INTRODUCTION

Fluor Mideast, Ltd. Contract No. AOWT

3.0

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

PURPOSE The puipose of this addendum is: •

To review and explain the modifications that have been made to the existing unit and update, as required, the process description and the start up and shutdown procedures.

•

To provide the procedure to switch from C2 Enhancement mode to E R M mode.

•

To provide the procedure to switch from E R M mode to lower ethane recovery modes.

•

Provide details for the normal operation ofthe E R M mode.

INTRODUCTION

Fluor Mideast, Ltd. ContractNo. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

CHAPTER 1

DESIGN BASIS

CONTENTS

SECTION 1.0

2.0

PAGE

GENERAL

2

1.1

2

Integration of E R M Project into Existing Facilities

FEED CHARACTERISTICS

3

2.1 2.2

Feed Gas Flow and Conditions Feed Gas Composition

3 4

2.3

Flexibility and Turndown

4

3.0

PRODUCT SPECIFICATIONS

5

4.0

3.1 Lean Gas 3.2 N G L 3.3 C5+ Condensate EFFLUENTS

5 5 5 6

5.0

PRINCIPLES OF OPERATION 5.1 5.2 5.3 5.4

Feed Chilling Demethanizer / Recycle Gas Loop Debutanizer New Propane Refrigeration System

7 7 7 8

6.0

PROCESS FLOW DIAGRAMS AND MATERIAL BALANCES

7.0

UTILITY REQUIREMENTS

10

8.0

CHEMICALS AND CONSUMABLES

11

CHAPTER 1

9

Fluor Mideast, Ltd. ContractNo. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

1.0

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

GENERAL A comprehensive Design Basis Memorandum containing mutually agreed and approved compilations of basic data, design criteria, and other parameters was developed for the ERM Project. The key information is provided in this section ofthe manual. Refer to RPT-AOWT44-06-001 for additional data.

1.1

Integration of ERM Project into Existing Facilities OGD-I Train 3 was commissioned in 1996 and processes approximately 610 MMSCFD of Thammama-F gas. The train consists of condensate stabilization (Unit 24), M D E A sweetening (Unit 34), molecular sieve dehydration of gas, and deep-NGL recovery by propane chilling followed by a turboexpander-based unit (Unit 44). OGD-I Train 3 was originally designed to produce a N G L stream containing a minimum quantity of ethane (maximum 5 mol %). However, in 2001, the unit underwent some modifications to recover about 300 TPD of total C2 (known as C2 Enhancement Project) to supplement the feed to the petrochemical plant at Ruwais. The objective ofthe E R M Project was to further increase the ethane production from OGD-I Train 3 by at least 400 TPD based on the design feed rate, composition, and inlet conditions defined in the Design Basis Memorandum. Within OGD-I Train 3, the focus ofthe E R M Project was entirely on Unit 44. No modifications were made to Unit 24 and 34. The main functions of Unit 44 are: •

Chill the sweet gas from Unit 34 to condense HC liquids and water upstream of the molecular sieve dryers

•

Dehydrate the feed gas to the NGL Recovery Unit

•

Recover C2+ NGL

•

Fractionate the raw NGL into a C2-C4 product and a C5+ product

CHAPTER 1

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

2.0

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

FEED CHARACTERISTICS The feed to OGD-I Train 3 is non-associated gas from the Thammama-F reservoir. The well fluid is sent to Unit 24 where the gas is separated from the condensate, and the condensate is stabilized to the specification. The sour gas from Unit 24 is then fed to the Gas Sweetening Unit, Unit 34, for acid gas removal. The sweet gas is sent to Unit 44, the Dehydration and N G L Recovery Units. The following cases were originally considered in the design of Train 3: •

Low Condensate Case

•

Maximum Condensate Case

•

Low H2S Case

Unit 44 was originally designed for the Low Condensate Case, and checked for the other cases. For the E R M Project, the design of the new equipment was based on the Low Condensate Case. The original design feed rate was increased by 5% to reflect the results of Step 1 of the Habshan Capacity Enhancement. The new equipment is also suitable for the Max Condensate Case. As for Low Condensate Case, the original Max Condensate design feed rate was increased by 5% to reflect the results of Step 1 of the Habshan Capacity Enhancement. The rates, conditions, and compositions for the sweet gas from Unit 34 are given in the sections below. 2.1

Feed Gas Flow and Conditions Low Condensate Case

34-V-103

Source of Feed Normal Rate (dry basis), MMscfd Temperature, C 0

Max Condensate Case

616 + 5%

627 + 5% 58 max.

Pressure, barg

65.5 min

Water Content

Saturated

Data source: Low Condensate Case data are from the C2 Enhancement Material Balance, PFD 44-0020012. Max Condensate Case data are from the C2 Enhancement Material Balance, PFD 44-0020-013.

CHAPTER 1

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44

Fluor Mideast, Ltd. Contract No. AOWT

Doc. No.: PP-AOWT-44-00-001

Addendum for the ERM Project - Rev. 1

2.2

GASCO ProjectNo.: 13522102

Feed Gas Composition Outlet of 34-V-103 (Dry Basis) Low Condensate Case

Max Condensate Case

Mole %

Mole %

N2

0.300%

0.319%

Cl

76.766%

75.463

C2

9.313%

9.733

C3

5.089%

5.637

iC4

1.569%

1.771

nC4

2.558%

2.904

iC5

0.714%

0.772

nC5

0.595%

0.640

NC6

0.444%

0.453

NBP[I]_91

0.431%

0.394

NBP[1]_138

0.065%

0.056

NBP[1L182

0.006%

0.005

H2S

20 ppmv

20 ppmv

C02

2.143%

1.850%

M-Mercaptan

11 ppmv

0 ppmv

E-Mercaptan

13 ppmv

0 ppmv

nP-Mercaptan

45 ppmv

18 ppmv

Component

Data Source: Low Condensate Case data are from the C2 Enhancement Material Balance, PFD 440020-012. Max Condensate Case data are from the C2 Enhancement Malerial Balance, PFD 44-0020013.

2.3

Flexibility and Turndown Unit 44 can be operated in either C2 recovery mode or C2 rejection mode. As the objective of the project is to recover additional C2, the design case for the E R M Project was the C2 recovery mode of operation. However, the design of the new equipment allows the unit to be switched back to C2 rejection mode of operation without demerits to existing performance. The plant is also designed with the flexibility to operate at any point between the maximum C2 recovery case and the C2 rejection case. New equipment was designed for turndown to 50% of design rates.

CHAPTER

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

Fluor Mideast, Ltd. Contract No. AOWT

3.0

PRODUCT SPECIFICATIONS

3.1

Lean Gas

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

The lean gas specifications are given below. 0

Hydrocarbon dew point

-5 C max. at 39.2 bara

Water dew point

-30 C max. at 39.2 bara

H2S Content

20 ppm vol. max

Net calorific value

900 BTU/SCF min.

o

Required conditions at the export gas grid: Temperature

62°C max.

Pressure

41.5 barg

Data Source: OGD-II "Operating, Maintenance and Safety Manual: Overall Plant Summary and Start-up Considerations", Chapter]: Overall Plant Description. Date: October 1999, Rev.:A, Page 116. 3.2

NGL The N G L product specifications are given below. C2 Recovery Mode

C2 Rejection Mode

C1/C2

4.5 wt% max.

Not Applicable

C02/C2

5.5 wt% max.

Not Applicable

C2 and lighter

Not Applicable

5 mol% max.

Water Content

5 ppm wt max.

5 ppm wt max.

4 mol% max.

4 mol% max.

C5+ Content

3.3

C5+ Condensate The C5+ condensate from the bottom ofthe Debutanizer (44-V-401) is to contain 1 mol% (max.) C4.

CHAPTER 1

Fluor Mideast, Ltd. Contract No. AOWT

4.0

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

EFFLUENTS The ERM Project does not impact the effluents from Unit 44.

CHAPTER 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

Fluor Mideast, Ltd. Contract No. AOWT

GASCO ProjectNo.: 13522102

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44

Doc. No.: PP-AOWT-44-00-001

Addendum for the ERM Project - Rev. 1

5.0

PRINCIPLES OF OPERATION The E R M Project impacts the following areas of Unit 44: •

Feed Chilling

•

Demethanizer / Recycle Gas Loop

•

Debutanizer

•

Propane Refrigeration System

A high-level overview of the modified operation is provided in this section. Refer to Chapter 2 for additional information.

5.1

Feed Chilling The 2nd Feed Chiller (44-E-318) is added upstream of the 1 st Stage Feed K O Drum (44-V301). Propane refrigerant from the new Refrigeration Package is fed to the shell side of the kettle-type exchanger. This new exchanger lowers the temperature profile of the majority of the downstream unit and allows more ethane to be recovered from the feed gas.

5.2

Demethanizer / Recycle Gas Loop The Demethanizer (44-V-306) in Unit 44 is fabricated out of Low Temperature Carbon Steel (LTCS). This currently limits ethane recovery as operating temperatures at the top of the tower must be maintained a safe margin from the design temperature (-45°C). In order to operate at the colder temperatures that result from the addition of the 2 Feed Chiller, a new 8-tray stainless steel Cold Demethanizer (44-V-308) is added. This column acts as an extension ofthe existing Demethanizer. The liquid from the existing Recovery Tower Bottom Flash Drum (44-V-307) and 2nd Stage Liquid from 44-E-314 are combined and fed to the top of 44-V-308. The overhead vapor from 44-V-306 is fed to the bottom of 44-V-308 and the new Cold Demethanizer Bottoms Pumps (44-P-302A/B) pump the liquid from the bottom of 44-V-308 back to the top of 44-V-306 via the existing Demethanizer Reflux Condenser (44-E-305). nd

In the recycle gas loop, new bypasses are added around 44-E-315 and 44-E-303. The total bypass of the 1st Stage Liquid/Recycle Gas Exchanger (44-E-315) helps maintain lower temperatures in 44-V-306. The Recovery Tower Reboiler (44-E-303) is not required when operating in C2 recovery mode.

5.3

Debutanizer Raw N G L from the Demethanizer is sent to the Debutanizer (44-V-401) forfractionationinto C2-C4 N G L and a C5+ product. Currently, the Debutanizer overhead vapor is fully condensed in an air-cooled condenser. The Debutanizer currently operates very close to the design pressure of the equipment. Because the pressure of the Debutanizer cannot be increased any further, the temperature required to condense the Debutanizer overhead stream

CHAPTER 1

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

will decrease as the ethane content of the NGL increases. For the E R M Project, a new Debutanizer Trim Condenser (44-E-406) is added downstream of the existing aircooler to completely condense the C2 rich NGL product. Propane refrigerant from the new Refrigeration Package is fed to the shell side ofthe kettle-type exchanger. New cold insulation is applied to the existing Debutanizer Overhead Accumulator (44-V-402) and to the existing line from 44-V-402 to the Debutanizer Overhead Pumps (44-P-401 A/B). A new N G L Subcooler (44-E-407), which is a kettle-type exchanger with propane refrigerant on the shell side, cools the NGL product from Unit 44 down to 20 C. Subcooling the NGL ensures that the vapor pressure of the combined NGL stream is less than the maximum operating pressure of the existing NGL Storage Spheres (45-V-501 A/B/C). o

5.4

New Propane Refrigeration System The new Refrigeration Package (44-ME-201) includes a two-suction Propane Compressor (44-C-202) with an electric motor driver, a high pressure knock-out drum (44-V-206), a low pressure knock-drum (44-V-207), and a propane receiver (44-V-205). As discussed above, the new system provides the following two levels of refrigerant to the process: 0

o

Low level at about -26 C and 1.0 barg to 44-E-318 for chilling the feed gas

»

High level at about 16 C and 6.4 barg to 44-E-406/7 for condensing and subcooling the N G L product

0

Subcooling the refrigerant is required due to the remote location ofthe new chillers. An existing air cooler (currently tagged 45-E-701) purchased for a previous project is used as the Propane Condenser for the new system (44-E-203).

CHAPTER 1

Fluor Mideast, Ltd. Contract No. AOWT

6.0

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

PROCESS FLOW DIAGRAMS AND MATERIAL BALANCES The E R M Process Flow Diagrams for Unit 44 are included in this section. Drawing Number

Description

44-00-20-001

Inlet Gas Dehydration

44-00-20-003

N G L Recovery Plant Sheet 1

44-00-20-004

N G L Recovery Plant Sheet 2

44-00-20-004A

NGL Recovery Plant Sheet 3

44-00-20-005

Fractionation

44-00-20-006

N G L Refrigeration Area

44-00-20-006A

E R M Refrigeration Package

The following four Material Balance cases are also provided:

CHAPTER 1

Document Number

Description

44-00-20-010

Low Condensate Case - C2 Rejection Mode

44-00-20-011

Max Condensate Case - C2 Rejection Mode

44-00-20-012

Low Condensate Case - C2 Recovery Mode

44-00-20-013

Max Condensate Case - C2 Recovery Mode

44-V-101

44-r-ios

41-F-I01 A/8

,

4'1-ME-^01-8L .

P£C£t€R»nOH C« FLttR

A.lm IQ I 15.Orr. t/t

i/B

44-WE-)0!-H1 fiiCtHEFHItW G»S HUIER - . 1 , GMl/kr

44-/-102/I03/1'34/105 C« CEKYOSlICfiS J.im ID I 5.2a I/l

«f-E-101 (IEC£H;fiit:tn C t i COOLER 5.Si C:oi/Hr

REtfNEPiTlQH C4S 5EF/?l*Tffi

DUTl.tl CtS FlLTEfl

ntt FEzB c*s FROM ^ - E - J l O

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fii

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;s;^o -'dfl fiEwrv

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NOTES; i. * L l TEtPEHMUBIS. PflESSUHES. FLG* QUAHIITIES AUD COI^CSIHOIIS *RE fCR PROCESS 0ESIGJ1 PURPISES DHLT. NO G'JAfUNrEE IS EXPR-SSEO 3R [UPUEO.

I. IHC ClUlPtCNI C»P*C!T1ES U C l CUED CII IKIS P^D REFER IO THE LO* CCNDidSilE WSE. « flECOVtF.r UOOE. :.FOR V-iJEfiJu DRAWINGS: 44-00-20012 i*-00-;001D 4iHX)-2001J *»-00-!00;I

FLUOR. EJHAKE RECOVERV

WL»»K5. fl£FEP IC IHE FDllOUWC : LOK COVDEnSUE C*SE. C2 RECO'/ERI : LOW COH0ENi*TE C*S-:. C2 REJEC"!OH : M»X CON0EHS*TE C»Si. C: RECOVEST : M l CONKHSm C»SE. RZJEC'ION

MAX IMIZAT; OM

PROCESS FLOW OI^GFfiM I M E T GftS DEHYGRflTiON THAMMAMA ' F * S23!

|4,4l

1001

ftl

F[£t) CHILLER 10.78 Gcol/Hr

FECfCLE O'S COVPRESSOR (STElU ItSSlNE DRIVER)

^-£-306 FEED CHiLLEfi B.99 Gcul/Hr

«-E-3:6 1ST S U K L fOyiC/FEtO EJC--»HG£R S . N Ocol/Hr

ISl SEISE lIOJID/HiCYCL: MS FKChlMCEFI 0.03 Gcol/Hr

^4-£-31•^

PtCTCLE IRIH COOLER WD SHOE LlOUIO/fEtD EJCHJHCEB 0.3S CMt/Mr Z-Ot Ceat/hr

-f^-f-JO?

4J-V-306

DEltTHlHITta SIOE REBDILER J.COCeai/Mr

CErflHiVIZEfl BDIIOU RtBOSLEfi i.DCeoi/Hr

DEUElHWIIIER 2.

LP P1PEHSA1E

< -~ L

-, -0-

*

44-E-407

:S;FER O I

PFC 44-00-ZC0051 FOR SHELL SiOE)

< ^

TO s&L STCRAGL

—

; «i-oo-o:-i ~>

-p s : E i y s.-P": - < 62-00-003

3»

6Z-OO-:M

10 CDNDLN'SAT:

SIIRtCE l i f t t 26-'F-lD: i/3

-ESS-

APPROND FGR lONSIRUCIION eepfiOVEO TOP. I S O ISSIJEO FCP APPROVE liSLEO FCF RE»]EW

HQTES: 1. ALL • E I P E B A I U R E S . PRESSURES. FLO* OUA-UIIIES AHD COlPOSiriONS ARE FOR PROCESS OESIvN PURPOSES DMLY. NO CUARAMIEE IS EXPRESSED OR IMPLIED2. ALL FLO RATES WO PROCESS CONDIIIONS SHOVN m AT OPERAIINC C0N0II10I1S. O-T.ESS CTKER^ISE NOTEO. 3. TKE EOUIPMENT CAPAClliES M C I C A T E D OH IHIS PFO REFER TO IHE LC» CCKDENStlc CASE. C2 RECOVERI lOCE. 4. FOR MAT-RIAL DRAVINGS: 44-O0-2CO13 44-00-20010 44-O0-2C013 4'-O0-ZO0H

BALANCES. REFER 10 THE FOL LOW! IiG : : : :

LCW COMDENSATE LOT COWDENSAIE UAX COMOEHSAlE MAX CONDENSATE

NE* LINES. EOUIPNENT. AKD INSIRJICHIS

CASL. CASE. CASE. CASE.

C2 RECOVERV C2 PEJECIION Ct RECDvERY C2 REJECT IOM

FLUOR. THOIJE

RECOVERY MAXIMIZATION PRDCESS FLCW DIAGRAM FRACTiONAT!DN TH^^MftHfl ' F ' ORfiwiNG NUMBER

l±4j

10,0]

PPOJECT

>

44-E-306 FEED CKILLER tcol/Hr

44-V-2CJ nm siiCE sxricN osuu ID » J.T™

T-I

44-v-202 •EFRIGERMK FLASH ORIN Z.ifn IP « 4.0-n I-I

44-C-201 CJ REFRICERATW C0iffitSS3H 12 S7ACB) 5St2 « (SiEAK TlffiflJ.'.E M / V E S ;

4a-v-204 :JO SUCE SUCTICH

2.on ID X M n

aw.

I-I

44-E-310 HEI FEED CHlUEt 10.71 Gcol/Hr

44-E-201 BEFRtSERWI COwaENSER 21.6! Ctol/Hr

44-E-202 REFR1CEPAM I 5U3COOLifl l . l l Gcoi/Xr

44-V-20i RilRICERAHI SUHCE KIM J.CCT ID ) S.Om

T-I

P. SIEAV SUPPLT

E.?. STEAM RETURN < 6;-00-OOj |

--0«-v-JC1 I FRCM IC AT «

;

rr

• r i FEID LJCU13 F=;CU A4-V-IC1

Jfc-

JL FRO>J « - f - i - : ; A / B

/£\

I 2'-C'Q-2O:0?>

JL

J> IFF ROV E J FCR COAISUIIICA

FHC

W i t i t p m , n FOR OESIGM ISSUED fCH APPPOVftL mvu

NOTES: 1. ALL TEMPERATURES. PRESSURCS. ELC" DUAiniTIES XUO COUPOSHIONS ARE FOR PROCESS DESIGN PURPOSES ONLT- NO GUARANTEE IS EXPR-ISSEO OR IfP'.IED. 2. ALL ^LOw RATES AND PROCESS CCNOITIONS SHOWi APE Af (FEB* f I WC COWfTICWS. yvLESS 0IrtER»I5E NE-TEO. J.IHE ZOUIPICNI CAPACITIES IN0ICAIE3 ON IHIS PFD REFEi TO IHE LO* CEWOENSAIE CASE• CZ RECOVERT IODE. 4. FOR IATERIAL BALANCES. REF;R 10 TrE FOLLO*iNG DRAVINGS: 4^-03-?00ir i LCV CONCENSAIE CASE. C2 firCOVES) 4^-02-20010 : LOV CDIICEHSATE CASE. Z i REJLCIION 4'-00-200l3 : MAX CDNCtNEATE CASE- CZ RECOVERi 4 ' - 0 a - 2 0 0 n : UAX CONCENSATE CASE. C2 SEJECTION

ISSLtO FCR R

FLUOR. ETHANE

R E C O V E R t MAX IMf ZA T I O N PRDCESS FLOW DIAGRAM NGL REFRIGERATION AREA THSKMAKP "F" DflAWiHC NUMEIER

PROJECT

44-C-202 PMPASE CDWEESSEH

44-V-2C7 vm PP.tssiRINOZF.CUt ZfLU

44-E-205

44-E-40&

LCi U*EP.UU3£

;.?[« co-^WEfl

0.7* C c a l / *

: I :

I

jl!

I

: :

; ' L

:

44-V-2?t HICH PPESVJRE WOClOlI VWU

a4-E-'i07

Al9

Approved Proj. GASCO

GS-L-FML046

13-Feb-04

Approved for Construction

4-Sep-03

Approved for Design

OPM

DTS

ED

7-Aug-03

Issued for Approval

OPM

DTS

ED

FLUOR Conlracl AOWT Rev.2

GASCO Ethane Reoovery Maxtmization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composilion (kgmole/h) Nilrooen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weighl Vapor Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

1

10

11

20

22

23

24

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

39.5 10013.0 1165.5 568.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

39.5 10013.0 1165.5 588.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

56.3 14281.0 1662.3 838.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5 0.0 0.2 0.2 0.3 0.0

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

96.6 24733.6 3000.5 1639.8 50S.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

96.6 24733.6 3000.5 1639.B 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

96.6 24733.6 3000.5 1639.6 505.5 8242. 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 21.9

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 0.0

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.0 0.0 0.0 0.0 0.0 87.7

0.8 439.5 172.7 212.6 110.3 216.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

32330.0 732576 5B.0 66.5 1.00 -686.7 22.66

32330.0 732576 43.9 65.8 0.98 -694.9 22.66

32330.0 732576 27.0 65.4 0.95 -705.4 22.66

30659.8 653637 27.0 65.3 1.00 -647.7 21.32

30637.9 653241 27.8 62.8 1.00 -645.5 21.32

1582.5 77359 27.0 65.3 0.00 -51.7 48.88

1582.5 77359 18.1 31.4 0.23 -51.7 48.88

87.7 1581 27.0 65.3 0.00 -6.0 18.02

1582.5 77359 51.9 30.7 0.36 -49.7 48.88

12627.7 269239 27.6 62.5 1.00 -266.1 21.32

12627.7 269239 -7.0 60.8 0.91 -274.2 21.32

18010.1 384000 27.6 62.5 1.00 •379.5 21.32

14023.5 299000 27.5 62.4 1.00 -295.5 21.32

64.4 0.62 0.014 0.034 22.66 732575 647.9

66.6 0.64 0.014 0033 22.14 703470 636.6

69.3 0.66 0.014 0.032 21.32 653737 614.4

69.2 0.66 0.014 0.032 21.32 653637 614.4

65.6 0.65 0.013 0.032 21.32 653241 614.0

69.2 0.66 0.014 0.032 21.32

32.4 0.54 0.012 0.027 22.08 8149 7.4

69.2 0.66 0.014 0.032 21.32

35.0 0.54 0.013 0.028 27.02 15318 11.4

65.3 0.65 0.013 0.032 21.32 269239 253.1

71.9 0.74 0.012 0.030 19.72 227245 230.9

65.3 0.65 0.013 0.032 21.32 384000 360.9

65.2 0.65 0.013 0.032 21.32 299000 281.0

529.8 0.60 0.129 0.073 7.99 55.33 28130 53.1

513.4 0.60 0.121 0.074 7.70 48.87 77259 150.5

513.6 0.60 0.121 0.074 7.71 48.88

513.6 0.60 0.121 0.074 7.71 48.88 77359 150.6

577.8 0.57 0.168 0.081 10.59 57.04 69207 119.8

513.6 0.60 0.121 0.074 7.71 48.88

551.9 0.60 0.137 0.073 8.59 61.09 62041 112.4

976

1580

—

Simulation Basis: Train 3 - Selecled Option + 5'X. - C3 Mode Rev. 5A

o.o

1581

Paget of 10

480.6 0.62 0.103 0.079 7.53 38.02 41994 87.4

FLUOR Contract AOWT Rev.2

GASCO Elhane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Compoaition (kgmole/h) Nilrogen Methane Ethane Propane I-Butane n-8utane i-Pentane n-Pentane n-Hexane NBP91 NBP138 'NBP182 H2S C02

25

26

28

29

30

31

32

33

34

36

37

38

43

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9

56.3 14281.0 1662.3 83B.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7

93.9 23052.2 2308.3 869.6 169.6 216.5 27.3 18.1 3.7 1.3 0.0 0.0 0.5 596.8

54.7 13434.6 1345.2 506.8 99.0 126.2 15.9 10.5 2.2 0.7 0.0 0.0 0.3 349.0

54.7 13434.6 1345.2 506.8 99.0 126.2 15.9 10.5 2.2 0.7 0.0 0.0 0.3 349.0

14.6 3622.9 362.8 136.7 26.7 34.0 4.3 2.8 0.6 0.2 0.0 0.0 0.1 94.1

14.8 3622.9 362.8 136.7 26.7 34.0 4.3 2.8 0.6 0.2 0.0 0.0 0.1 94.1

93.9 23052.4 2308.4 869.7 169.8 216.5 27.3 18.1 3.7 1.3 0.0 0.0 0.5 598.8

92.2 22086.3 1945.6 564.8 79.9 85.5 6.2 3.5 0.3 0.1 0.0 0.0 0.4 546.0

92.2 22086.3 1945.6 564.8 79.9 85.5 6.2 3.5 0.3 0.1 0.0 0.0 0.4 546.0

CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Row (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat How (Qcal/h)

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

0.1 0.1 0.2 0.0

0.0 0.0 0.1 0.0

0.0 0.0 0.1 0.0

0.2 0.2 0.3 0.0

0.3 0.3 0.5 0.0

0.1 0.1 0.0 0.0

0.1 0.0 0.0 0.0

0.1 0.0 0.0 0.0

0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0

0.1 0.1 0.0 0.0

0.1 0.0 0.0 0.0

0.1 0.0 0.0 0.0

14023.5 299000 -6.7 61.3 0.91 • -304.5

3986.6 85000 27.5 62.4 1.00 -84.0

3986.6 85000 -21.4 60.9 0.85 -87.8

18010.1 384000 -15.2 60.8 0.88 -394.2

30637.9 653241 -11.9 60.7 0.89 -668.4

27360.2 532785 -11.9 60.7 1.00 -573.6

15945.2 310501 -11.9 60.7 1.00 -334.3

15945.2 310501 -35.9 60.2 0.91 -342.2

4300.0 83734 -11.9 60.7 1.00 -90.2

4300.0 83734 -32.4 60.2 0.93 -91.9

27360.6 532797 -32.3 60.2 0.93 -584.8

25410.9 474718 -32.2 60.2 1.00 -532.7

25410.9 474718 -50.7 39.6 0.95 -535.5

21.32

21.32

21.32

21.32

21.32

19.47

19.47

19.47

19.47

19.47

19.47

18.68

18.68

72.5 0.74 0.012 0.030 19.74 252761 256.6

65.2 0.65 0.013 0.032 21.32 85000 79.9

77.1 0.82 0.012 0.029 19.00 64216 67.7

74.6 0.78 0.012 0.029 19.31 305472 317.0

73.3 0.76 0.012 0.029 19.47 532749 548.3

73.3 0.76 0.012 0.029 19.47 532785 548.3

73.2 0.76 0.012 0.029 19.47 310458 319.5

85.9 0.98 0.012 0.029 18.53 267767 289.7

73.2 0.76 0.012 0.029 19.47 83722 86.2

83.4 0.93 0.012 0.029 18.67 74485 79.9

83.2 0.93 0.012 0.029 18.68 474504 509.1

83.4 0.93 0.012 0.029 18.68 474718 509.2

52.0 0.75 0.010 0.024 18.04 433423 481.6

466.1 0.63 0.096 0.080 7.33 34.21 20784 44.6

473.1 0.63 0.100 0.080 7.45 35.87 78528 166.0

476.6 0.62 0.101 0.079 7.50 36.78 120493 252.8

476.4 0.62 0.101 0.079 7.49 36.75 —

476.5 0.62 0.101 0.079 7.49 36.75 43 0.1

421.3 0.69 0.074 0.079 6.26 28.66 42734 101.4

476.5 0.62 0.101 0.079 7.49 36.75 12 0.0

430.5 0.68 0.07B 0.080 6.49 29.75 9249 21.5

431.1 0.68 0.079 0.080 6.50 29.80 58293 135.2

430.7 0.68 0.079 0.080 6.49 29.79 -

474.9 0.64 0.096 0.087 8.27 29.94 41296 87.0

-

-

-

—

~

Molecular W e i g h t

Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermai Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weighl Mass Flow (kg/h) Actual Volume Flow (m3/h) Waler Phase Mass Flow (kg/h)

479.5 0.62 0.103 0.079 7.49 37.98 46239 96.4

Slmulalion Basis: Train 3 • Selected Option . 514 • C3 Mono Rev. 5A

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— — — — — -

Page 2 of 10

-

FLUOR Contract AOWT Rev.2

QASCO Elhane Recoveiy Maximizalion

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 N8P138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperalure C O Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weighl Vapor Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Row (m3/h) Water Phase Mass Flow (kg/h)

se

57

58

70

72

73

75

76

77

i.i

0.5 S79.6 332.2 298.4 89.3 130.3 21.1 14.5 3.4 1.2 0.0 0.0 0.1 43.2 0.0 0.1 0.1 0.0 0.0

25 913.9 87.1 24.0 3.6 4.1 0.4 0.2 0.0 0.0 0.0 0.0 0.0 24.8 0.0 0.0 0.0 0.0 0.0

95.8 24294.4 2747.4 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

95.8 24294.3 2747.3 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

95.8 24294.3 2747.3 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

95.8 24294.3 2747.3 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

89.7 22735.7 2671.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0

435.7 7943 -43.9 39.7 l.OO -9.1 18.23

1514.0 50136 -43.9 39.7 0.00 -43.0 33.11

1060.7 19998 -29.7 39.7 1.00 •22.2 18.85

27949.2 510831 -56.6 39.5 1.00 -588.4 18.28

27949.0 510826 -46.0 39.1 1.00 -584.1 18.28

0.0 0 22.0 38.6 1.00 0.0 18.28

27949.0 510826 -11.9 38.8 1.00 •572.9 18.28

27949.0 510826 22.0 38.6 1.00 -562.9 18.28

26156.0 478055 22.0 38.4 1.00 -526.7 18.28

83.4 0.93 0.012 0.029 18.68

49.6 0.71 O.OtO 0.024 18.23 79« 8.7

49.6 0.71 0.010 0.024 18.23

46.1 0.65 0.011 0.025 18.82 19926 21.2

57.2 0.83 0.010 0.024 18.28 510829 560.1

49.8 0.71 0.010 0.024 18.28 510826 560.1

31.4 0.57 0.012 0.030 18.28

37.9 0.59 0.011 0.027 18.28 510826 560.1

31.4 0.57 0.012 0.030 18.28 510826 560.1

31.3 0.57 0.012 0.030 18.28 478055 524.2

430.7 0.68 0.079 0.080 6.49 29.79 58079 134.9

498.8 0.62 0.112 0.088 9.04 33.11

498.8 0.62 0.112 0.088 9.04 33.11 50136 100.5

521.1 0.69 0.127 0.087 9 64 37.88 72 0.1

415.8 0.75 0.065 0.085 6.40 24.79 2 0.0

50

52

53

64

2.0 1241.9 519.6 557.5 225.4 389.2 107.6 86.6 46.0 30.6 1.5 0.0 0.1 68.9 0.0 0.2 0.2 0.5 0.0

1.4 527.3 56.5 17.6 2.9 34 0.4 0.2 0.0 0.0 0.0 00 0.0 15.2 0.0 0.0 0.0 0.0 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 86.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

1.6 966.1 362.8 304.9 90.0 131.0 21.1 14.6 3.4 1.2 0.0 0.0 0.1 52.9 0.0 0.1 0.1 0.0 0.0

3277.6 120456 -11.9 60.7 0.00 -94.7 36.75

624.9 12055 -20.5 39.7 1.00 •13.1 19.29

2652.7 108401 -20.5 39.7 0.00 -81.6 40.86

1949.8 58079 -32.2 60.2 0.00 -52.1 29.79

73.3 0.76 0.012 0.029 19.47

44.7 0.62 0.011 0.026 19.29 12055 12.5

44.7 0.62 0.011 0.026 19.29

476.4 0.62 0.101 0.079 7.49 36.75 120456 252.8

531.5 0.59 0.134 0.086 9.78 40.86

531.5 0.59 0.134 0.086 9.78 40.86 108401 204.0

Slmulalion Basis: Train 3 • Salocted Option . 5% • C3 Mode Bev. 5A

386.5 30.6 6.4 0.7 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 9.6 0.0 0.0 0.0 0.0 0.0

Page 3 o l i o

o.o o.o o.o o.o o.o o.o

0.0

0.0 0.0 0.0

FLUOR Contract AOWT Rev. 2

GASCO Ethane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaplan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature C O Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume Row (m3*) Water Phase Masa Flow (kg/h)

78

79

80

81

89

90

91

92

93

94

95

96

103

89.7 22735.7 2571.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0 0.0 0.0 0.0 0.0

89.7 22735.7 2571.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0 0.0 0.0 0.0 0.0

89.7 22735.7 2571.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0 0.0 0.0 0.0 0.0

6.1 1558.5 176.2 9.0 0.2 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 42.8 0.0 0.0 0.0 0.0 0.0

1.1 1511.9 1380.5 714.6 939 97.8 6.8 3.9 0.4 0.1 0.0 0.0 0.3 144.6 0.0 0.1 0.0 0.0 0.0

1.1 1511.9 1380.5 714.6 93.9 97.8 6.8 3.9 0.4 0.1 0.0 0.0 0.3 144.6 0.0 0.1 0.0 0.0 0.0

0.1 205.5 1625.3 1010.4 105.3 106.3 7.1 4.0 0.4 0.1 0.0 0.0 0.3 41.6 0.0 0.1 0.0 0.0 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 66.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 86.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 86.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

0.5 579.6 332.2 298.4 89.3 130.3 21.1 14.5 3.4 1.2 0.0 0.0 0.1 43.2 0.0 0.1 0.1 0.0 0.0

0.5 579.6 332.2 298.4 89.3 130.3 21.1 14.5 3.4 12 0.0 0.0 0.1 43.2 0.0 0.1 0.1 0.0 0.0

0.0 146.1 933.3 1896.0 328.5 410.3 49.5 32.8 6.8 24 0.0 0.0 0.2 25.3 0.0 0.3 0.2 0.1 0.0

26156.0 478055 52.2 38.0 1.00 -518.5 18.28

26156.0 478055 64.4 43.4 1.00 -515.8 18.28

26156.0 478055 53.8 42.8 1.00 -518.6 18.28

1793.0 32771 22.0 38.4 1.00 -36.1 18.28

3956.0 115642 -42.5 39.6 0.00 -106.9 29.23

3956.0 115642 -53.9 25.2 0.17 -106.9 29.23

3106.5 111715 0.2 29.6 0.00 -83.9 35.96

2652.7 108401 -27.2 25.5 0.13 -81.6 40.86

2652.7 108401 16.0 24.8 0.34 -77.8 40.86

2652.7 108401 32.0 24.1 0.45 -76.0 40.86

1514.0 50136 -54.0 24.8 0.17 -43.0 33.11

1514.0 50136 -16.8 24.1 0.42 -41.2 33.11

3831.8 164887 33.2 23.8 0.00 -110.6 43.03

27.2 0.56 0.013 0.033 18.28 478055 524.2

29.9 0.57 0.013 0.035 18.28 478055 524.2

30.6 0.57 0.013 0.034 18.28 478055 524.2

31.3 0.57 0.012 0.030 18.28 32771 35.9

-

31.8 0.60 0.009 0.021 18.88 12847 13.6

-

28.1 0.55 0.010 0.023 19.57 6960 7.1

29.9 0.52 0.011 0.024 25.22 22986 18.3

31.1 0.52 0.011 0.024 28.25 33874 24.0

29.5 0.59 0.009 0.021 18.15 4667 5.2

28.6 0.53 0.010 0.023 21.83 13995 12.9

456.5 0.67 0.083 0.088 7.55 29 23 115642 253.3

506.5 0.62 0.113 0.097 9.96 31.38 102795 202.9

466.1 0.66 0.087 0.081 5.99 35.96 111715 239.7

565.9 0.57 0.168 0.091 11.77 44.16 101441 179.2

537.0 0.60 0.132 0.079 8.88 49.06 85415 159.1

527.0 0.61 0.120 0.074 7.93 51.27 74527 141.4

546.3 0.58 0.153 0.096 11.65 36.17 45469 83.2

534.7 0.59 0.135 0.089 9.99 41.40 36141 67.6

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—

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—

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Simulalioo Basis: Tram 3 - Salocted Option • 5% - C3 Mode Rev. 5A

—

Page 4 of 10

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468.7 0.67 0.085 0.070 5.24 43.03 164887 3S1.8

FLUOR Contract AOWT Rev.2

OASCO Elhane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP9I NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Meroaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Aclual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

104

109

110

111

112

113

115

116

117

118

119

120

121

0.0 146.1 933.3 1896.0 328.5 410.3 49.5 32.8 6.8 2.4 O.O 0.0 0.2 25.3 0.0 0.3 0.2 0.1 0.0

0.0 0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

1.1 1499.3 2339.6 561.0 24.4 17.7 0.5 0.2 0.0 0.0 0.0 0.0 0.5 138.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.0 2095.2 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

2.2 2606.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

3831.8 164887 44.9 23.8 0.17 -107.8 43.03

2689.3 142428 88.9 23.9 O.OO -83.1 52.96

4582.9 127791 2.5 23.7 1.00 -105.4 27.88

5433.5 131752 -19.3 23.3 1.00 -126.8 24.25

5433.7 131757 -11.0 22.9 1.00 -126.2 24.25

5433.7 131757 22.0 22.6 1.00 -123.9 24.25

5433.7 131757 86.9 52.5 1.00 -120.6 24.25

5433.6 131755 86.9 52.5 1.00 -120.6 24.25

0.0 1 86.9 52.5 1.00 0.0 24.25

5433.6 131755 49.8 51.9 1.00 -123.4 24.25

0.0 1 86.9 52.5 • 1.00 0.0 24.25

0.0 1 55.0 51.9 1.00 0.0 24.25

5433.7 131757 49.8 51.9 1.00 -123.4 24.25

36.2 0.55 0.010 0.021 27.88 127790 91.8

32.6 0.54 0.010 0.021 24.21 131139 108.5

30.2 0.52 0.010 0.021 24.25 131757 108.9

24.8 0.50 0.011 0.024 24.25 131757 108.9

47.6 0.57 0.014 0.034 24.25 131757 108.9

47.6 0.57 0.014 0.034 24.25 131755 108.9

47.6 0.57 0.014 0.034 24.25 1 0.0

56.3 0.59 0.013 0.030 24.25 131755 108.9

47.6 0.57 0.014 0.034 24.25 1 0.0

54.7 0.58 0.013 0.030 24.25 1 0.0

56.3 0.59 0.013 0.030 24.25 131757 108.9

468.2 0.67 0.088 0.080 6.04 36.63 1 0.0

484.5 0.64 0.098 0.089 7.62 34.35 613 1.3

43.1 0.58 0.011 0.022 36.38 23340 12.9 458.6 0.69 0.082 0.067 4.67 44.37 141547 308.6

SiTHjlation Basis: Train 3 • Selected Option • 5% - C3 Mode Rev. SA

440.9 0.75 0.076 0.055 2.99 52.96 142428 323.1

Page 5 of 10

o.o o.o o.o o.o o.o o.o

FLUOR Contraci AOWT Rev.2

QASCO Elhane Recovery Maximizalion

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composilion (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP13B NBP182 H2S C02 CS2 M-Mercaplan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Row (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std G a s Flow ( M M S C F D )

124

125

126

127

128

129

130

131

132

141

142

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0,0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.8 1032.9 771.2 97.7 4.8 3.4 0.1 0.0 0.0 0.0 0.0 0.0 0.2 88 9 0.0 0.0 0.0 0.0 0.0

0.8 1032.9 771 2 97.7 4.8 3.4 0.1 0.0 0.0 0.0 0.0 0.0 0.2 88.9 0.0 0.0 0.0 0.0 0.0

0.0 0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

0.0 0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

o.o

265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

0.0 0.0 121.5 1938.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.4 0.4 0.0 0.0

0.0 0.0 121.5 1938.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.4 0.4 0.0 0.0

5433.7 131757 27.5 51.5 1.00 -125.1 24.25

5433.7 131757 •6.0 51.2 0.86 -129.3 24.25

5433.7 131757 -21.9 51.0 0.51 •133.3 24.25

5433.7 131757 -30.6 50.7 0.32 -135.3 24.25

5433.7 131757 -55.7 50.5 O.OO -139.5 24.25

5433.7 131757 -56.8 39.5 0.02 -139.5 24.25

2000.0 48496 -21.9 51.0 0.51 -49.1 24.25

2000.0 48496 -47.6 50.7 0.00 -51.1 24.25

26B9.3 142428 75.8 18.0 0.16 -83.1 52.96

2689.3 142428 75.0 16.8 0.30 -82.0 52.96

2689.3 142428 74.2 16.5 0.31 -82.0 52.96

3649.2 182792 74.8 16.0 1.00 -98.5 50.09

3649.2 182792 59.8 22.5 0.00 -112.1 50.09

64.4 0.64 0.013 0.028 24.25 131757 108.9

82.9 0.86 0.012 0.027 23.50 110234 94.0

80.4 0.69 0.012 0.027 21.57 59344 55.1

79.3 092 0.012 0.027 20.57 35608 34.7

58.1 0.84 0.010 0.024 18.37 1805 2.0

80.4 0.89 0.012 0.027 21.57 21843 20.3

39.7 0.59 0.011 0.021 48.12 21163

37.0 0.58 0.010 0.021 48.66 39284 16.2

362 0.57 0.010 0.021 48.66 40228 16.6

36.4 0.56 0.010 0.021 50.09 182792 73.1

373.3 0.84 0.053 0.077 4.07 28.97 21523 57.7

376.7 0.84 0.053 0.081 4.78 26.99 72412 192.2

377.4 0.83 0.053 0.082 5.07 25.97 96148 254.8

409.8 0.77

376.7 0.84 0.053 0.081 4.78 26.99 26653 70.6

473.4 0.69 0.090 0.061 4.37 53.91 121265 256.2

480.8 0.68 0.094

482.6 0.68 0.094 0.062 4.78 54.87 102200 211.8

122 2.2 2806.1 2095.3

Hydrocarbon Uquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Aclual Volume Flow (m3/h) Waler Phase Mass Flow (kg/h)

Simulation Baale: Train 3 - Selectea Option + 5% • C3 Mode Rov. 5A

123

404.8 0.76 0.061 0.085 6.06 24.25 131757 . 325.5

Page 6ot10

0.062 0.085 6.23 24.36 129952 317.1

383.3 0.81 0.054 0.082 5.45 24.25 48496 126.5

0.062 4.69 54.81 103144 214.5

478.5 0.68 0.092 0.065 4.93 50.09 182792 382.0

FLUOft Contract AOWT Rev.2

GASCO Ethane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kgm) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h) Water Phase Mass Row (kg/h)

ISO

151

152

153

501

502

503

504

505

507

600

601

602

14.1 3467.1 347.2 130.8 25.5 32.6 4.1 2.7 0.6 0.2 0.0 0.0 0.1 90.1 0.0 0.0 0.0 0.0 0.0

14.1 3467.1 347.2 130.8 25.5 32.6 4.1 2.7 0.6 0.2 0.0 0.0 0.1 90.1 0.0 0.0 0.0 0.0 0.0

1.1 1511.9 1380.5 714.6 93.9 97.8 6.8 3.9 0.4 0.1 0.0 0.0 0.3 144.6 0.0 0.1 0.0 0.0 0.0

1.0 882.5 190.4 22.4 1.0 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 43.7 0.0 0.0 0.0 0.0 0.0

0.2 629.4 1190.1 692.2 92.9 97.1 6.6 3.9 0.4 0.1 0.0 0.0 0.2 100.9 0.0 0.1 0.0 0.0 0.0

0.2 629.4 1190.1 692.2 92.9 97.1 6.8 3.9 0.4 0.1 0.0 0.0 0.2 100.9 0.0 0.1 0.0 0.0 0.0

0.2 629.7 1190.3 692.4 93.0 97.2 6.8 3.9 0.4 0.1 0.0 0.0 0.2 100.9 0.0 0.1 0.0 0.0 0.0

43.9 11119.8 1294.4 6S3.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

1.3 1920.2 1899.6 241.7 12.0 8.6 0.2 0.1 0.0 0.0 0.0 0.0 0.4 197.5 0.0 0.0 0.0 0.0 0.0

4115.0 80131 •11.9 60.7 1.00 -86.3 19.47

4115.0 80131 -30.3 60.2 0.94 -87.8 19.47

3956.0 115642 -43.2 24.6 0.29 -105.4 29.23

1141.8 22923 -43.2 24.6 1.00 -25.4 20.08

2614.2 92719 -43.2 24.6 0.00 -80.0 32.95

2814.2 92719 -44.3 23.3 0.02 -80.0 32.95

2815.2 92752 -44.3 23.3 0.02 -80.0 32.95

14023.5 299000 •13.3 60.9 0.B9 •306.4 21.32

4281.7 108549 •14.0 23.3 1.00 -101.2 25.35

73.2 0.76 0.012 0.029 19.47 80120 82.5

82.1 0.90 0.012 0.029 18.76 72451 77.4

31.1 0.57 0.010 0.021 20.08 22923 22.9

31.1 0.57 0.010 0.021 20.08 22923 22.9

31.1 0.57 0.010 0.021 20.08

29.4 0.56 0.009 0.021 20.10 941 0.9

29.4 0.56 0.009 0.021 20.10 951 0.9

74.1 0.77 0.012 0.029 19.40 241227 249.2

33.8 0.54 0.010 0.021 25.35 108549 85.8

476.5 0.62 0.101 0.079 7.49 36.75 11 0.0

435.4 0.67

507.3 0.62

507.3 0.62

0.081 0.080 6.61 30.38 7680 17.6

0.112 0.096 9.68 32.95 92719 182.8

0.112 0.096 9.68 32.95

507.3 0.62 0.112 0.096 9.68 32.95 92719 182.8

511.6 0.62 0115 0.097 9.93 33.16 91778 179.4

511.6 0.62 0.115 0.097 9.93 33.17 91801 179.4

474.6 0.63 0.100 0.079 7.46 36.34 57773 121.7

478.8 0.65 0.092 0.087 7.09 34.61 0 0.0

0.0 0.0 80.7 1287.6 392.5 602.1 41.4 18.9 0.3 0.0 0.0 0.0 0.0 0.0 0.0 0.3 0.3 0.0 0.0

0.0 0.0 0.0 0.0 o.i 2.5 93.5 85.8 49.4 31.9 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.5 0.0

0.0 0.0 0.0 0.0 0.1 2.5 93.5 85.8 49.4 31.9 1.5 0.0

0.0 0.0 0.5 0.0

0.0 0.0 0.0 0.0 0.1 25 93.5 85.8 49.4 31.9 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.5 0.0

2424.1 121424 59.8 22.5 0.00 -74.5 50.09

265.2 21004 160.5 16.3 0.00 -10.1 79.20

265.2 21003 82.0 15.6 0.00 -11.2 79.20

2652 21003 49.0 15.4 0.00 •11.6 79.20

478.5 0.68 0.092 0.065 4.93 50.09 121424 253.8

Simulation Basis: Train 3 • Selected Option . 5% • C3 Mode Rev. 5A

470.1 0.75 0.084 0 049 3.21 79.20 21004 44.7

o.o o.o o.o

584.9 0.61 0.156 0.077 10.21 79.20 21003 35.9

620.4 0.57 0.205 0.086 13.53 79.20 21003 33.9

Page 7 of 10

FLUOR Contract AOWT Rev.2

GASCO Ethane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBPie2 H2S C02 CS2

504

605

606

607

0.1 205.5 1625.3 1010.4 105.3 106.3 7.1 4.0 0.4 0.1 0.0 0.0 0.3 41.6 0.0

0.0 0.0 121.5 1936.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0

0.1

0.4

0.0 0.0

o.o

0.4 0.0 0.0

0.0 0.0 121.5 1938.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.4 0.4 0.0 0.0

0.0 0.0 80.7 1287.6 392.5 602.1 41.4 18.9 0.3 0.0 0.0 0.0 0.0 0.0 0.0 0.3 0.3 0.0 0.0

3106.5 111715 0.2 27.0 0.00 -83.9 35.96

3649.2 182792 59.0 15.7 0.00 -112.2 50.09

3649.2 182792 59.0 15.5 0.00 -112.2 50.09

2424.1 121424 35.0 22.0 0.00 -76.4 50.09

466.1 0.66

476.3 0.68 0.093 0.066 5.00

476.3 0.68 0.093 0.066 5.00

50.09 182792 383.7

50.09 182792 383.7

518.9 0.62 0.116 0.075 7.51 50.09 121424 234.0

M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Row (kg/h)

0.087 0.081 5.99 35.96 111715 239.7

Simulation Bajii: Train 3 • Selactao Option - 5% • C3 Mode Rav. 5A

PageSol 10

FLUOR Contract AOWT Rev.2

GASCO Ettiane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE • REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Elhane Propane t-Bulane Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h)

200

201

202

203

204

205

206

207

208

210

213

220

701

148.7 7212.5 74.4

148.7 7212.5 74.4

148.7 7212.5 74.4

23.2 2687.5 42.9

23.2 2687.5 42.9

23.3 2685.4 44.6

23.3 2685.4 44.6

8.2 4174.2 196.8

8.2 4174.2 196.8

125.5 4524.9 31.4

125.5 4524.9 31.4

148.8 7210.4 76.0

42.1 2041.6 21.0

7435.5 326842 57.4 21.0 0.00 -205.9 43.96

7435.5 326842 49.2 20.3 0.00 -207.8 43.96

7435.5 326842 20.5 8.8 0.24 -207.8 43.96

2753.6 121704 21.1 8.8 0.00 -79.6 44.20

2753.6 121704 -9.2 3.6 0.20 -79.6 44.20

2753.3 121712 -8.2 3.6 1.00 -70.6 44.21

2753.3 121712 -8.5 3.5 1.00 -70.6 44.21

4379.1 195750 -8.2 3.6 0.00 -131.3 44.70

4379.1 195750 -7.6 3.6 0.50 -122.3 44.70

4681.9 205136 21.1 8.8 1.00 -117.8 43.82

4681.9 205138 20.5 8.5 1.00 -117.8 43.82

7435.2 326850 71.6 21.7 1.00 -182.7 43.96

2104,8 92519 54.5 19.8 0.00 -58.5 43.96

18.6 0.48 0.009 0.016 43.58 77530 35.7

16.7 0.48 O.OOS 0.016 43.82

7.8 0.41 0.007 0.013 43.88 24619 112

7.8 0.41 0.007 0.013 44.21 121712 55.2

7.6 0.40 0.007 0.013 44.21 121712 55.2

7.8 0.41 0.007 0.013 44.21

7.8 0.41 0.007 0.013 44.39 97201 43.9

18.7 0.48 0.009 0.016 43.82 205138 93.8

18.1 0.47 0.008 0.016 43.82 205138 93.8

45.2 0.61 0.011 0.022 43.96 326850 149.0

44.4 0.63 0.010 0.020

499.1 0.64 0.104 0.083 7.38 44.07 249312 499.5

498.9 0.64 0.104 0.083 7.35 44.20 121704 243.9

541.9 0.59 0.141 0.098 11.13 44.28 97085 179.2

542.6 0.59 0.142 0.098 11.10 44.70

542.6 0.59 0.142 0.098 11.10 44.70 195750 360.8

543.2 0.59 0.143 0.097 11.09 45.01 98549 181.4

498.9 0.64 0.104 0.083 7.35 44 20

47.7 0.66 0.010 0.021 43.56

432.3 0.77 0.072 0.065 3.28 43.96 326842 756.1

Slmulalion Baaia: Train 3 • SelectBd Option • 5% - C3 Moda Rev. 5A

450.9 0.72 0.078 0.069 4.12 43.96 326842 724.8

Page 9 otIO

43.56

438.4 0.75 0.074 0.066 3.57 43.96 92519 211.0

FLUOR Contract AOWT Rev. 2

GASCO Ethane Recovery Maximization

LOW CONDENSATE CASE • C2 REJECTION MODE • REFRIGERATION SYSTEMS

Stream Number Composition (kgmoia/h) Ethane Propane i-Butane Total Stream Molar Ftow (kgmole/h) Mass How (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h)

706

708

709

711

712

716

718

722

723

724

727

732

10.8 524.1 5.4

10.8 524.1 5.4

10.8 524.1 5.4

0.0 0.0 0.0

0.0 0.0 0.0

55.2 2679.5 27.6

21.4 1040.2 10.7

9.2 445.5 4.6

9.2 445.5 4.6

9.2 445.5 4.6

20.8 1011.1 10.4

76.1 3690.6 38.0

540.3 23751 18.1 19.2 0.00 -15.6 43.96

540.3 23750 14.5 7.6 0.03 -15.6 43.96

540.3 23750 16.0 7.6 1.00 -13.7 43.96

0.0 1 14.5 7.6 0.03 0.0 43.96

0.0 1 14.3 7.6 0.03 0.0 43.96

2762.4 121424 16.0 7.4 1.00 -69.8 43.96

1072.4 47140 18.1 19.2 0.00 -31.0 43.96

459.3 20190 -21.3 18,7 0.00 -13.7 43.96

459.3 20190 •25.0 2.2 0.03 •13.7 43.96

459.3 20190 -23.5 2.1 1.00 -11.8 43.96

1042.4 45821 -24.4 2.0 1.00 -26.8 43.96

3804.8 167245 76.3 20.3 1.00 -92.8 43.96

16.1 0.46 0.008 0.015

16.2 0.46 O.ooa 0.015 43.96 23750 10.8

16.1 0.46 0.008 0.015 4328 0 0.0

16.0 0.46 0.008 0.015 43.29 0 0.0

15.8 0.46 0.008 0.015 43.96 121424 55.'4

4.8 0.38 0.007 0.012 42.87 507 02

4.8 0.38 0.007 0.011 43.96 20190 9.2

4.6 0.38 0.007 0.011 43.96 45821 20.9

39.8 0.58 0.011 0.022 43.96 167245 76.3

507,4 0.63 0.110 0.086 8.06 43.98 1 0.0

507.7 0.63 0.110 0.086 8.08 43.98 1 0.0

469.6 0.63 0.105 0.086 8.00 44.35

43.28 6S9 0.3 505.8 0.63 0.107 O.OBS 7.62 43.96 23751 47.0

Simulation Basis: Train 3 - Selected Option + 5% - C3 Mode Rev. 5A

507.4 0.63 0.110 0.086 8.06 43.98 23090 45.5

Page 10 o l i o

505.8 0.63 0.107 0.085 7.62 43.96 47140 93.2

558.7 0.58 0.158 0.104 12.57 43.96 20190 36.1

560.3 0.58 0.163 0.106 13.07 43.99 19682 35.1

530.6 0.57 0.160 0.106 13.14 44.49

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Material Balance Max. Condensate Case - C2 Rejection Mode Rev.2

GASCO ProjectNo.: 13522102 Doc. No.: 44-00-20011

ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Material Balance Max. Condensate Case C2 Rejection Mode Revision 2

Rev.

Date

Description

13-Feb-04

Approved for Construction

4-Sep-03

Approved for Design

By

Chk.

Disc.

GS-L-FML046

'prsOPM

DTS

Approved Proj. GASCO

ED

FLUOR Contract AOWT Rev.2

GASCO Ethane Recovery Maximization

MAX. CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane 1-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weigh! Mass Flow (kg'h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) 0

10

11

20

22

23

24

104.6 24757.9 3193.1 1849.2 560.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 582.2 0.0 0.0 0.0 0.2 22.0

103 5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 12 0.0 0.6 582.2 0.0 0.0 0.0 0.2 0.0

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

1.1 557.9 226.0 286.4 147.4 269.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 00 0.0 89.1

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

43.6 10186.2 1248.9 657.8 182.5 279.1 57.7 44.3 19.4 11.1 0.5 0.0 0.2 245.0 0.0 0.0 0.0 0.1 0.0

43.6 10186.2 1246.9 657.8 182.5 279.1 57.7 44.3 19.4 11.1 0.5 0.0 0.2 245.0 0.0 0.0 0.0 0.1 0.0

59.9 14013.8 1718.2 905.0 251.0 363.9 79.4 61.0 26.8 15.2 0.7 0.0 0.3 337.1 0.0 0.0 0.0 0.1 0.0

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

32920.0 758433 58.0 66.5 1.00 -696.3 23.04

32920.0 758433 44.8 65.8 0.98 -704.4 23.04

32920.0 758433 27.0 6S.4 0.94 -716.3 23.04

30851.1 663517 27.0 65.3 1.00 -647.3 21.51

30829.1 663120 27.8 62.8 1.00 -645.1 21.51

1979.8 93309 27.0 65.3 0.00 -63.0 47.13

1979.8 93309 17.4 31.4 0.24 -63.0 47.13

89.1 1607 27.0 65.3 0.00 -6.1 18.02

1979.8 93309 49.2 30.7 0.37 -60.6 47.13

12976.5 279118 27.6 62.5 1.00 -271.5 21.51

12976.5 279118 -4.0 60.8 0.91 -279.4 21.51

17852.5 384000 27.6 62.5 1.00 -373.5 21.51

13900.8 299000 27.5 62.4 1.00 -290.9 21.51

66.2 0.63 0.014 0.034 23.04 758432 659.7

68.0 0.64 0.014 0.033 22.50 726421 647.0

70.5 0.67 0.014 0.032 21.51 663625 618.3

70.3 0.67 0.014 0.032 21.51 663517 618.3

66.7 0.65 0.013 0.032 21.51 663120 617.8

70.3 0.67 0.014 0.032 21.51

32.8 0.55 0.012 0.027 22.21 10542 9.5

70.3 0.67 0.014 0.032 21.51

35.5 0.54 0.013 0.028 27.01 19602 14.5

66.4 0.65 0.013 0.032 21.51 279118 260.0

71.4 0.73 0.013 0.030 19.90 235403 237.0

66.4 0.65 0.013 0.032 21.51 384000 357.8

66.3 0.65 0.013 0.032 21.51 299000 278.6

515.2 0.61 0.119 0.072 7.54 53.40 31069 60.3

499.6 0.61 0.112 0.073 7.32 47.11 93202 186.5

499.9 0.61 0.113 0.073 7.32 47.13

499.9 0.61

567.6 0.58 0.158 0.080 10.21 55.00 82763 145.8

499.9 0.61 0.113 0.073 7.32 47.13

543.3 0.61 0.131 0.073 8.32 58.77 73708 135.7

943

1606

Sftnulation Baeis: Train 3 - Mar Condensale + S% - C3 Mode Rev. 3A

0.113 0.073 7.32 47.13 93309 186.7

1607

Page 1 of 10

475.3 0.63 0.101 0.078 7.34 38.08 43715 92.0

FIUOR

GASCO Ethane Recovery Maximization

Contract AOWT Rev. 2

MAX. CONDENSATE CASE • C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature CC) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Denslly (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg*)

25

•

26

28

29

30

31

32

33

34

36

37

38

43

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

13.3 3102.0 380.3 200.3 55.6 85.0 1 7.6 1 3.5 5.9 3.4 0.1 0.0 0.1 74.6 0.0 0.0 0.0 0.0 0.0

13.3 3102.0 380.3 200.3 55.6 85.0 17.6 13.5 5.9 3.4 0.1 0.0 0.1 74.6 0.0 0.0 0.0 0.0 0.0

59.9 14013.8 1718.2 905.0 251.0 383.9 79.4 61.0 26.8 15.2 0.7 0.0 0.3 337.1 0.0 0.0 0.0 0.1 0.0

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 562.2 0.0 0.0 0.0 0,2 0.0

101.1 22822.1 2376.8 919.4 177.7 225.4 26.3 17.2 3.3 1.0 0.0 0.0 0.5 516.6 0.0 0.0 0.0 0.0 0.0

69.8 15749.9 1640.3 634.5 122.6 155.5 18.1 11.9 2.3 0.7 0.0 0.0 0.3 356.5 0.0 0.0 0.0 0.0 0.0

69.8 15749.9 1640.3 634.5 122.6 155.5 18.1 11.9 2.3 0.7 0.0 0.0 0.3 356.5 0.0 0.0 0.0 0.0 0.0

16.0 3609.6 375.9 145.4 28.1 35.6 4.2 2.7 0.5 0.2 0.0 0.0 0.1 81.7 0.0 0.0 0.0 0.0 0.0

16.0 3609.6 375.9 145.4 28.1 35.6 4.2 2.7 0.5 0.2 0.0 0.0 0.1 81.7 0.0 0.0 0.0 0.0 0.0

101.1 22822.1 2376.8 919.4 177.7 225.4 26.3 17.2 3.3 1.0 0.0 0.0 0.5 516.6 0.0 0.0 0.0 0.0 0.0

99.3 21869.1 2006.0 599.6 84.2 89.8 6.1 3.4 0.3 0.0 0.0 0.0 0.4 471.5 0.0 0.0 o.o 0.0 0.0

99.3 21869.1 2006.0 599.6 84.2 89.8 6.1 3.4 0.3 0.0 0.0 0.0 0.4 471.5 0.0 0.0 o.o 0.0 0.0

13900.8 299000 -5.7 61.3 0.90 -299.8 21.51

3951.7 85000 27.5 62.4 1.00 -82.7 21.51

3951.7 85000 -21.8 60.9 0.83 -86.6 21.51

17852.5 384000 -15.9 60.8 0.86 -389.0 21.51

30829.1 663120 -11.0 60.7 0.88 -668.4 21.51

27187.4 630687 -11.0 60.7 1.00 -564.5 19.52

18762.4 366234 -11.0 60.7 1.00 -389.6 19.52

18762.4 366234 -31.0 60.2 0.93 -397.2 19.52

4300.0 83934 -11.0 60.7 1.00 -89.3 19.52

4300.0 83934 -30.9 60.2 0.93 -91.0 19.52

27187.4 530687 -30.7 60.2 0.93 -575.4 19.52

25229.7 471978 -30.7 60.2 1.00 -523.5 18.71

25229.7 471978 -49.0 39.6 0.95 -526.3 18.71

72.6 0.74 0.013 0.030 19.81 248878 251.8

66.3 0.65 0.013 0.032 21.51 85000 79.2

77.4 0.82 0.012 0.029 18.96 61915 65.4

75.0 0.78 0.012 0.029 19.26 295152 307.1

73.2 0.76 0.012 0.029 19.52 530652 544.8

73.3 0.76 0.012 0.029 19.52 530667 544.8

73.2 0.76 0.012 0.029 19.52 366178 376.0

82.4 0.92 0,012 0.029 18.69 324858 348.3

73.2 0.76 0.012 0.029 19.52 83922 86.2

82.3 0.92 0.012 0.029 18.70 74495 79.9

82.1 0.91 0.012 0.029 18.70 471765 505.5

82.4 0.91 0.012 0.029 18.71 471978 505.6

51.3 0.74 0.010 0.024 18.05 430893 478.4

472.7 0.63 0.099 0.078 7.29 37.53 50122 106.0

•— ----

459.7 0.64 0.093 0.080 7.17 33.65 23085 50.2

455.9 0.63 0.096 0.079 7.27 35.14 88848 190.7

470.4 0.63 0.098 0.079 7.33 36.37 132468 281.6

470.3 0.63 0.098 0.079 7.32 36.37 -

470.3 0.63 0.098 0.079 7.33 36.36 58 0.1

429.6 0.68 0.078 0.080 6.47 29.92 41376 96.3

470.3 0.63 0.098 0.079 7.33 36.36 13 0.0

429.8 0.68 0.079 O.OBO 6.4B 29.94 9439 22.0

430.4 0.68 0.079 0.080 6.49 30.00 58922 136.9

430.0 0.68 0 079 0.080 6.48 29.99 -

475.5 0.64 0.097 0.087 6.31 30.31 41084 86.4

SimuiaUm Basis: Train 3 - Max Condensale * 5% - C3 Mode Rev. 5A

Page 2 0110

FLUOR

GASCO Ethane Recovery Maximization

Contract AOWT Rev.2

MAX. CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Uquld Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) 0

50

52

53

54

56

57

58

70

72

73

75

76

77

2.4 1377.9 590.2 643.4 255.8 437.6 110.9 88.1 42.9 25.3 1.2 0.0 0.1 65.6 0.0 o.o 0.0 0.2 0.0

1.7 587.4 65.4 20.9 3.4 4.0 0.4 0.2 0.0 0.0 0.0 0.0 0.0 14.7 0.0 0.0 0.0 0.0 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 87.9 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

1.7 953.1 370.9 319.9 93.5 135.5 20.2 13.8 3.0 1.0 0.0 0.0 0.1 45.0 0.0 0.0 0.0 0.0 0.0

1.2 363.7 32.0 7.0 0.8 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 8.4 0.0 0.0 0.0 0.0 0.0

0.5 569.4 338.8 312.8 92.8 134.8 20.2 13.8 3.0 1.0

103.5 24200.1 2880.1 157.6 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

103.5 24200.0 2880.1 157.7 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

103.5 24200.0 2880.1 157.7 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

103.5 24200.0 2880.1 157.7 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

96.9 22646.3 2695.2

o.i 36.7 0.0 0.0 0.0 0.0 0.0

2.9 971.1 97.4 27.9 4.2 4.7 0.4 0.3 0.0 0.0 0.0 0.0 0.0 23.1 0.0 0.0 0.0 0.0 0.0

3641.7 132433 •11.0 60.7 0.00 •103.8 36.37

698.3 13489 •19.7 39.7 1.00 -14.5 19.32

2940.4 118944 -19.7 39.7 0.00 -89.3 40.41

1957.7 58710 -30.7 60.2 0.00 -51.8 29.99

433.9 7922 -422 39.7 1.00 -8.9 18.26

1523.8 50788 -42.2 39.7 0.00 -42.9 33.33

1132.2 21411 -27.9 39.7 1.00 -23.4 18.91

27928.1 510575 -55.3 39.5 1.00 -581.4 1828

27928.1 510578 -41.5 39.1 1.00 -576.0 18.28

0.0 0 22.6 38.6 1.00 0.0 18.26

27928.1 510578 -9.2 38.8 1.00 -565.6 18.28

27928.1 510578 22.6 38.6 1.00 -556.1 18.28

26135.1 477799 22.6 38.4 1.00 -520.4 18.28

73.3 0.76 0.012 0.029 19.52

44.6 0.62 0.011 0.026 19.32 13489 14.0

44.6 0.62 0.011 0.026 19.32

82.4 0.91 0.012 0.029 18.71

49.0 0.70 0.010 0.024 18.26 7922 8.7

49.0 0.70 0.010 0.024 18.26

45.8 0.65 0.011 0.025 18.88 21337 22.7

56.6 0.82 0.010 0.024 18.28 510573 559.7

47.8 0.69 0.010 0.024 18.28 510578 559.7

31.4 0.57 0.012 0.030 18.28

37.3 0.59 0.011 0.027 18.28 510578 559.7

31.4 0.57 0.012 0.030 18.28 510578 559.7

31.2 0.57 0.012 0.030 18.28 477799 523.7

470.3 0.63

525.9 0.59 0.130 0.085 9.59 40.41

525.9 0.59 0.130 0.085 9.59 40.41 118944

430.0 0.68 0.079 0.080 6.48 29.99 58710 136.5

497.4 0.62

497.4 0.62 0.111 0.087 9.00 33.33 50788 102.1

5178 0.60 0.125 0.086 9.51 37.92 74 0.1

416.2 0.74 0.066 0.086 6.43 25.00 2 0.0

0.098 0.079 7.32 36.37 132433 281.6

Simulation Basis: Train 3 • Max Condensate t 5% - C3 Mode Rev. 5A

226.2

0.111 0.087 9.00 33.33

PageSol 10

o.o 0.0

147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

FLUOR Contract AOWT Rev.2

OASCO Ethane Recovery Maximization

MAX. CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Penlane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Tolal Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kgm)

78

79

80

81

96.9 22646.3 26952 147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

96.9 22646.3 2695.2 147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

96.9 22646.3 2695.2 147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

6.6 1553.7 184.9 10.1 0.2 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 37.4 0.0 0.0 0.0 0.0 0.0

26135.1 477799 52.4 38.0 1.00 •512.3 18.28

26135.1 477799 64.7 43.5 1.00 •509.5 18.28

26135.1 477799 54.0 42.8 1.00 -512.4 18.28

1793.0 32779 22.6 38.4 1.00 -35.7 18.28

27.2 0.57 0.013 0.033 18.28 477799 523.7

29.9 0.58 0.013 0.035 18.28 477799 523.7

30.7 0.57 0.013 0.034 18.28 477799 523.7

31.2 0.57 0.012 0.030 18.28 32779 35.9

Simulation Basis: Tram 3 • Max Condensale • 5% • C3 Mode Rev. 5A

90

91

92

93

94

95

96

103

1.3 1520.9 1439.3 775.7 100.2 103.8 6.7 3.8 0.3 0.1 0.0 0.0 0.3 124.2 0.0 0.0 0.0 0.0 0.0

1.3 1520.9 1439.3 775.7 100.2 103.8 8.7 3.8 0.3 0.1 0.0 0.0 0.3 124.2 0.0 0.0 0.0 0.0

0.1 208.4 1557.1 1159.9 114.4 114.2 7.0 3.9 0.3 0.1 0.0 0.0 0.3 35.3 0.0 0.0 0.0 0.0 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 879 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 87.9 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 87.9 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

0.5 569.4 338.8 312.8 92.8 134.8 20.2 13.8 3.0 1.0 0.0 0.0 0.1 36.7 0.0 0.0 0.0 0.0 0.0

0.5 569.4 338.8 312.8 92.8 134.8 20.2 13.8 3.0 1.0 0.0 0.0 0.1 36.7 0.0 0.0 0.0 0.0 0.0

0.1 157.4 919.6 2020.0 349.1 433.7 48.2 31.6 6.0 1.9 0.0 0.0 0.2 22.9 0,0 0.0 0.0 0.0 0.0

4076.3 120037 -40.9 39.6 0.00 -108.6 29.45

4076.3 120037 -52.2 25.2 0.17 •108.6 29.45

3201.0 116987 2.7 29.6 0.00 •86.6 36.55

2943.4 118944 •26.4 25.5 0.13 -89.3 40.41

2943.4 118944 14.0 24.8 0.33 -85.4 40.41

2943.4 118944 30.0 24.1 0.44 -83.4 40.41

1523.8 50788 •52.1 24.8 0.17 -42.9 33.33

1523.8 50788 •15.8 24.1 0.41 •41.2 33.33

3990.7 172250 33.9 23.8 0.00 •115.1 43.16

28.0 0 55 0.010 0.023 19.59 7747 7.9

29.8 0.52 0.011 0.024 24.94 24462 19.7

31.1 0.52 0.011 0.024 27.98 36473 26.1

29.2 0.59 0.009 0.021 18.19 4652 5.1

28.5 0.53 0.010 0.023 21.84 13645 12.5

560.6 0.57 0.163 0.091 11.56 43.64 111197 198.3

533.6 0.60 0.130 0.079 8.B4 48.14 94481 177.1

523.4 0.61 0.120 0,074 7.86 50.29 82471 157.6

544.1 0.58 0.152 0.096 11.57 36.38 46135 84.8

531.8 0.59 0.133 0.088 9.86 41.32 37142 69.8

o.o

31.5 0.60 0.009 0.021 18.91 13137 13.9 455.4 0.67 0.083 0.088 7.51 29.45 120037 263.6

Page 4 ol 10

504.6 0.62 0.113 0.097 9.88 31.61 106899 211.8

466.6 0.66 0.087 0.080 5.97 38.55 116987 250.7

468.2 0.67 0.085 0.070 5.25 43.16 172250 367.9

FLUOR Contract AOWT Rev.2

GASCO Elhana Recovery Maximization

MAX. CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentana n-Hexane NBP91 NBP138 NBP1B2 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Row (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heal Capadty (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) n

104

109

110

0.1 157.4 919.6 2020.0 349.1 433.7 46.2 31.6 6.0 1.9 0.0 0.0 0.2

0.0 0.0 87.0 1405.3 430.6 661.7 137.2 105.3 46.2 26.3 1.2 0.0 0.0 0.0

1.3 1567.9 2333.5 689.7 28.9 20,9 0.5 0.2 0.0 0.0 0.0 0.0 0.5 122.8 0.0 0.0 0.0 0.0 0.0

22.9 0.0 0.0 0.0 0.0 0.0 3990.7 172250 46.0 23.8 0.17 •112.1 43.16

o.o 0.0 0.0 0.2 0.0 2901.0 152546 88.1 23.9 0.00 •89.3 52.58

43.2 0.58 0.011 0.022 36.60 24931 13.7 457.5 0.70 0.082 0.067 4.63 44.51 147319 322.0

Simulallon Basis: rrain 3 - Max Condensate -* 5% - C3 Mode Rev. 3A

439.3 0.75 0.076 0.055 2.95 52.58 152546 347.3

111 2.5 2880.7 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 O.O 0.4 211.7 0.0 0.0 0.0 0.0 0.0

112

113

115

116

117

118

119

120

121

2.5 2680.8 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

2.5 2880.8 2216.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

2.5 2880.7 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0

2.5 2880.7 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 00 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0

0.0

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 O.O 0.0

0.0 0.0 0.0 0.0 0.0

o.o 0.0

o.o o.o 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

4766.2 134139 5.3 23.7 1.00 •108.4 28.14

5642.5 137221 •17.5 23.3 1.00 -129.0 24.32

5642.6 137223 -11.0 22.9 1.00 •128.4 24.32

5642.6 137223 21.0 22.6 1.00 -126.1 24.32

5642.6 137223 85.4 52.5 1.00 -122.7 24.32

5642.5 137221 85.4 52.5 1.00 -122.7 24.32

0.0 1 85.4 52.5 1.00 0.0 24.32

5642.5 137221 47.7 51.9 1.00 -125.7 24.32

36.1 0.54 0.010 0.021 28.14 134139 95.5

32.5 0.54 0.010 0.021 24.29 136608 112.7

30.5 0.52 0.010 0.021 24.32 137223 113.1

25.1 0.50 0,011 0.024 24.32 137223 113.1

48.2 0.58 0.014 0.033 24.32 137223 113.1

48.2 0.58 0.014 0.033 24.32 137221 113.1

48.2 0.58 0.014 0.033 24.32 1

57.5 0.60 0.013 0.030 24.32 137221 113.1

468.6 0.67 0.088 0.080 6.01 37.27 0 0.0

482.8 0.65 0.095 0.089 7.51 34.58 613 1.3

Page 5 o f l 0

0.0

o.o 0.0 0.0 0.0 0.0 0.0

o.o 0.0 0.0 0.0 0.0 0.0

o.o o.o i 85.4 52.5 1.00 0.0 24.32 48.2 0.58 0.014 0.033 24.32 1 0.0

0.0 0.0

o.o o.o o.o o.o 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 1 55.0 51.9 1.00 0.0 24.32 55.1 0.59 0.013 0.030 24.32 1 0.0

5642.6 137223 47.7 51.9 1.00 -125.7 24.32 57.5 0.60 0.013 0.030 24.32 137223 113.1

FLUOR Contract AOWT Rev.2

GASCO Ethane Recovery Maximization

MAX. CONDENSATE CASE • C2 REJECTION MODE

StreamNumber Composition (kgmole/h) Nitrogen Methane Ethane propane I-Butane n-Butane i-Pentane

122

123

124

125

126

127

128

129

130

131

132

141

142

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

0.8 867.9 667.6 92.1 4.4 3.2 0.1

0.8 867.9 667.6 92.1 4.4 3.2 0.1

0.0 0.0 87.0 1405.3 430.6 661.7 137.2

0.0 0.0 87.0 1405.3 430.6 661.7 137.2

0.0 0.0 87.0 1405.3 430.6 661.7 1372

0.0 0.0 126.9 2048.8 627.6 961.2 65.7

0.0 0.0 126.9 2048.8 627.6 961.2 65.7

0.1

0.1

0.1

0.1

0.1

0.1

0.0

0.0

105.3

105.3

105.3

30.2

30.2

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.1 63.8 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.1 63.8 O.O 0.0 0.0 0.0 0.0

46.2 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

46.2 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

46.2 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

5642.6 137223 24.5 51.5 1.00 -127.6 24.32

5642.6 137223 -4,0 51.2 0.87 -131.5 24.32

5642.6 137223 -17.0 51.0 0.58 -134.9 24.32

5642.6 137223 -25.3 50.7 0.41 -136.9 24.32

5642.6 137223 -54.4 50.5 0.00 -142.3 24.32

5842.6 137223 -55.9 39.5 0.02 -142.3 24.32

1700.0 41342 -17.0 51.0 0.58 -40.6 24.32

1700.0 41342 -47.3 50.7 0.00 -42.6 24.32

2901.0 152546 75.0 18.0 0.16 -89.3 52.58

2901.0 152546 73.8 16.8 0.29 -88.3 52.58

2901.0 152546 73.1 16.5 0.30 -88.3 52.58

3861.2 193488 74.9 16.0 1.00 -104.2 50.11

3861.2 193488 59.9 22.5 0.00 -118.7 50.11

66.7 0.65 0.013 0.028 24.32 137223 113.1

82.4 0.85 0.012 0.027 23.58 115349 98.1

80.1 0.87 0.012 0.027 21.98 71818 65.5

78.6 0.89 0.012 0.027 21.01 48026 45.8

57.4 0.83 0.010 0.024 18.35 2577 2.8

80.1 0.87 0.012 0.027 21.98 21637 19.7

39.8 0.59 0.011 0.021 48.04 22767 9.5

37.0 0.58 0.010 0.021 48.50 40576 16.8

36.3 0.57 0.010 0.021 48.50 41599 17.2

36.4 0.58 0.010 0.021 50.11 193488 77.4

— -

371.0 0.85 0.053 0.076 3.96 29.17 21874

374.3 0.64 0.053 0.080 4.56 27.53 65405

376.4 0.83 0.053 0.081 4.90 26.58 89197

402.3 0.76 0.061 0.084 5.39 24.32 137223

409.2 0.76 0.062 0.085 6.22 24.47 134646

374.3 0.84 0.053 0.080 4.56 27.53 1970S

383.8 0.80 0.055 0.083 5.46 24.32 41342

471.7 0.69 0.089 0.061 4.34 53.47 129779

478.9 0.68 0.093 0.062 4.65 54.24 111970

480.6 0.68 0.094 0.062 4.74 54.30 110947

— -

478.4 0.68 0.092 0.065 4.92 50.11 193488

—

59.0

174.8

237.0

34t.1

329.0

52.7

107.7

275.1

233.8

230.8

—

404.5

n-Pentane

n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature C O Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Sld Gas Flow (MMSCFD) Hydrocartxm Uquld Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual V o l u m e ROW (m3m)

— -

Water Phase Mass Flow (kgm)

Simulalioo Basla: Train 3 - Max Conflonsala + 5% • C3 Moda Rev. 5A

Page6ot 10

— — — — -

FLUOR Contract AOWT Rev.2

GASCO Ethane Recovery Maximization

MAX. CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane l-Butane n-Butane i-Peraane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

150

151

152

153

501

502

503

504

505

507

600

601

602

0.0 0.0 87.0 1405.3 430.5 659.3 45.1 20.7 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0 0.0

0.0 0.0 0.0 0.0 0.1 2.4 92.1 84.5 45.8 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

0.0 0.0 0.0 0.1 2.4 92.1 84.5 45.8 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

15.3 3454.3 359.8 139.2 26.9 34.1 4.0 2.6 0.5 0.2 0.0 0.0 0.1 78.2 0.0 0.0 0.0 0.0 0.0

15.3 3454.3 359.8 139.2 26.9 34.1 4.0 2.6 0.5 0.2 0.0 0.0 0.1 78.2 0.0 0.0 0.0 0.0 0.0

1.3 1520.9 1439.3 775.7 100.2 103.8 6.7 3.8 0.3 0.1 0.0 0.0 0.3 124.2 0.0 0.0 0.0 0.0 0.0

1.1 881.4 198.9 24.7 1.1 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 37.7 0.0 0.0 0.0 0.0 0.0

0.2 639.5 1240.4 750.9 99.1 103.0 6.7 3.8 0.3 0.1 0.0 0.0 0.2 86.5 0.0 0.0 0.0 0.0 0.0

0.2 639.5 1240.4 750.9 99.1 103.0 6.7 3.8 0.3 0.1 0.0 0.0 0.2 86.5 0.0 0.0 0.0 0.0 0.0

0.2 639.9 1240.6 751.1 99.2 103.1 6.7 3.8 0.3 0.1 0.0 0.0 0.2 86.5 0.0 0.0 0.0 0.0 0.0

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

1.4 1999.3 2017.0 280.9 13.6 9.8 0.2 0.1 0.0 0.0 0.0 0.0 0.4 174.1 0.0

252.7 19833 80.3 15.6 0.00 -10.6 78.50

252.7 19833 49.0 15.4 0.00 •11.0 78.50

4115.0 80323 -11.0 60.7 l.OO -85.5 19.52

4115.0 80323 -29.2 60.2 0.94 -87.0 19.52

4076.3 120037 •41.7 24.6 0.28 -107.1 29.45

1145.6 23005 -41.7 24.6 1.00 -25.0 20.08

2930.8 97031 -41.7 24.6 0.00 -62.2 33.11

2930.8 97031 -42.8 23.3 0.02 -62.2 33.11

2931.8 97065 -42.8 23.3 0.02 -82.2 33.11

13900.8 299000 -14.1 60.9 0.87 -302.3 21.51

4497.0 114216 -12.5 23.3 1.00 -104.0 25.40

73.2 0.76 0.012 0.029 19.52 80311 82.5

81.4 0.90 0.012 0.029 18.77 72273 77.2

30.8 0.57 0.010 0.021 20.08 23005 23.0

30.8 0.57 0.010 0.021 20.08 23005 23.0

30.8 0.57 0.010 0.021 20.08

29.1 0.56 0.009 0.021 20.11 972 1.0

29.1 0.56 0.009 0.021 20.11 981 1.0

74.5 0.78 0.012 0.029 19.35 233213 241.5

33.6 0.54 0.010 0.021 25.40 114216 90.1

470.3 0.63 0.098 0.079 7.33 36.36 12 0.0

433.4 0.67 0.080 0.060 6.56 30.44 8050 18.6

504.9 0.62 0.111 0.096 9.57 33.11 97031 192.2

504.9 0.62 0.111 0.096 9.57 33.11

504.9 0.62 0.111 0.096 9.57 33.11 97031 192.2

509.1 0.62 0,114 0.097 9.82 33.33 96060 188.7

509.1 0.62 0.114 0.097 9.82 33.33 96083 188.7

467.2 0.63 0,097 0.079 7.28 35.55 65787 140.8

477.3 0.65 0.092 0.086 7.00 34.83 0 0.0

2648.3 132710 59.9 22.5 0.00 -81.4 50.11

478.4 0.68 0.092 0.065 4.92 50.11 132710 277.4

Simulation Basis: Train 3 • Max Contonsato + 5% • C3 Mode Rev. 5A

o.o 0.0 0.1 2.4 92.1 84.6 45.8 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0 252.7 19836 159.2 16.3 0.00 -9.6 78.50

468.8 0.75 0.083 0.049 3.19 78.50 19836 42.3

584.2 0.61 0.156 0.077 10.25 78.50 19833 34.0

o.o

618.0 0.58 0.202 0.085 13.40 78.50 19833 32.1

Page7ol 10

o.o 0.0 0.0 0.0

FLUOR Contract AOWT Rev.2

GASCO Ethane Recoveiy Maximization

MAX. CONDENSATE CASE • C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S

C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Row (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

604

605

606

607

0.1 208.4 1557.1 1159.9 114.4 114.2 7.0 3.9 0.3 0.1 0.0 0.0 0.3 35.3 0.0 0.0 0.0 0.0 0.0

0.0 0.0 126.9 2048.8 627 6 961.2 65.7 30.2 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

0.0 0.0 126.9 2048.8 627.6 961.2 65.7 30.2 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

0.0 0.0 87.0 1405.3 430.5 659.3 45.1 20.7 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

3201.0 116987 2.7 27.0 0.00 -86.6 36.55

3861.2 193488 59.1 15.7 0.00 -118.7 50.11

3861.2 193488 59.1 15.5 0.00 -118.7 50.11

2648 3 132710 35.0 22.0 0.00 -83.5 50.11

466.7 0.66 0.087 0.080 5.97 36.55 116987 250.7

476.2 0.68 0.093 0.066 4.99 50.11 193488 406.3

476.2 0.68 0.093 0.066 4.99 50.11 193488 406.3

518.9 0.62 0.116 0.075 7.51 50.11 132710 255.7

Stmulalron Basis: Train 3 - Max Condansata + 5% • C3 Moda Rav. 5A

PageSol 10

FLUOR Conirad AOWT Rev.2

GASCO Elhane Recovery Maximization

MAX. CONDENSATE CASE - C2 REJECTION MODE - REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Elhane Propane I-Butane Total Stream Molar Row (kgmole/h) Mass Flow (kg/h) Temperature f C ) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume Flow (m3/h)

200

201

202

203

204

205

206

207

208

210

213

220

701

157.8 7652.4 78.9

157.8 7652.4 78.9

157.8 7652.4 78.9

22.5 2677.4 43.7

22.5 2677.4 43.7

22.5 2677.4 43.7

22.5 2677.4 43.7

7.8 4162.0 194.5

7.8 4162.0 194.5

135.3 4975.0 35.2

135.3 4975.0 35.2

157.8 7652.4 78.9

49.1 2383.7 24.6

7889.1 346778 57.4 21.0 0.00 -218.4 43.96

7889.1 346778 48.4 20.3 0.00 -220.7 43.96

7889.1 346778 19.6 8.6 0.24 -220.7 43.96

2743.6 121282 20.3 8.6 0.00 -79.4 44.21

2743.6 121282 -10.2 3.5 0.20 -79.4 44.21

2743.6 121281 -9.3 3.5 1.00 -70.4 44.21

2743.6 121281 -9.5 3.4 1.00 -70.4 44.21

4364.3 195070 -9.3 3.5 0.00 -131.0 44.70

4364.3 195070 -8.7 3.5 0.50 -122.0 44.70

5145.5 225496 20.3 8.6 1.00 -129.5 43.82

5145.5 225496 19.8 8.4 1.00 -129.5 43.62

7889.0 346777 71.6 21.7 1.00 •193.8 43.96

2457.4 108021 54.5 19.8 0.00 -68.3 43.96

18.2 0.47 0.008 0.016 43.58 81605 37.5

18.3 0.47 0.008 0.016 43.82

7.5 0.40 0.007 0.013 43.89 24519 11.2

7.6 0.40 0.007 0.013 44.21 121281 55.0

7.3 0.40 0.007 0.0)3 44.21 121281 55.0

7.6 0.40 0.007

7.6 0.40 0.007 0.013 44.39 96866 43.7

18.3 0.47 0.008 0.016 43.82 225496 103.1

17,8 0.47 0.008 0.016 43.82 225496 103.1

45.2 0.61 0.011 0.022 43.96 346777 158.1

44.4 0.63 0.010 0.020 43.56

500.4 0.64 0.105 0.084 7.49 44.07 265173 529.9

500.2 0.64 0.105 0.084 7.46 44.21 121262 242.4

543.2 0.59 0.142 0.099 11.26 44.29 96763 178.1

543.9 0.59 0.143 0.098 11.23 44.70

544.6 0.59 0.145 0.097 11.22 45.00 98205 180.3

500.2 0.64 0.105 0.084 7.46 44.21

47.7 0.66 O.OIO 0.021 43.58

432.3 0.77 0.072 0.065 3.28 43.96 346778 802.2

Simulabixi Basis: Train 3 • Max Condensata * 5% - C3 Mode Rav. 5A

452.8 0.72 0.079 0.069 4.21 43.96 346778 765.8

Page 9 ol 10

0.013 44.21

543.9 0.59 0.143 0.098 11.23 44.70 195070 358.6

436.4 0.75 0.074 0.066 3.57 43.96 108021 246.4

FLUOR Contract AOWT Rev.2

GASCO Elhane Recovery Maximization

MAX. CONDENSATE CASE - C2 REJECTION MODE - REFRIGERATION SYSTEMS

Stream Number Composilion (kgmole/h) Ethane Propane i-Butane Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperalure (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h)

706

708

709

711

712

716

718

722

723

724

727

732

11.9

576.0 5.9

11.9 575.0 5.9

11.9 575.0 5.9

0.0 1.0 0.0

0.0 1.0 0.0

56.2 2725.5 28.1

22.5 1088.9 11.2

12.0 580.3 6.0

12.0 580.3 6.0

12.0 580.3 6.0

20.0 967.7 10.0

76.1 3693.2 38.1

593.8 26102 18.1 19.2 0.00 -17.1 43.96

5928 26058 14.5 7.6 0.03 •17.1 43.96

592.8 26058 16.0 7.6 I. 00 -15.0 43.96

1.0 44 14.5 7.6 0.03 0.0 43.96

1.0 44 14.3 7.6 0.03 0.0 43.96

2809.6 123511 17.4 7.4 1.00 -70.9 43.96

1122.6 49346 18.1 19.2 0.00 -32.4 43.96

598.2 26295 •21.3 18.7 0.00 -17.9 43.96

598.2 26295 -25.0 2.2 0.03 -17.9 43.96

598.2 26295 •23.5 2.1 1.00 •15.4 43.96

997.6 43852 •21.0 2.0 1.00 -25.6 43.96

3807.4 167362 77.9 20.3 1.00 -92.7 43.96

16.1 0.46 0.008 0.015 43.28 724 0.3

16.2 0.46

16.1 0.46 0.006 0.015 43.28 1 0.0

16.0 0.46 0.008 0.015 43.29 1 0.0

15.7 0.46 0.008 0.015 43.96 123511 56.3

4.8 0.38 0.007 0.012 42.87 661 0.3

4.8 0.38 0.007 0.011 43.96 26295 12.0

4.5 0.38 0.OO7 0.012

39.4 0.58 0.011 0.022 43.96 167362 76.3

507.4 0.63 0.110 0.086 8.06 43.98 43 0.1

507.7 0.63 0.110 0.086 8.08 43.98 43 0.1

467.1 0.63 0.103 0.085 7.84 44.35

505.8 0.63 0.107 0.085 7.62 43.96 26102 51.6

Simulallon Basis: Train 3 • Max Condensale • 5% - C3 Mode Rev. SA

507.4 0.63 0.110 0.086 8.06 43.98 25334 49.9

0.008

0.015 43.96 26058

II. 9

Page 10 o l i o

505.8 0.63 0.107 0.085 7.62 43.96 49346 97.6

558.7 0.58 0.158 0.104 12.57 43.98 26295 47.1

560.3 0.58 0.163 0.106 13.07 43.99 25634 45.8

43.96

43852 20.0 526.0 0.58 0.154 0.104 12.70 44.48

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Material Balance Low Condensate Case - C2 Recovery Mode Rev.2

GASCO ProjectNo.: 13522102 Doc. No.: 44-00-20012

ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Material Balance Low Condensate Case C2 Recovery Mode Revision 2

Approved Rev.

Date

Description

13-Feb-04

Approved for Construction

4-Sep-03

7-Aug-03

By

Chk.

Disc.

Proj.

GASCO

GS-L-FML046

Approved for Design

m

OPM

DTS

ED

Issued for Approval

OPM

DTS

ED

FLUOH Contract A O W T Rev. 2

GASCO Ethane Recovery Maximization

LOW CONDENSATE CASE - C2 RECOVERY MODE

S t r e a m Number C o m p o s i l i o n (kgmole/h) Nitrogen Methane Elhane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 HSS C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total S t r e a m Molar Flow ( k g m o l e * ) M a s s Flow (kg/h) Temperalure ("C) Pressure (bara) Vapour Fraction Heat F l o w (Gcal/h) Molecular Weight Vapor P h a s e Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight M a s s Flow (kg/h) Std G a s F l o w ( M M S C F D ) Hydrocarbon Liquid P h a s e Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP)

1

10

11

20

22

23

24

0.0 0.0 0.0 0.0 0.0 0.0 0.0

39.5 10013.0 1165.5 5BB.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

39.5 10013.0 1165.5 588.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

56.3 14281.0 1662.3 838.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5 0.0 0.2 0.2 0.3 0.0

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

96.6 24733.6 3000.5 1639.8 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

96.6 24733.6 3000.5 1639.8 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0,6 690.4 0.0 0.4 0.4 1,5 110.5

96.6 24733.6 3000.5 1639.8 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

95.8 24294.1 2B27.B 1427.1 39S.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 21.9

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 0.0

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 87.7

0.8 439.5 172.7 2126 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

32330.0 732576 58.0 66.5 1.00 -686.7 22.66

32330.0 732576 44.4 65.8 0.98 -694.6 22.66

32330.0 732576 27.0 65.4 0.95 •705.4 22.66

30659.8 653637 27.0 65.3 1.00 -647.7 21.32

30637.9 653242 27.8 62.8 1.00 -645.5 21.32

1582.5 77358 27.0 65.3 0.00 -51.7 48.88

1582.5 77358 18.1 31.4 0.23 •51.7 48.88

87.7 1581 27.0 65.3 0.00 -6.0 18.02

1582.5 77358 50.2 30.7 0.35 -49.8 48.88

12627.7 269240 27.6 62.5 1.00 •266.1 21.32

12627.7 269240 -22.5 60.8 0.84 -278.4 21.32

18010.1 384000 27.6 62.5 1.00 -379.5 21.32

14023.5 299000 27.5 62.4 1.00 •295.5 21.32

64.4 0.62 0.014 0.034 22.66 732575 647.9

66.5 0.64 0.014 0.033 22.17 704689 637.1

69.3 0.66 0.014 0.032 21.32 653737 614.4

69.2 0.66 0.014 0.032 21.32 653637 614.4

65.6 0.65 0.013 0.032 21.32 653242 614.0

69.2 0.66 0.014 0.032 21.32

32.4 0.54 0.012 0.027 22.08 8149 7.4

69.2 0.66 0.014 0.032 21.32

34.8 0.54 0.013 0.028 25.74 14870 11.1

65.3 0.65 0.013 0.032 21.32 269240 253.1

77.6 0.82 0.012 0.029 18.95 201505 213.1

65.3 0.65 0.013 0.032 21.32 384000 360.9

65.2 0.65 0.013 0.032 21.32 299000 281.0

530.4 0.60 0.129 0.073 8.00 55.55 26936 50.8

513.4 0.60 0.121 0.074 7.70 48.87 77259 150.5

513.6 0.60

513.6 0.60 0.121 0.074 7.71 48.88 77358 150.6

577.8 0.57 0.168 0.081 10.59 57.04 69207 119.8

513.6 0.60

553.2 0.60 0.138 0.074 8.68 60.88 62488 113.0

951

1580

Thermal Conductivity (Kcal/m-hr-C) S u r f a c e T e n s i o n (dyne/cm) Molecular W e i g h t M a s s Flow (kg/h) A c l u a l V o l u m e Flow (m3/h) Water Phase M a s s Ftow ( M i )

Simulaiion Basis Train 3 - Selected Option • 5% - C2 Mode Rev. BA

0.121 0.074 7.71 48.88

P a g e 1 o l 10

o.o

0.121 0.074 7.71 48.88

465.0 0.64 0.096 0.080 7.31

33.95 67735 145.7

FLUOR Conlract AOWT Rev.2

GASCO Elhane Recovery Maximization

LOW CONDENSATE CASE - C2 RECOVERY MODE

Stream Number Composilion (kgmo!e/h) Nitrogen Methane Elhane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Uquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Ftow {m3/h) Water Phase Mass Flow (kg/h)

25

26

28

29

30

31

32

33

34

36

37

38

43

43.9 11119.8 1294.4 653.2 160.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9 0.0 0.0 0.0 0.1 0.0

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9 0.0 0.0 0.0 0.1 0.0

56.3 14281.0 1662.3 838.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5 0.0 0.2 0.2 0.3 0.0

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 0.0

92.6 22268.9 2025.3 660.0 114.6 139.2 15.9 10.3 2.0 0.6 0.0 0.0 0.4 555.7 0.0 0.1 O.t 0.0 0.0

62.6 15029.6 1366.9 445.4 77.3 94.0 10.7 6.9 1.3 0.4 0.0 0.0 0.3 375.0 0.0 0.1 0.0 0.0 0.0

62.5 15029.6 1366.9 445.4 77.3 94.0 10.7 6.9 1.3 0.4 0.0 0.0 0.3 375.0 0.0 0.1 0.0 0.0 0.0

15.4 3699.2 336.4 109.6 19,0 23.1 2.6 1.7 0.3 0.1 0.0 0.0 0.1 92.3 0.0 0.0 0.0 0.0 0.0

15.4 3699.2 336.4 109.6 19.0 23.1 2.6 1.7 0.3 0.1 0.0 0.0 0.1 92.3 0.0 0.0 0.0 0.0 0.0

92.6 22269.1 2025.4 660.0 114.6 139.3 15.9 10.3 2.0 0.6 0.0 0.0 0.4 555.7 0.0 0.1 0.1 0.0 0.0

90.3 20994.1 1624.6 390.5 47.6 48.1 3.1 1.7 0.1 0.0 0.0 0.0 0.3 490.2 0.0 0.0 0.0 0.0 0.0

90.3 20994.1 1624.8 390.5 47.6 48.1 3.1 1.7 0.1 0.0 0.0 0.0 0.3 490.2 0.0 0.0 0.0 0.0 0.0

14023.5 299000 -6.7 61.3 0.91 -304.5 21.32

3986.6 85000 27.5 62.4 1.00 -84.0 21.32

3986.6 85000 -35.3 60.9 0.75 -89.1 21.32

18010.1 384000 -21.6 60.8 0.85 -396.8 21.32

30637.9 653242 -22.0 60.7 0.84 -675.2 21.32

25865.7 491218 -22.0 60.7 1.00 •541.4 18.96

17470.6 331529 •22.0 60.7 1.00 •365,4 18.98

17470.6 331529 •41.5 60.2 0.92 -372.6 18.98

4300.0 81599 -22.0 60.7 1.00 -89.9 18.98

4300.0 81599 -44.0 60.2 0.90 -92.0 18.98

25886.0 491225 -42.2 60.2 0.91 -552.6 18.98

23691.0 432930 •42.2 60.2 1.00 •496.2 18.27

23691.0 432930 -59.5 40.6 0.93 -498.3 18.27

72.5 0.74 0.012 0.030 19.74 252750 256.6

65.2 0.65 0.013 0.032 21.32 85000 79.9

84.8 0.96 0.012 0.029 18.37 55242 60.3

77.1 0.82 0.012 0.029 19.00 289744 305.7

77.1 0.82 0.012 0.029 18.98 491188 518.7

77.2 0.82 0.012 0.029 18.98 491218 518.7

77.1 0.62 0.012 0.029 18.98 331481 350.1

90.9 1.10 0.012 0.029 18.30 294251 322.2

77.1 0.82 0.012 0.029 18.98 81587 86.2

93.5 1.16 0.012 0.030 18.20 70472 77.6

91.5 1.11 0.012 0.029 18.27 432670 474.6

91.8 1.12 0.012 0.029 18.27 432930 474.8

57.6 0.85 0.010 0.024 17.67 389966 442.3

443.9 0.66 0.085 0.080 6.79 30.39 29758 67.0

466.1 0.63 0.096 0.080 7.33 34.19 94256 2022

465.9 0.63 0.096 0.080 7.33 34.10 162054 347.8

465.8 0.63 0.096 0.080 7.33 34.09

465.8 0.63 0.096 0.080 7.33 34.09 49 0.1

402.6 0.73 0.067 0.078 5.76 26.82 37278 92.6

465.8 0.63 0.096 0.080 733 34.09 12 0.0

392.3 0.75 0.063 0.078 5.49 25.96 11126 28.4

399.9 0.73 0.066 0.078 5.69 26.57 58555 146.4

399.4 0.73 0.066 0.078 5.68 26.56

443.5 0.69 0.079 0.084 7.10 26.50 42964 96.9

479.5 0.62 0.103 0.079 7.49 37.98 46250 96.5

Simutation Basis: Train 3 - Selecled Oplion + 5% - C2 Mode Rev. 8A

Page 2 of 10

FLUOR Contract AOWT Rev. 2

QASCO Ethane Recovery Maxtmization

LOW CONDENSATE CASE - C2 RECOVERY MODE

Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Slream Molar Row (kgmole/h) Mass Flow (kg/h) Temperalure (°C) Pressure (bara) Vapour Fracilon Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density {kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

50

52

53

54

56

57

58

70

72

73

75

76

77

3.3 2025.2 802.5 767.2 280.6 466.5 119.0 94.3 47.8 31.2 1.5 0.0 0.2 112.0 0.0 0.2 0.2 0.5 0.0

22 806.1 73.3 18.9 2.7 3.0 0.3 0.2 0.0 0.0 0.0 0.0 0,0 21.5 0.0 00 0.0 0.0 0.0

1.0 1219.0 729.2 746,2 277.9 463.5 118.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0 0.2 0.2 0.5 0.0

2.3 1275.0 400.5 269.5 67.0 91.1 12.8 8.6 1.8 0.6 0.0 0.0 0.1 65.5 0.0 0.1 0.0 0.0 0.0

1.5 470.3 28.9 4.7 0.4 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 10.2 0.0 0.0 0.0 0.0 0.0

0.8 804.6 371.6 264.8 66.6 90.7 12.8 8.6 1.8 0.6 0.0 0.0 0.1 55.3 0.0 0.1 0.0 0.0 0.0

• 3.8 1276.4 102.2 23.6 3.1 3.4 0.3 0.2 0.0 0.0 0.0 0.0 0.0 31.7 0.0 0.0 0.0 0.0 0.0

95.8 24269.4 1722.0 105.2 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

95.8 24269.1 1722.0 105.2 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0

o.o o.o

95.8 24269.1 1722.0 105.2 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

95.8 24269.1 1722.0 1052 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

89.4 22646.8 1606.9 98.2 2.2 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0 0.0 o.o 0.0 0.0

4752.2 162024 -22.0 60.7 0.00 -133.8 34.09

928.3 17348 •31.3 40.7 1.00 -19.4 18.69

3823.9 144676 •31.3 40.7 0.00 •114.4 37.83

2195.0 58296 •42.2 60.2 0.00 -56.4 26.56

516.5 9163 -54.8 40.7 1.00 -10.7 17.74

1678.4 49133 -54.8 40.7 0.00 -45.8 29.27

1444.8 25511 •39.5 40.7 1.00 •30.0 18.35

26823.1 476258 •63.9 40.5 1.00 -563.3 17.76

26822.9 476258 -53.5 40.1 1.00 -559.0 17.76 .

0.0 0 21.9 39.6 1.00 0.0 17.76

26822.9 476258 -26.3 39.8 1.00 -550.2 17.76

26822.9 476258 21.9 39.6 1.00 •536.5 17.76

25029.9 444422 21.8 39.4 1.00 •500.7 17.76

77.2 0.82 0.012 0.029 18.98

47.7 0.66 0.011 0.025 18.69 17348 18.6

47.7 0.66 0.011 0.025 18.69

91.8 1.12 0.012 0.029 18.27

54.9 0.80 0.010 0.024 17.74 9163 10.4

54.9 0.80 0.010 0.024 17.74

49.6 0,69 0.010 0.025 18 32 26419 28.9

61.6 0.94 0.010 0.024 17.76 476258 537.5

52.8 0.76 0.010 0.024 17.76 476258 537.5

31.2 0.57 0.012 0.030 17.76

41.2 0.63 0.011 0.026 17.76 476258 537.5

3t.2 0.57 0.012 0.030 17.76 476258 537.5

31.1 0.57 0.012 0.030 17.76 444422 501.6

465.8 0.63 0.096 0.080 7.33 34.09 162024 347.8

523.0 0.59 0.129 0.087 9.66 37.83

523.0 0.59 0.129 0.087 9.66 37.83 144676 276.6

399.4 0.73 0.066 0.078 5.68 26.56 58296 145.9

472.4 0.65 0.095 0.086 8.07 29.27

472.4 0.65 0.095 0.086 8.07 29.27 49133 104.0

508.9 0.60 0.119 0.087 9.31 34.89 92 0.2

Simulation Basis: Train 3 - Salecled Oplion • 5% - C2 Mode Rev. 8A

Page 3 of 10

o.o o.o 0.0

o.o o.o o.o o.o o.o o.o 0.0 0.0 0.0 0.0

FLUOR Contract AOWT Rev.2

GASCO Elhane Recovery Maximization

LOW CONDENSATE CASE • C2 RECOVERY MODE

StreamNumber Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2

78

79

80

81

89

90

91

92

93

94

95

96

103

89.4 22646.8 1606.9 98.2 2.2 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0

89.4 22646.8 1606.9 98.2 2.2 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0

89.4 22646.8 1606.9 98.2 22 1-1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0

6.4 1622.3 115.1 7.0 0.2 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 41.9 0.0

2.5 1799.2 836.0 414.9 54.7 55.2 3.6 2.0 0.2 0.0 0.0 0.0 0.2 124.3 0.0

2.5 1799.2 836.0 414.9 54.7 55.2 3.6 2.0 0.2 0.0 0.0 0.0 0.2 124.3 0.0

0.1 367.2 1363.5 706.0 124.0 148.5 16.5 10.6 2.0 0.7 0.0 0.0 0.3 88.7 0.0

1.0 1219.0 729.2 748.2 277.9 463.5 116.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0

1.0 1219.0 729.2 748.2 277.9 463.5 118.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0

1.0 1219.0 729.2 748.2 277.9 463.5 118.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0

0.8 804.6 371.6 264.8 66.6 90.7 12.8 8.6 1.8 0.6 0.0 0.0 0.1 55.3 0.0

0.8 804.6 371.6 264.8 66.6 90.7 12.8 8.6 1.8 0.6 0.0 0.0 0.1 55.3 0.0

0.1 303.4 1051.3 812.1 149.8 181.4 20.1 12.9 2.4 0.8 0.0 0.0 0.2 53.1 0.0

0.0

0.0

0.0

0.0

0.1

0.1

0.1

0.2

0.2

0.2

0.1

0.1

O.t

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.1 0.0 0.0

0.2 0.5 -0.0

0.2 0.5 0.0

0.2 O.S 0.0

o.o 0.0 0.0

o.o 0.0 0.0

o.i 0.0 0.0

25029.9 444422 52.9 39.0 1.00 -492.8 17.76

25029.9 444422 63.0 43.4 1.00 -490.6 17.76

25029.9 444422 53.8 42.8 1.00 -492.9 17.76

1793.0 31836 21.8 39.4 1.00 -35.9 17.76

3292.9 84658 -60.2 40.6 0.00 -85.9 25.71

3292.9 84658 -73.8 25.6 0.20 -85.9 25.71

2826.2 99984 -19.2 29.6 0.00 -80.6 35.35

3823.9 144676 -38.8 26.5 0.14 -114.4 37.83

3823.9 144676 3.4 25.8 0.37 -109.3 37.83

3823.9 144676 2.9 25.1 0.38 -109.3 37.83

1678.4 49133 -66.7 25.8 0.19 -4S.8 29.27

1678.4 49133 -28.2 25.1 0.52 -43.7 29.27

2587.8 96570 -10.9 24.8 0.00 -73.9 37.32

27.0 0.57 0.013 0.034 17.76 444422 501.6

29.0 0.58 0.013 0.035 17.76 444422 501.6

29.6 0.57 0.013 0.034 17.76 444422 501.6

31.1 0.57 0.012 0.030 17.76 31836 35.9

--

34.2 0.68 0.009 0.020 17.38 11269 13.0

--

30.0 0.57 0.010 0.022 18.78 10362 11.1

30.4 0.52 0.011 0.024 23.47 33494 28.6

29.6 0.52 0.011 0.024 23.50 33997 29.0

32.6 0.65 0.009 0.020 17.51 5441 6.2

30.0 0.55 0.010 0.022 20.73 18140 17.5

33.2 0.53 0.010 0.022 24.21 1 0.0

~ ~ --

433.4 0.71 0.073 0.084 6.79 25.71 84658 195.3

492.3 0.64 0.106 0.093 9.35 27.75 73389 149.1

494.4 0.63 0.101 0.089 7.97 35.35 99964 202.2

561.4 0.57 0.166 0.093 11.84 41.05 134314 239.3

538.8 0.59 0.135 0.082 9.36 46.39 111182 206.3

540.6 0.59 0.137 0.083 9.47 46.56 110679 204.7

526.3 0.60 0.135 0.094 10.76 31.94 43692 83.0

531.1 0.S9 0.132 0.092 10.20 38.58 30992 58.4

495.8 0.63 0.104 0.086 7.83 37.32 96570 194.8

M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature CC) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume How (m3*) Water Phase Mass Flow (kg/h)

Simulation Baals: Train 3 - Selected Option + 5% - C2 Mode Rev. 8A

~ — — -

---

— -

PagB4oM0

FIUOR

GASCO Elhane Recovery Maximization

Contract AOWT Rev.2

LOW CONDENSATE CASE - C2 RECOVERY MODE

Stream Numbar Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 HSS C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/Vg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Row (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heal Capacity (kcal/Kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weighl Mass Flow (kg/h) Actual Volume Row (m3/h) Water Phase Mass Flow (kg/h) 0

104

109

110

111

112

113

115

116

117

118

119

120

121

0.1 303.4 1051.3 812.1 149.8 181.4 20.1 12.9 2.4 0.8 0.0 0.0 0.2 53.1 0.0 0.1 0.1 0.0 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 0.5 0.0

1.1 1561.8 987.1 132.3 9.0 7.4 0.3 0.2 0.0 0.0 0.0 0.0 0.2 138.5 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 02 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

42 3798,0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

1.7 1552.3 339.6 43.3 2.6 2.0 0.1 0.0 0.0 0.0 0.0 0.0 0.1

93.7 0.0 0.0 0.0 0.0 0.0

0.4 374.3 81.9 10.4 0.6 0.5 0.0 0.0 0.0 0.0 0.0 0.0 0.0 22.6 0.0 0.0 0.0 0.0 0.0

1.7 1552.3 339.6 43.3 2.6 2.0 0.1 0.0 0.0 0.0 0.0 0.0 0.1 93.7 0.0 0.0 0.0 0.0 0.0

2.1 1871.4 409.5 52.2 3.1 2.4 0.1 0.0 0.0 0.0 0.0 0.0 0.1 113.0 0.0 0.0 0.0 0.0 0.0

2.1 1871.4 40S.5 52.2 3.1 2.4 0.1 0.0 0.0 0.0 0.0 0.0 0.1 113.0 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

2587.8 96570 8.3 24.8 0.16 -71.9 37.32

3815.1 176993 50.0 24.9 0.00 -115.1 46.39

2838.0 67697 -18.0 24.7 1.00 -66.9 23.85

4980.1 101475 -41.7 24,3 1.00 -113.6 20.38

4980.1 101475 •27.0 23.9 1.00 -112.8 • 20.38

4980.1 101475 22.0 23.6 1.00 -110.2 20.38

4980.1 101475 88.8 52.5 1.00 -107.2 20.38

2035.5 41475 88.8 52.5 1.00 -438 20.38

490.8 10000 88.8 52.5 1.00 -10.6 20.38

2035.5 41475 5.4 51.9 1.00 •45.8 20.38

2453.9 50000 88.8 52.5 1.00 -52.8 20.38

2453.9 50000 55.0 51.9 1.00 -53.8 20.38

4980.1 101475 37.5 51.9 1.00 -110.2 20.38

33.8 0.54 0.010 0.021 23.85 67697 56.9

30.7 0.56 0.010 0.021 20.34 101062 99.6

27.4 0.53 0.010 0.022 20.38 101475

21.0 0.51 0.012 0.027 20.38 101475

37.8 0.57 0.014 0.037 20.38 101475 99.8

37.8 0.57 0.014 0.037 20.38 41475 40.8

37.8 0.57 0.014 0.037 20.38 10000 9.8

55.9 0.62 0.012 0.028 20.38 41475 40.8

37.8 0.57 0.014 0.037 20.38 50000 49.2

42.7 0.57 0.013 0.033 20.38 50000 49.2

46.4 0.58 0.013 0.031 20.38 101475 99.8

36.9 0.54 0.011 0.022 28.05 11956 8.5 480.7 0.65 0.094 0.078 6.31 39.14 84614 176.0

Simulallon Basis: Train 3 - Solaclsd OpUon + 3% • C2 Mode Rev. 8A

467.8 0.68 0.085 0.065 4.73 46.39 176993 378.4

516.2 0.61 0.117 0.096 9.84 33.96 413 0.8

Pags 5 of 10

FLUOR Contract AOWT Rev.2

GASCO Elhane Recovery Maximization

LOW CONDENSATE CASE - C2 RECOVERY MODE

Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane i-Butane n-Butane l-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 HZS C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Tolal Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/Vg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg*) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

122

123

124

125

126

127

128

129

130

131

132

141

142

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 .0.2 0.1 0.0 00 0.0 0.0 0.2 229.4 0.0 0.0 00 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 O.S 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 0.5 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 0.5 0.0

0.0 25.6 1136.4 1358.5 403.6 619.5 82.4 48.1 8.2 2.7 0.0 0.0 0.3 41.9 0.0 0.3 0.3 0.1 0.0

0.0 25.6 1136.4 1358.5 403.6 619.5 82.4 48.1 8.2 2.7 0.0 0.0 0.3 41.9 0.0

4980.1 101475 37.3 51.5 1.00 -110.2 20.38

4980.1 101475 -22.5 51.2 1.00 -114.0 20.38

4980.1 101475 •41.5 51.0 0.85 •116.5 20.38

4980.1 101475 -41.7 50.7 0.85 -116.5 20.38

4980.1 101475 -60.4 50.5 0.28 -120.8 20.38

4980.1 101475 -68.3 40.5 0.38 -120.8 . 20.38

0.0 0 •41.5 51.0 0.85 0.0 20.38

0.0 0 -41.5 51.0 0.85 0.0 20.38

3815.1 176993 45.5 22.0 0.06 -115.1 46.39

3815.1 176993 47.5 20.8 0.16 -113.8 46.39

3815.1 176993 52.8 20.5 0.30 -111.8 46.39

3727.7 166257 71.8 19.5 1.00 -96.7 44.60

3727.7 166257 29.5 26.0 0.00 -111.9 44.60

46.0 0.58 0.013 0.031 20.38 101475 99.8

69.8 0.76 0.012 0.027 20.38 101475 99.8

80.0 0.98 0.011 0.027 19.48 82197 84.5

79.3 0.97 0.011 0.027 19.48 82105 84.5

89.7 1.45 0.011 0.027 17.96 24594 27.5

64.9 1.04 0.010 0.024 17.61 33429 38.0

80.0 0.98 0.011 0.027 19.48

80.0 0.98 0.011 0.027 19.48

40.0 0.56 O.011 0.021 37.29 8138 4.4

38.2 0.55 0.011 0.021 38.12 23519 12.4

38.2 0.56 0.011 0.021 39.36 44424 22.6

39.5 0.57 0.011 0.022 44.60 166253 74.7

388.8 0.60 0.055 0.082 5.56 25.31 19278 49.6

390.2 0.80 0.055 0.082 5.59 25.34 19371 49.7

334.6 1.01 0.041 0.075 4.12 21.29 76881 229.8

384.6 0.64 0.052 0.079 5.17 22.06 68046 176.9

388.8 0.80 0.055 0.082 5.56 25.31

388.8 0.80 0.055 0.082 5.56 25.31

480.1 0.67 0.090 0.067 5.24 46.95 16B8S5 351.7

484.0 0.66 0,093 0.067 5.40 47.99 153474 317.1

484.0 0.66 0.094 0.066 5.35 49.35 132569 273.9

478.3 0.66 0.093 0.062 4.68 53.48 4 0.0

Simulation Basia: Train 3 - Selected Option + 5*. - C2 Mo 44-V-301 at -22°C 0

44-V-302 at -42 C o

44-V-305 bottom temperature at -60 C 0

o

-» 44-V-306 top / bottom temperatures are -18 C and 50 C 0

0

44.V-401 top / bottom temperatures are 72 C and 177 C 0

_> 44-V-402 at 29 C Once the system has stabilized, HS-5056 should be positioned such that temperature of 44-V-301 is maintained by adjusting the load of existing refrigeration system via TIC5056. The new refrigeration package should be based loaded (fixed level set point for 44LIC-2111).

CHAPTER 3

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

Once the system has stabilized, the anti-surge valves for the new Propane Compressor should be closed (44-FV-1402 and 44-FV-1403 at 44-C-202). If not, the following steps are recommended: a. ) Increase the load on 44-E-406 by decreasing the duty of the upstream aircooler (44-E402). b. ) Increase the load on 44-E-318 by decreasing the duty ofthe upstream exchanger (44E-306) or by slightly opening the warm feed gas bypass valve M-052.

CHAPTER 3

32

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

CHAPTER 4

N O R M A L START-UP

CONTENTS

SECTION 1.0

2.0

PAGE

GENERAL

2

1.1 1.2 1.3

2 3 3

Stepl Step 2 Step 3

CONTROLLER SETPOINT, A L A R M AND TRIP SETTINGS

4

2.1 2.2

4 2

CHAPTER 4

Existing Controls Modified for E R M Operation New Controls Added for ERM Operation

Fluor Mideast, Ltd. Contract No. AOWT

1.0

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

GENERAL The unit will be started up using the normal start up procedures described in the following: •

Chapter 4 of the existing Operating, Maintenance and Safety Manual

•

Section 6 of Chapter 11 of the existing Operating, Maintenance and Safety Manual (C2 Enhancement Addendum)

•

Chapter 3 of the E R M Operating, Maintenance and Safety Manual

Using the above referenced procedures, Unit 44 will normally be started up in the following sequence:

1.1

•

Step 1: C3 mode + E R M Phase 1

•

Step 2: Transition to C2 Enhancement mode

•

Step 3: Transition to ERM mode (ERM Phase 2)

Step 1 In a normal start-up (i.e. all start-ups after the initial start-up), the E R M Phase 1 equipment will be prepared, purged, dried, pressurized and started up along with the existing systems. nd

2 Feed Chiller (44-E-318): The tube side ofthe exchanger is dried and pressurized with 44E-306 in Step b ofthe procedure provided in Chapter 3, Section 5.2.5.2 ofthe existing manual. Cold Demethanizer (44-V-308): The column is dried and pressurized with 44-V-306 in Step d of the procedure provided in Chapter 3, Section 5.2.5.2 of the existing manual. Debutanizer Trim Condenser (44-E-406) and NGL Subcooler (44-E-407): The tube side of the exchanger is dried and pressurized with Debutanizer system in Step i of the procedure provided in Chapter 3, Section 5.2.5.2 ofthe existing manual. The Cold Demethanizer Bottoms Pumps should also be prepared, purged, pressurized and dried along with the Cold Demethanizer as a part of Step 1. The pumps will not be started until Step 3. Refer to Chapter 3 of this manual for more information. For a normal start-up, separation blinds will not be required to isolate the Phase 2 systems from the rest of the plant.

CHAPTER 4

Fluor Mideast, Ltd. Contract No. AOWT

A

1.2

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

Step 2 Using the procedure contained in the C2 Enhancement Addendum, the unit is transitioned to C2 Enhancement mode.

A

1.3

Step 3 Once the unit is operating stably in C2 Enhancement mode, the Cold Demethanizer Bottoms Pumps can be started. Refer to the procedure in Section 10.1 of Chapter 3 for more information. The E R M refngeration system is prepared, purged, pressurized and start-up according to the procedures contained in Chapter 4 of this manual. This procedure can also be selective applied for re-starts of the E R M refrigeration system after trips. Once the E R M refrigeration system is operating smoothly in recycle, the unit can be transitioned to the E R M operating mode using the procedure in Section 10.3 of Chapter 3.

CHAPTER 4

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

2.0

CONTROLLER SETPOINT, ALARM AND TRIP SETTINGS

2.1

Existing Controls Modified for ERM Operation

2.1.1

Setpoints and Alarms

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

The E R M Project does not impact the existing Dehydration System or the existing Refrigeration System. Therefore, there are no changes to the controller set points or alarms shown in the following P&ID's: 44-00-30001 44-00-30002 44-00-30003 44-00-30004 44-00-30005 44-00-30007

44-00-30008 44-00-30009 44-00-30014 44-00-30015 44-00-30016 44-00-30017

The changes to the existing controller set points and alarms for the P&ID's listed below are summarized in Table 2.1. 44-00-30018 44-00-30019- 1 of 2 44-00-30019-2 of 2 44-00-30020 44-00-30021 44-00-30022 44-00-30023 - 1 of4 44-00-30023-2 of 4 44-00-30023-3 of 4 44-00-30023-4 of 4 44-00-30024 44-00-30025 44-00-30026 44-00-30027 44-00-30028- 1 of 3 44-00-30028- I of 3 44-00-30028- 1 of 3

2.1.2

Trips No changes to existing trip settings are required.

CHAPTER4

FLUOR Conlract AOWT Rev. 0. 23-Sept-04

GASCO Ethane Recovery Maximization Project 5221

TABLE 2.1 - UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)

Alarms

Operating Mode Description

Tag Number

P&ID

TIC-5054

018

ERM Case

30% C2 20% C2 10% C2 C2 Recovery Recovery Recovery Rejection

High

Comments

Low

TEMPERATURE Residue Gas to E-309 LP Recycle Gas from E-301 V-301 Temperalure Feed Gas from E-301

018

22

23

18

22

22

30

New conlrol selpoinl. New TAL selpoinl. Currenl TAL = -19.

TIC-5056 TI-5057

018

-23

-20

V-302 Temperature Feed Gas from E-302

TI-5059

HP Recycle Gas from E-302

TI-5060

HP Recycle Gas from E-304

TI-5075

HP Recycle Gas from E-303

TI-5118

Feed Gas from E-313

018

-38

-60

-58

-55

-56

018

-42

-38

-32

-31

019

-35

-28

019

Feed Gas from E-306

TI-5063

019

V-304 Temperature

TI-5065

020

2nd Stage Liquid lo E-314

TI-5066

020

TIC-5067

020

2nd Stage Liquid from E-314

TI-5068

020

-28

-24

EC-301(Expander) Outlei

TI-5070

021

-60

-56

021

-40

New control setpoint. New TAL setpoint. Current TAL = -30.

-55 -62

-57

-53

-54

63

-50

-51

52 64

-35

New TAL setpoint.

-36

-65

New TAL selpoinl. Currenl TAL = -58.

62

42

-18 -53

64

New conlrol setpoint.

-15

-34

53 TI-5113

New control setpoint. New TAL setpoint. Current TAL = -37.

-36

018

EC-301 (Compressor) Inlet

-17

-32

TI-5062

EC-301 (Compressor) Outlet

-35

-42

1st Stage Liquid from E-313

Feed Gas from E-314

New control setpoint.

64

64

FLUOR Contract AOWT Rev. 0, 23-Sept-O'f

GASCO Ethane Recovery Maximization Project 5221

TABLE 2.1 - UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)

Operating Mode Description

Tag Number

P&ID

Units

ERM Case

Residue Gas from E-311

TI-5073

021

•C

54

V-30S Overhead

TI-5076

022

•C

022

•C

-60

022

•c

-42

Reboiler Retum HP Recycle Gas fram E-303

TI-5078

V-305 Tray 11

TI-5079

V-305 Bottoms

TIC-5080

022

V-306 Overhead

TIC-5081

023 1/3

V-306 Tray 2

TIC-5082

023 1/3

V-306 Reboiler Draw

TI-5083

023 1/3

V-306 Reboiler Return

TI-5084

023 1/3

V-306 Overhead lo E-305

TI-5085

023 1/3

Alarms

30% C2 20% C2 10% C2 C2 Recovery Recovery Recovery Rejection 54

54

-61

60

-38

54

54

55

-53

-12

•35

-32

-31

High

Comments

65

60

42

•C

V-305 Bottoms from E-317

TI-5205

023 3/3

Feed Gas from E-317

TI-5206

023 3/3

V-307 Ovhd Temperature

TIC-5207

023 3/3

V-306 Side Reboiler Outlet

TIC-5088

024

Recycle Gas from E-307

TI-5089

024

Recycle Gas to E-315

TI-5090

024

Recycle Gas from E-315

TI-5092

024

C-301 Suction

TI-5740

48

35

69 70

-19

V-306 Top Feed from E-305

New conlrol selpoinl. New TAL setpoinL Current TAL = -56 New conlrol setpoint. New TAH setpoinL Curren TAH = 1. New control setpoint. New TAL setpoint. Current TAL = 67.

•c

-12

-38

-43

-53 32

New TAL setpoint. Current TAL = -37

-30 -45

15

22

33

38

40

38

37

40

37

22

27

22

22

22

22

22

64

65

New control setpoint. New TAL setpoint. Current TAL = -53. New conlrol setpoint. New TAL setpoinL Currenl TAL = 24.

GASCO Ethane Recovery Maximization Project 5221

FLUOR Contract AOWT Rev. 0, 23-Sept-04

TABLE 2.1 • UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)

Operating Mode Description

Tag Number

PSID

C-301 Discharge V-401 Feed Temperature

TIC-5212

026

Units

ERM Case

•C

89

•C

53

V-306 Bolloms from E-101 C5+ form E-401

87 63

71

TI-5096

50

026

V-306 Bottoms to E-401

TI-5107

V-401 Overhead

TI-5098

TI-5102

V-401 Tray 26

TI-5294

V-401 Reflux/NGL Product

TI-5105

177

177

73

80

°C

29

40

barg

59.3

59.3

027

028

New control setpoint. New TAH setpoint. Curren TAH = 73

82

62

74

New TAL setpoint. Current TAL = 84

120

75

77

55

55

73

75

156

•C

TIC-5099

V-401 Reboiler Retum

72

027

Comments

High

76

58

C5+ to Storage

V-401 Tray 7

Alarms

10% C2 C2 30% C2 20% C2 Recovery Recovery Recovery Rejection

145 165

161

48

59

65

160

110

PRESSURE EC-301 (Expander) Inlet

PIC-3501

59.3

59.3

59.3

39.1

38.6

EC-301 (Expander) Outlet

PI-3044

021

barg

39.6

39.6

Residue Gas from E-311

PIC-3046

021

barg

41.8

42.1

42.0

42.2

Residue Gas from E-311

PI-3047

021

barg

42.1

42.0

42.2

EC-301 (Compressor) Outlet

PI-3515

021

barg

42.7

42.6

42.4

44.2

39.2

46.2

40.4

41.8 42.4

37.1

37.1

37.0

EC-301 (Compressor) Inlet

PI-3516

021

barg

38.0

V-305 Overhead

PI-3049

022

barg

39.5

39.5

39.0

39.0

38.5

PDI-3050

022

bar

0.2

0.2

0.2

0.2

0.2

V-305 Pressure Drop

68.0

0.5

GASCO Ethane Recovery Maximization Project 5221

FLUOR Contract AOWT Rev. 0,23-Sept^4

TABLE 2.1 - UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)

Operating Mode Description HP Recycle from E-315 V-306 Overhead V-306 Overhead to E-305 V-306 Pressure Drop V-306 Tray 17

Tag Number

P&ID

PIC-3058

Units

ERM Case

barg

50.5

023 1/3

barg

23.0

23.0

PI-3052

023 1/3

barg

23.0

23.0

023 1/3

PI-3055

023 1/3

V-306 Tray 10

barg

23.0

23.0

23.6

23.6

barg

PIC-3060

025

barg

21.7

PIC-3201

025

barg

51.5

C-301 Suction

PI-3730

025

barg

C-301 Discharge

PI-3731

V-401 Pressure Drop

23.0

0.2

023 3/3

C-301 Discharge

50.5

23.0

High

50.5

New control setpoint.

22.7

New control setpoint. New PAH setpoint. Cunen PAH = 23.3

23.0

22.7

0.2

0.2

23.0

22.7

barg PIC-3202

C-301 Suction

50.5

PIC-3051

PDI-3054

Alarms

30% C2 20% C2 10% C2 C2 Recovery Recovery Recovery Rejection

PIC-3064

027

PDI-3065

027

PIC-3068

028

23.6

23.6

23.6

21.7

21.7

21.4

51.5

51.5

21.7

21.4

51.5

51.5

15.0

15.0

51.5 21.7

barg

51.5

barg

18.5 0.2

barg

17.5

Nm3/h

283000

51.5 18.5 0.2

0.2

0.2

20.0

New PAH setpoint. Currenl PAH = 24.5

19.6

New PAH selpoinl. Current PAH = 22.6

59.5 17.9 59.0

50.5

New PAL setpoint. Currenl PAL = 51.6 New PAH setpoint. Current PAH = 18.5

0.5

17.5

14.5

14.5

13.9

283000

283000

283000

283000

240000

89400

89400

581500

586300

257

253

336

323'

New PAH selpoinl. Current PAH = 18.0

FLOW Feed Gas to E-301 Feed Gas to E-313 EC-301 (Compressor) Inlet

FIC-1034 FIC-1035

019

FI-1501

021

Liquid from V-305

FIC-1041

Liquid from V-306

FIC-1042

023 1/3

89400

89400

89400

561000

568420

574800

m3/h

195

213

m3/h

378

365

Nm3/h

351

Cascade from TIC-5054 Cascade from TIC-5061

642000

270400 Cascade from LIC-2046

420

275

New control setpoint. Current FAH = 380. Cascade from LIC-2047

FLUOR Contract AOWT Rev. 0, 23-Sept-M

GASCO Ethane Recovery Maximization Project 5221

TABLE 2.1 - UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)

Alarms

Operating Mode Description

Tag Number

ERM Case

Feed Gas to E-317

FIC-1203

023 3/3

Liquid from V-307

FIC-1204

023 3/3

Flow from E-316

FIC-1201

024

C-301 Suclion

FI-1730 FIC-1046

C2 10% C2 20% C2 30% C2 Recovery Recovery Recovery Rejection 92200

92200

92200

153

m3/h 55000

52400

50700

111600

113600

117100

58

91

NGL to Storage

High

92200

110000

183

200

121800

87000

60000

13000

120000

61700

60 350

200

Cascade from TIC-5207 New FAH setpoint. Current FAH = 136. Cascade from LIC-2204 New controi setpoint. New FAH setpoint. Curren FAH = 39000 New FAH selpoinl. Current FAH = 109500 New control setpoint. Current FAL = 60. Cascade from FIC-1048 New FAL and FAH setpoints. Currenl FAH = 280 Cunent FAL = 250. Cascade from LIC-2059

LEVEL V-301 Level

795

1190

400

No impact.

V-302 Level

LIC-2038

550

740

350

No impact.

V-303 Level

LIC-2040

1675

2900

450

No impact.

250

No impact.

018

LIC-2042

019

680

V-304 Level

LIC-2044

020

1400

2480

320

No impact.

V-305 Level

LIC-2046

1050

250

No impact.

LIC-2047

023 1/3

70%

3000

300

No impact.

E-308 Level

LIC-2050

023 1/3

250

No impact.

E-403 Level

LIC-2052

026

80%

1020

500

No impact.

LIC-2204

023 3/3

20%

5250

300

No impact.

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44

Fluor Mideast, Ltd. Contract No. AOWT

Addendum for the ERM Project - Rev. 1

2.2

New Controls Added for ERM Operation

2.2.1

Setpoints and Alarms

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

The setpoints for the new controllers and alarms added for the E R M Project are described in Table 2.2a. 2.2.2

Trips The new trip functions and the associated trip settings that have been added for the E R M Project are described in Table 2.2b. The following Cause and Effect Diagrams are also provided:

2.2.3

Drawing Number

Description

CEC 44-00-25-001

Unit 44 Process Cause and Effect Chart

04305 CET

E R M Refrigeration Package Cause and Effect

Manual Valves Table 2.2c provides a summary of the position (open or closed) for the manual valves added for the E R M Project based on the target ethane recovery level. N O T E : When changing the positions of a set of valves, it is critical that the closed valve be opened before the open valve is closed. This will prevent the system from being blocked-in. For example, when transitioning from C2 Enhancement mode to E R M mode, manual valve M-4402 is opened before M-4401 is closed.

CHAPTER4

GASCO Ethane Recovery Maximization Project 5221

FLUOR Conlract AOWT Rev. 0, 23-Sept-04

TABLE 2.2a - UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW)

Alarms

Operating Mode Description

Tag Number

P&ID

Units

30% C2 ERM Case Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

-36

-32

-27

51

55

40

40

20

58

High

Low

Comments

TEMPERATURE E-313 Shell Side Inlet

TI-5131

019-1

-39

-37

V-401 Overtiead from E-402

TI-5124

028-1

51

51

E-406 Tube Side Outlet

TI-5127

028-1

20

30

35

35

E-407 Tube Side Outlet

TI-5121

028-3

20

35

35

35

59 35 35

-41

E-203 Outlet

TI-5410

22717-104

55

55

55

55

55

C-202 Low Stage Inlet

TIC-5405

22717-102

-24

-24

-24

-24

-24

C-202 Side Load Inlet

TIC-5404

22717-103

16

16

16

16

16

25

C-202 Discharge

TI-5401

22717-101

75

75

75

75

75

85

Lube Oil Supply

TI-5416

10512S

60

71

Lube Oil Reservoir

TI-5417

10512S

75

50

C-202 Motor Bearing

TI-5420AB

GE 127

70

80

High-high alarm at 90°C

C-202 Motor Bearing

TI-5421AB

GE 127

70

80

High-high alarm at 90°C

40 o

15

Set TAL at 0.1 C above the vapor dew point at suction pressure read by PT-3405. Set TAH at I O X above the vapor dew point at suclion pressure read by PT-3405. Set TAL al 0.1 "C above the vapor dew point at suction pressure read by PT-3404. Set TAH al 10°C above the vapor dew point al suction pressure read by PT-3404.

C-202 Motor Stator

TI-5422AB

G E 127

120

130

High-high alarm a l l 40°C

C-202 Molor Slator

TI-5423AB

G E 127

120

130

High-high alarm at M O ' C

C-202 Motor Stator

TI-5424AB

GE 127

120

130

High-high alarm at M O ' C

C-202 Gear High Speed Bearings

TI-5430AB

GE127

97

107

C-202 Gear High Speed Bearings

TI-5431AB

G E 127

TI-5432AB

GE 127

C-202 Gear Low Speed Bearings

TI-5433AB

GE 127

C-202 Gear Inboard Thrust Bearings

TI-5434A-C

G E 127

C-202 Gear Outboard Thrust Bearings

TI-5435A-C

G E 127

C-202 Bearings

TI-5440AB

GE 127

97 97 97 97 97 89

107

C-202 Gear Low Speed Bearings

C-202 Bearings

TI-5441AB

GE127

89

99

C-202 Bearings

TI-5442AB

G E 127

89

C-202 Bearings

TI-5443A8

G E 127

89

99 99

107 107 107

107 99

GASCO Ethane Recovery Maximization Project 5221

FLUOR Contract AOWT Rev. 0, 23-Sep(-04

TABLE 2.2a • UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW

Alarms

Operating Mode Tag Number

P&ID

C-202 Bearings

TI-5444AB

GE 127

89

C-202 Bearings

TI-5445AB

GE 127

89

Description

Units

30% C2 ERM Case Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejeclion

High

C-202 Bearings

TI-5446AB

GE 127

89

99

C-202 Bearings

TI-5447AB

G E 127

89

99

CM-202 Inlet Air

TI-5425A

GE411

CM-202 Inlet Air

TI-5425B

GE411

^

f-r-

Low

99 99

80

„ ^ .

PRESSURE PI-3081

023-4

barg

23.3

23.3

23.3

23.3

22.3

PDI-3082

023-4

bar

0.2

0.2

0.2

0.2

0.2

P-302 Discharge

PI-3083

023^

barg

26.0

23.0

P-302A Seal Pot

PI-3084A

023^1

barg

28.0

27.0

P-302B Seal Pot

PI-3084B

023-4

V-308 Tray 8 V-308 AP

V-205

PIC-3410A 22717-104

0.5

27.0

28.0 barg

18.8

18.8

18.8

18.8

19.7

17.0

C-202 Low Stage Inlet

PI-3403

22717-102

barg

1.0

1.0

1.0

1.0

C-202 Side Load Inlet

PI-3402

22717-103

barg

6.4

6.4

6.4

C-202 Discharge

PI-3401

22717-103

barg

19.3

19.3

V-206

PI-3413

22717-103

barg

6.4

V-207

PI-3414

22717-102

barg

1.0

PDI-3430

GE561

mmH20

1000

2540

Seal Gas Filler AP (N2)

PDI-3431

G E 561

mmH20

1000

2540

Balance Chamber AP

PDI-3432

GE 561

mmH20

1000

1270

Buffer Gas

PI-3433

GE561

barg

1.4

C-202 Lube Oil

PI-3421

G E 529

barg

1.4

Lube Oil Pump A Discharge

PI-3415A

10512S

barg

5.2

4.5

Lube Oil Pump A Discharge

PI-3415B

10512S

barg

5.2

4.5

Lube Oil Filter AP

PDI-3416

10512S

_bar _

0.3

PI-3417

10512S

PDI-3425

GE411

Seal Gas Filler A P (Process Gas)

Lube Oil Supply CM-202 Air Intake

g

b a r

9-

mmH20

0.2

6.4

1.0 6.4

7.3

5.3

19.3

19.3

19.3

20.2

17.5

6.4

6.4

6.4

6.4

8.6

1.0

1.0

1.0

1.0

1.4

2.8

0.7

1.0 1.0 20.0

Comments

GASCO Ethane Recovery Maxtmization Project 5221

FLUOR Contract AOWT Rev. 0, 23-Sept-04

TABLE 2.2a • UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW)

Alarms

Operating Mode Description

Tag Number

P&ID

Units

30% C2 ERM Case Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

201

241

239

High

Low

Comments

FLOW P-302 Discharge

FIC-1070

023^1

m3/h

265

60

22717-102

Nm3/h

22500

26000

18000

Alarm settings to be confirmed by vendor.

FI-1402

22717-103

Nm3/h

78400

90000

63000

Alarm sellings lo be conlirmed by vendor. Alarm sellings to be confirmed by vendor.

C-202 Low Stage Inlet C-202 Side Load Inlei C-202 Discharge

202

236

FI-1400

22717-103

Nm3/h

100900

116000

81000

C-202 Discharge to Seal System

FIC-1430

G E 561

Nm3/h

1.7

2.9

1.2

^ 2 to C-202 Seal System

FIC-1431

GE 561

Nm3/h

1.7

Primary Vent Gas to Flare (Suction)

FI-1432D

GE 561

3.4

Primary Vent Gas to Flare (Discharge)

FI-1433D

G E 561

Nm3/h NmS/h

Cascade from LIC-2126

1.2

3.4

6.8

2.4

LEVEL E-318 Level

LIC-2111

019-2

1390

1590

500

V-308 Level

LIC-2126

023^1

4100

5000

2000

E-406 Level

LIC-2116

028-1

1240

1440

E-407 Level

LIC-2121

028-3

810

960

500 500

V-205 Level

LI-2403

22717-104

888

-1194

V-206 Level

LIC-2404

22717-103

-381

Measured from centerline of E-204

V-207 Level

LIC-2405

22717-102

-229

Measured from centerline of E-205

C-202 Lube Oil Rundown Tank

LI-2420

GE529

533 305 92%

C-202 Lube Oil Reservoir

LI-2431

10512S

100%

830

MISCELLANEOUS E-203 Vibration Bay 1

VAH-9050

041

E-203 Vibration Bay 2

VAH-9051

041

E-203 Vibration Bay 3

VAH-9052

041

E-203 Vibralion Bay 4

VAH-9060

041

E-203 Vibration Bay 5

VAH-9061

041

E-203 Vibration Bay 6

VAH-9062

041

E-203 Vibration Bay 7

VAH-9070

041

E-203 Vibration Bay 8

VAH-9071

041

E-203 Vibration Bay 9

VAH-9072

041

77%

^*

f-'V

^

mm

ass

d''J.-1~--- .... *

Measured from centerline of V-205

FLUOR Contract AOWT Rev. 0, 23-Sept-04

GASCO Elhane Recovery Maximization Project 5221

TABLE 2.2a - UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW)

Alarms

Operating Mode 30% C2 ERM Case Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

Tag Number

P&ID

C-202 Motor - Vibration X

VXI-9410

G E 127

72

VYI-9410

GE 127

72

85 85

High-high Alarm at 99 um

C-202 Motor - Vibration Y C-202 Motor - Vibration X

VXI-9411

G E 127

72

85

High-high Alarm at 99 um

C-202 Motor - Vibration Y

VYI-9411

GE 127

72

85

High-high Alarm at 99 um

C-202-E1A Vibration

VAH-9415A

10512S

C-202-E1B Vibration

VAH-9415B

10512S

C-202-E1C Vibralion

VAH-9415C

10512S

VXI-9420

G E 127 32

45

Description

C-202 Gear High Speed - Vibration X

Units

High

iC-202 Gear High Speed - Vibration Y

VYI-9420

GE 127

C-202 Gear Low Speed - Vibralion X

VXI-9421

G E 127

C-202 Gear Low Speed - Vibration Y

VYI-9421

GE 127

51

64

C-202 Gear Low Speed - Vibration X

VXI-9422

G E 127

51

64

C-202 Gear Low Speed - Vibration '

VYI-9422

GE 127

51

C-202 Gear High Speed - Vibralion X

VXI-9423

G E 127

32

64 45

C-202 Gear High Speed - Vibration Y

VYI-9423

G E 127

32

45

C-202 Compressor - Vibration X

VXI-9430

G E 127

32

C-202 Compressor - Vibralion Y

VYI-9430

G E 127

32

45 45 45 45

Low

Comments

High-high Alarm al 99 um

64

C-202 Compressor - Vibration X

VXI-9431

G E 127

32

C-202 Compressor - Vibration Y

VYI-9431

G E 127

32

C-202 Gear Low Speed - Axial Posilion

VZI-9424AB

GE 127

0.13

C-202 Compressor - Axial Position

VZ1-9432AB

G E 127

0.13

C-202 Gear High Speed - Acceleration

VI-9441

GE 127

m/s2

C-202 Gear Low Speed - Acceleration

VI-9440

G E 127

m/s2

C-202 Compressor - Acceleration

VI-9450

G E 127

m/s2

C-202 Compressor - Acceleration

VI-9451

GE 127

m/s2

39 39 39 39

High-High Alarm at 50 m/s2 High-High Alarm at 50 m/s2

GASCO Ethane Recovery Maximization Project 5221

FLUOR Contract AOWT Rev. 0, 23-Sept-04

TABLE 2.2b - UNIT 44 SETTINGS FOR NEW TRIPS

Description

Tag Number

P&ID

Units

Trip

Action

TEMPERATURE E-314 Shell Side Outlet

TALL-5126

020

-43

Closes LV-2044

E-313 Shell Side Inlet

TALL-5130

019-1

-43

Closes XV-9080 and LV-2111

C-202 Discharge

TAHH-5400

22717-101

90

C-202 shutdown

TI-5417 TI-5417

10512S

32

Heater on

10512S

50

Heater off

C-202-E2A

TI-5418A

10512S

75

Heater off

C-202-E2B

TI-5418B

10512S

75

Heater off

C-202 Gear High Speed Bearings

TAHH-5430

G E 127

C-202 shutdown

C-202 Gear High Speed Bearings

TAHH-5431

G E 127

C-202 Gear Low Speed Bearings

TAHH-5432

G E 127

C-202 Gear Low Speed Bearings

TAHH-5433

G E 127

C-202 Gear Inboard Thrust Bearings

TI-5434A-C

G E 127

115 115 115 115 115 115 115 115 115 115 115 115 115 115

Lube Oil Reservoir Lube Oil Reservoir

C-202 Gear Outboard Thrust Bearings

TI-5435A-C

GE127

C-202 Suction End Bearings

TAHH-5440

G E 127

C-202 Suction End Bearings

TAHH-5441

G E 127

C-202 Discharge End Bearings

TAHH-5442

G E 127

C-202 Discharge End Bearings

TAHH-5443

GE127

C-202 Active Thrust Bearings

TAHH-5444

G E 127

C-202 Active Thrust Bearings

TAHH-5445

G E 127

C-202 Inactive Thrust Bearings

TAHH-5446

G E 127

C-202 Inactive Thrust Bearings

TAHH-5447

G E 127

P-302A Seal Pressure

PALL-3084A

P-302B Seal Pressure

PALL-3084B

023-1 023-1

C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown

PRESSURE barg

26.5

P-302A Trip

barg

26.5

P-302B Trip

Comments

GASCO Ethane Recovery Maximization Project 5221

FLUOR Contract AOWT Rev. 0, 23-Sept-04

TABLE 2.2b - UNIT 44 SETTINGS FOR NEW TRIPS

Tag Number

P&ID

Units

Trip

Action

C-202 Discharge

PAHH-3400

barg

C-202 Side Load

PALL-3404

barg

21.0 3.6

C-202 shutdown

Description

Comments

C-202 Suction

PALL-3405

22717-101 22717-103 22717-102

barg

0.0

C-202 shutdown

C-202-P1A Discharge

PAL-3415A

10512S

barg

4.5

Start B pump

C-202-P1B Discharge

PAL-3415B

10512S

barg

4.5

Start A pump

C-202 Lube Oil

PALL-3420

G E 529

barg

0.35

C-202 shutdown

2 out of 3 voting

Primary Vent Gas to Flare (Suction)

FAHH-1432

GE561

Nm3/h

9.5

C-202 shutdown

2 out of 3 voting

Primary Vent Gas to Flare (Discharge)

FAHH-1433

GE 561

Nm3/h

9.5

C-202 shutdown

2 out of 3 voting

V-308 Level

LALL-2127

023-4

300

P-302 A/B shutdown

V-206 Level

LAHH-2401

22717-103

-991

C-202 shutdown

Trip setting is measured from V-206 centerline.

V-207 Level

LAHH-2402

22717-102

-686

C-202 shutdown

Trip setting is measured from V-207 centerline.

E-203 Vibration Bay 1

VSH-9050AB

E-203 Vibration Bay 2

VSH-9051AB

E-203 Vibration Bay 3

VSH-9052AB

E-203 Vibration Bay 4

VSH-9060AB

E-203 Vibration Bay 5

VSH-9061AB

E-203 Vibration Bay 6

VSH-9062AB

E-203 Vibration Bay 7

VSH-9070AB

E-203 Vibration Bay 8

VSH-9071AB

041 041 041 041 041 041 041 041

C-202 shutdown

FLOW

LEVEL

MISCELLANEOUS Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

Fan motor shutdown

Activated from D C S

FLUOR Contract AOWT Rev. 0, 23-Sept-04

GASCO Ethane Recovery Maximization Project 5221

TABLE 2.2b - UNIT 44 SETTINGS FOR NEW TRIPS

Description

Tag Number

P&ID

Units

Trip

Action

Comments

Fan motor shutdown

Activated from D C S

E-203 Vibration Bay 9

VSH-9072AB

041

C-202 Gear High Speed - Vibration X

VXAHH-9420

G E 127

64

C-202 shutdown

C-202 Gear High Speed - Vibration Y

VYAHH-9420

G E 127

VXAHH-9421

GE 127

C-202 Gear Low Speed - Vibration Y

VYAHH-9421

GE 127

C-202 Gear Low Speed - Vibration X

VXAHH-9422

G E 127

64 102 102 102

C-202 shutdown

C-202 Gear Low Speed - Vibration X

C-202 Gear Low Speed - Vibration Y

VYAHH-9422

G E 127

C-202 shutdown

C-202 Gear High Speed - Vibration X

VXAHH-9423

GE 127

C-202 Gear High Speed - Vibration Y

VYAHH-9423

G E 127

102 64 64

C-202 Compressor - Vibration X

VXAHH-9430

G E 127

57

C-202 shutdown

C-202 Compressor - Vibration Y

VYAHH-9430

G E 127

57

C-202 shutdown

C-202 Compressor - Vibration X

VXAHH-9431

G E 127

57

C-202 shutdown

C-202 Compressor - Vibration Y

VYAHH-9431

G E 127

57

C-202 shutdown

2 out of 2 voting

C-202 Gear Low Speed - Axial Position

VZAHH-9424AB

GE 127

0.25

C-202 shutdown

2 out of 2 voting

C-202 Compressor - Axial Position

VZAHH-9432AB

G E 127

mm

0.25

C-202 shutdown

C-202 Gear High Speed - Acceleration

VAHH-9440

G E 127

m/s2

50

C-202 shutdown

C-202 Gear Low Speed - Acceleration

VAHH-9441

GE 127

m/s2

50

C-202 shutdown

->4

C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown

FLUOR Contract AOWT Rev. 0, 23-Sept-04

GASCO Ethane Recovery Maximization Project 5221

TABLE 2.2c - UNIT 44 MANUAL VALVES

Operating Mode Valve Tag

M-4401 M-4402

M-4404

20% C2 Recovery

10% C 2 Recovery

C2 Rejection

Comments

Open

Open

Closed

New valve

P&ID

ERM Phase 1

E-303 Bypass (HP Recycle)

018

Closed

Open

Open

E-314 Outlet to V-306

020

Open

Closed

Closed

Open

Open

Open

New valve. Works together with M-4402.

023-1

Closed

Open

Open

Closed

Closed

Closed

New valve. Works together with M-4401.

022

Closed

Closed

Closed

Closed

Closed

Open

Existing valve

023-1

Open

Closed

Closed

Closed

Closed

Closed

New valve. Works together with M-4404.

Description

E-314 Outlet to V-308 E-303 Isolation (V-305 Bottoms)

M-4403

30% C 2 Recovery

ERM Mode

V - S O / Liquid to V-306 V-307 Liquid to V-308

023-1

Closed

Open

Open

Open

Open

Open

New valve. Works together with M-4403.

Open

Closed

Closed

New valve. Works together with M-4406.

Closed

Open

Open

New valve. Works together with M-4405.

M-4405

E-315 Bypass (HP Recycle)

024

Closed

Open

Open

M-4406

E-315 Isolation (HP Recycle)

024

Open

Closed

Closed

Page ONSHORE GAS DEVELOPMENT PROJECT N" 545

TITLE

ADNOC - HABSHAN PROCESS CAUSE AND EFFECT CHART

UNIT 44 4 i 5

RevPage

Rev.

| 6 | 7

Page

! r

8 i 9

x ': x I x 1 X X I X

: X i

! X j X ' X j X

1 Bis

X I X | X

X

2 Bis . X

2 Ter

. -5

X X

X

X

FLUOR

Project 5221 Agreement 13522102 Fluor Contract AOWT

Unit

CEC

44

3/3/95

A. PIHOUEE

R. AGAZZI

8.1

19/9/94

Y. SIMON

J. CASTEL

7\ai/5/c*\

2 I'

2/8/94

Y. SIMON

R.AGAZZI

7Ai

1

25/1/94

i

H. MAHE

J. CASTEL

0

5/10/93

i

A LEGALL

R. AGAZZI

Rev.

JJ/MUfAA

Written by

Checked by

6/5/97 19/4/97

Document revisions 76001. CECO! - SPPW - R x . 1 - AKO-W1J0M.0 .

Serial No

Rev

25-001

CERTIFIED

1 W o4

Rev

Symbol

Dm

;

f >NiH A

;E

Y. SIMON

A. RABINIAUX

Y. SIMON

R. AGAZZI

Written by

Checked by

PROCESS SPECIFICATION OrjuctiC

TECHNIP CEC CLIENT

Rev. ADNOC

LOCATION HABSHAN

NOTES

UNIT 44

5

|

7 6 ^ J L C=C

Date 5/10/93 25/1/94 2/8/94

Made by ALG HM

3/3/95 19/4/96

PHA

GENERAL A/OTES-

Le«f«< 1 conBtponctstoa loea! sftm down ( t o pump E * M t»o*r) Level 2 corresponcft to • systam shut down (a.g. group of items) or zone anm oown Zona stu* down corresponds to Units 34 - *A shut down tor xor* 20

17 IE

WOTES 1 S I G N A l WITH START UP OVERRIDE •W-HS-SOIS FOR 44J'ALI -3029 t * - H S - X \ B FOH 4*4>ALL-3032

25 26

2 SIGNAL G E N E R A T E D BY COMPRESSOR VENDOR PLC

4DEIETCO 5 SIGNAL WITH START-UP OVERRIDE 4 4 + i & 9 0 M FOR 44-PALL-3069

8 SIGNAL W T H START UP O V E R R D E 44+IS-9021 FOR 44-FAU.-3071 9 XV-9006 PERMISSIVE TO O P E N : 44-PclSt-3Q73 10 CONTROL TRANSFERRED TO 44-LV-20S2B 11 ESO S E Q U E N C E O F MACHINES AND PACKAGES A R E BY VEWJORS 12 INWatTION O F 44-XHSC-9077 F THE HEATER W g - I O I U l IS RUNNING (STATUS OF HEATCR B Y 44-XL-7817) 13 44-XZSO-90O3 P E R M B S V E TO START 44-C-201 14 44-XZSC7501 PERMISSIVE TO OPEN 44.XV-S0OS B PERMISSIVE TO START 44-EC-301 (XS-9022) 15 CLOSING T H E V A L V E 44-XV-9006 WHL STOP THE TURBO EXPANDER AND WIU. GENERATE A N A L A R M IN D C S 16 44-XZSO9010 INHIBIT TO START THE TURBO-EXPANDER 44-)tZSO-9010 AUTHORISATION TO START THE TURBOEXPANDER 17 INHIBITION OF H - X H S O - M X H WHEN THE 44-C-201 IS RUNNING (44-XS-7620) 18 WITH THE TIME DELAY •= 1 MN. 19 R E S E T FACILITIES T O B E PROVIDED AFTER ACTIVATION OF HAND SWITCHES 20 SHUT OOWN OF EXPANDER WHEN M-XV-9007 IS CLOSED (INTERNAL SIGNAL)

7600L-CEC01 - S P P 1 - R*v.2- A N G - W l 2 3 * 4 0

C. •

Checked by RA JC RA RA RA

Page

PROCESS SPECIFICATION M-yuerK. '

j CEC ADNOC LOCATION HABSHAN

NOTES

UNIT

imm

Made by YS YS

Checked by RA JC

YS

RA

44

siSENERAL NOTES' L e v * 1 coTBsporKts t o * local shut down (•.& punp tnut oown) Level 2 ayrMpontlJ to a systam mul down (e.g. o™4> o* " m i ) or zone s h u (Sown Zone s i u down correspanOs to Units 34 • 44 shul down for zone 20

titOTES21 SIGNAl. WITH START U P OVERRIDE •M-HS-BOBS FOR 44-XZSC-9077 22 SIGNAL WITH START U P OVERRIDE -M-HS^OBT FOR M-XSC-gOCD 23 23 W Z S C - i 5 a \ AND 4+-XZSC-7S01 PERMISSIVE T O O P E N WOCV^OIO 24 444tS-711B AND 4 4 . X Z S O « 1 1 D A N D 4 4 j a S a « X » PERMISSIVE TO START 4 4 E C J 0 1 25 THE ACTION IS POSSIBLE ONLY IF OIL PUMPS HAVE BEEH SHUT DOWN FOR MORE THAN 5 MINUTES ( 4 4 - X M 1 0 5 )

37 ~ 38 39

r

42 43 45 46 ~ 47 48

-

49 50 51 52 S3 54 55 58 57 58 59 60 61 62 63 64 65 66 67 66 76OOL-CEC01 - S P P 1 - R*»-2- ANG - WI23M.0

Page:

1 Bis 19/4«6

'36 •'

-.Rti' . (

76CG_ Z=.Z Date. 2/8/84

CUENT

Sona'N:

FUNCTION PETtfORMED . 4-4H Am DEBUTANP J R REFLUX PUMP W-LV-30S2A

3 FOR CONSTRUCTION DESCRgTlON REV DATE ABU DHABI NATIONAL OIL COMPANY

BY

cmcD

Af.n

REV|

DATE

REISSUED FOR DESIGN REISSUED POR CONSTBUCTION DESCRIPTION DRAWING NO.

BECHTEL TECHNIP

i — ^ j l

J j ^

iSjJi

JOINT VENTURE ONSHORE OAS DEVEUPMENT PROJECT

CAUSE 4 EFPECT CHART

7600L

CEC-44-00-25-001

I REV

1 CLIENT PAGE

EFFECT FUNCTION PRRPORMTO ' -«-C.2flI SHUTPOHW 5TCNAL l "FIRST STAGE SUCTION 44-0301 SECOND STAGE SUCTION 44-0101 DISCHARGE ANTISURGE FIRST STAGE DESUPERHEATING ANTISURGE SECOND STAGE DESUPERHEATINC 44-EOM1 EXPANDER SUCTION. 44-gC-Ml COMPRESSOR DISCHARGE 44-EC.3B1 SEAL GAS 44-EOm S/D SIGNAL REGENERATION GAS TO FUEL WATER TO SOUR WATER STRIPPER SALE GAS FROM HEADER SIGNAL TO UNIT 14

SSSSSSSSSSSSiSSiSSSSSg

144-HV-7W

Z M \ DISCHARGE 4*0401 SUCTION 44-OM1 SUCTION fBYPASS) 44-034! DEPRESSURIZATION ^ 0 1 S/D SIGNAL CONDENSATE TO STORAGE CONDENSATE TO STORAGE CONDENSATE TO FLARE DRUM STEAM CONDENSATE FROM 44-E-4a3 NCL TO STORAGE 44-ME.m-Hl SHUTDOWN SIGNAL 44-P-4D1 Am DEBUTANIZER REFLUX PUMP

ABU DHABI NATIOMAL OIL COMPANY

REISSUED FOR CONSTRUCTION ISSUED FOR DESIGN DESCRIPTION. DRAWING NO.

DRAWING TITLE

BECHTEL TECHNIP CAUSE d EFFECT CHART JOTNT VENTURE ONSHOM CAS DEVELOPMENT PROJeCT

7600L

CEC-44-00-25-001

TRIP

CLOSE

CLOSE CLOSE

STOP

p ir.m

[CLIENT

FUNCTION PERFORMED RgFRlC UQUID FROM **-g-302 j 44-XV-90TT

S TO H R A T E R 44-Ng^iai HI

WATER TO SOUR WA1TR STTUPPER

In g CM'QtAL'nuy

sis

44-t.U I TOTAL SHUTDOWN U-RJ1U404 TOTAL SHUTDOWN U-E;!* 1 TOTAL SHUTDOWN _ U-E-311 TOTAL SHUTDOWN U-E-Wl TOTAL SHUTDOWN

TRIP TRIP

Nl

ABU DHABI NATIONAL OIL COMPANY

ISSUED FOR DESIGN DESCRIPTION DRAWING NO,

DRAWING TITLE

• I C H r r n . TECHNIP CAUSE A EFFECT CHART JOINT VENTURE ONSHORE CAS DEVELOPMENT PROJECT

7600L

CEC-44-00-25-001

BY

CHCD Af.fR

53

mmmmm

mmtm®

mmmmmtmmm

FUNCTION PERFORMED U-C-202 COMPRESSOR

U-E-203 PROPANE OOWOENSgR F W S

_ DEMETHANIZER BUTTOMS PUMP 44-p-302A DEMETHANIZER BUTTOMS PUMP 44.P-302B

_ W - 3 0 B COLD OEUETHANIZER B O n O M S O U U E T

4*£>31B 2ND FEED CHILLER

4AE-tO& DEBUTANIZER TRIM CONDENSER

44E-407 NGL SUBCOOLER

ISSUED FOR CONSTRUCTION NOTES:

FOR

REVISED PER GASCO COMMENTS

LOGIC R E F E R TO TOROMONT C&E.

ISSUED FOR APPROVAL

C O N D E N S E R W . E . 2 0 3 F A N S TRIP F R O M O C S .

DESCRIPTION

SflKO

FIUOR. G A S C O E T H A N E R E C O V E R Y MAXIMIZATION P R O J E C T

C A U S E AND E F F E C T CHART

CEC-44-00-25-001

St!

S

c z 3

3

FUNCTION P E R F O R M E D *j-C-202 C O M P R E S S O R

i:

U-E-203 P R O P A N E C O N D E N S E R FANS

DEMETHAHLZER BUTTOMS PUMP A4-P-302A DEMETHANIZER BUTTOMS PUMP 44-P-303B

44V-30B COLD DEMETHANIZER BOTTOMS OUTLET

I

44E-31B gND FEED CHILLER

I

r

*4E-

60F8

Materials of Construction

Compr. Type

centrifugal

Driver: Motor or turbine

Requistion Esfd Driver Manufacturer kW P&ID 5800

4-0701-01 Toromont 22717-101

Remarks Part of Refrigeration Package 44-ME-201. Spare rotor provided

FLUOR Contract AOWT Date: 22-Mar-04, Rev. 2 By: DTS / OPM / PL CHK: ED

ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 • Unit 44 EQUIPMENT LIST - TANKS Criticality Rev

Item No.

Description

Rating

Diameter

Operating

Design

Inside T/T

Press

Temp

C-202 TK-1

C-202 44- TK-2

Lube Oil Reservoir

Lube Oil Rundown Tank

Equipment List - Unit 44 - Rev 2.xls

Insul.: Ih/lc

Orient.:

Requistion

Hor./Vert.

Manufacturer

2.2 L 1.5 W

1.4 H

ATM.

0.5

1.8

ATM.

317LSS

316L

93

7 OF 8

Remarks

P&ID

barg

m 44-

Press

Materials of Constnjction

Vert.

4-0701-01 Toromont 10512S 4-0701-01 Toromont 16-440-901-526

Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201.

FLUOR Contract AOWT Date: 22-Mar-04, Rev. 2 By: DTS / OPM / PL CHK: E[

ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 - Unit 44 EQUIPMENT LIST - MISCELLANEOUS Requistion

Criticality Rev

Item No.

Description

Duty Specification

Rating

Manufacturer

Remarks

P&ID

44- C-202-X1

44-

C-202GB-202

44- Y-202

Lube Oil Console

C-202 Gearbox

Overhead Travelling Crane

44-

C-202F1 A/B

Lube Oil Filters

44-

C-202F2 A/B

Primary Seal Gas Filters

C-202F3 A/B

Secondary Seal Gas Filters

44-

44-

CM-202CM-202 Motor Air BL1 A/B/C Blowers

Equipment List - Unit 44 - Rev 2.xls

API-614 Lube Oil Console Containing: Lube Oil Reservoir (44-C-202-TK1) Lube Oil Filters (44-C-202-F1A/B) Lube Oil Pumps (44-C-202-P1A/B) Lube Oil Heater (44-C-202-E2A/B) Lube Oil Cooler (44C-202-E1A/B/C) API-613 Gearbox and API-671 Coupling Rated Capacity = 12,000 kg Span = 12 m Lift = 9 m Crane Travel = 44 m Cartridge Type, 10 micron, 316SS elements Design pressure = 16.2 barg Design temperature = 100°C 316 SS construction, 1 micron, glass fiber elements Design pressure = 24 barg Design temperature = -45°C 316 SS construction, 1 micron, glass fiber elements Design pressure = 24 barg Design temperature = -45 C 0

Cooling for CM-202 (TEAAC type). 3 x 10 kW motors.

8 OF 8

4-0701-01 Toromont

Part of Refrigeration Package 44-ME-201.

10512S 4-0701-01 Toromont 4-0801-02 J. Barnsely Cranes 4-0701-01 Toromont 10512S 4-0701-01 Toromont 16-440-938-561

4-0701-01 Toromont 16-440-938-561

Part of Refrigeration Package 44-ME-201. Spare gear set provided. Existing surplus crane (45-Y-101) modified for this new service. This service replaces existing 6T (Y001) crane. Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201.

4-0701-01 Part of Refrigeration Package Toromont 44-ME-201. M68D100087

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

CHAPTER 10

DRAWINGS

CONTENTS

SECTION

("AS-BUILT" DRA WINGS TO BE INSERTED WHEN AVAILABLE)

CHAPTER 10

PAGE

^-393 1ST STAGE LIDUiD FLASH ORUH s.... mm . sua m IT Dtiip

f

x 'S BSW/ Full

FEED CHILLER

1ST STAGE LIOU1D/FEEO EXCHfiWDER

flEFR 1 LiRAliT FLASH DRUH £.» i IESS m m . 4e3a HH II P

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