Post on 01-Feb-2018
transcript
NGL Recovery Project at Badak LNG Plant
byRahmat Safruddin and Abdul Gafar
PT Badak NGLBontang-Indonesia
23rd World Gas Conference5-9 June 2006
Amsterdam – The Netherlands
2
Safety Massage
3
Agenda
• Background and Objective
• Project Scope
• Plant Location
• Material Balance
• Project Staging
• Conclusions
4
East Kalimantan Gas Gathering and Pipeline System
C
F
G
Gas Pipelines
Oil Pipelines
SENIPAH
PECIKO
BEKAPAI
HANDIL
TAMBORA
TUNU
BontangDomestic Plants
LNG Plant
Santan (LEX Plant)
Mah
akamR
iver
Muara Badak (VICO)
57 km
5
Background
East Kalimantan Gas Distribution
LNG Plant
Domestic Plants
BontangKM-57
Chevron Liquid
Extraction (LEX) Plant
VICO
MuaraBadakKM-0 Santan
From TotalIndonesie
Rich Gas1109.2 btu/scf
Lean Gas1017 btu/scf
300 mmscfd
KM-53
3,320 mmscfd
150 mmscfd
6
Background
Domestic Plants
• Fertilizer Plant: 4 Trains• Ammonia Plants: 2 Plants• Methanol Plant• Gas delivery Contract: 457,055 mmbtu/d• Supplied by 2 x 16”, 20” rich gas, and 16” lean gas p ipelines
Badak LNG Plant
• Train Number: 8 (A-H)• Production Capability: 22.1 mtpa LNG, 1 mtpa LPG, 10 million
bbl/yr condensate• Supplied by 2 x 36” and 2 x 42” gas pipelines
7
Feed Gas Condition
Background
950−12001109.2HHV
0.437C6+
0.167nC5
0.261iC5
0.823nC4
0 − 50.718iC4
0 − 83.482C3
0 − 125.215C2
70 − 9983.285C1
5.528CO20 − 9
0.084N2
Domestic Contract
From Pipeline
Component
• Pressure: 35-40 kg/cm 2g• Temp : 27-32 oC
Background
Composition (Vol%)
• Pressure: 45-47 kg/cm 2g• Temp : 27-32 oC
To LNG Plant
To Domestic Plants
HHV in BTU/SCF
8
Current Situations
• Feed Gas price to Domestic Plants is cheap
• Domestic Plants require primarily methane
• Price of heavier HC components is higher than metha ne
• Condensed hydrocarbon in pipeline transmission to D omestic Plants is flared
• Part of LPG Component is recombined with LNG to mai ntain LNG heating value (LPG price is higher than LNG pri ce)
• So, supplying lean gas instead of rich gas to Domes tic Plants will benefit from:
replacing LPG component in LNG with C2recovering LPG & Condensate from rich gaseliminating flared condensed HC
Background
9
LNG Plant Process Overview
FEED GAS
K.O.D.
CO2
LNG
MARINE LOADING
MARINE LOADING
FRACTIONATION
C5+
BOIL OFF TOPLANT FUEL
PROPANEREFRIGERATION
M C RREFRIGERATION
DEETHANIZERDEPROPANIZERDEBUTANIZER
LNGSTORAGE
LPG
LPGSTORAGE
CO2 REMOVAL
(ABSORBER & REGENERATOR)
DEHYDRATION FRACTIONATION LIQUEFACTION(MCHE) STORAGE TANK(SCRUB COLUMN)(H2O & Hg REMOVAL)
4KT-1 4KT-2 4KT-3
4E-54E-6
4E-124E-10
4E-14
Background
LPG
10
• To recover 99.2% of ethane and 100% components heavie r than ethane from pipeline rich gas delivered to Domest ic Plants
• To eliminate the flared condensed hydrocarbon in pipel ine to Domestic Plant
Objective
NGL Recovery Ethane Plus Extraction Plant (EPEP) Project
11
CO2 Removal Unit Dehydration
Propane Refrigeration Unit LPG Product Refrigeration
LNG Plant
StorageTanks
EPEP Project Scope
C5+
Pipeline Distribution System
C2Vapor
EPEP Plant Utility
To DomesticPlants
Turboexpander + Fractionation Unit
KOD
Project Scope
C3C4
Field
StabilizerResidue Gas (C1)
ExistingKM-53
12
Turboexpander Unit
Project Scope
C2 Product
Residue GasExport
Fuel
NGL Product
PretreatmentUnit
Raw Gas From Pipeline
Recycle Compressor
Residue Gas Compressor
Demethanizer
De-ethanizer
Booster Compressor
Expander
Ethane Compressor
TURBO EXPANDER TECHNOLOGY FOR
ETHANE PLUS EXTRACTION PROJECT
-106oC19 kg/cm 2
13
EPEP Plant Characteristics
• High NGL recovery: 99.2% of C2 and 100% of other heavier HC components
• Highly Energy-efficient plant: fuel consumption 4.2% of its feed (Plant thermal efficiency of 95.8%)
Project Scope
14
EPEP Plant Utilities
• Hot Oil: 5,000 m 3/h, WHRU Preheater + Furnace
• Electricity: Gas Turbine Generator, 3 x 50%
• Air : Instrument, Utility (compressor 3 x 100%)
• Nitrogen: Cryogenic and PSA Units (2 x 100%)
• Fuel Gas: High, Medium and Low Pressures
• Wastewater Treatment
• Smokeless Flares and Blowdown: LTCS, LTSS, Wet Flar es, Liquid Drain Collection and burnpit
• Water Storage ( supplied from LNG Plant ) : Amine water makeup, Potable, Utility & Fire Suppression Water S ystem
• Air cooling system
Project Scope
15
R 1,830m
R 3,354m
R 1830m
Conical
zone
SWL 38m
Location
Condensate
stab unit
16
Before EPEP Project
LEX PLANT LEAN GAS 150 MMSCFDHHV 1,017.0 BTU/SCF
DELIVERY CONTRACT
FEED GAS 457,055 MMBTU/D
DISTRIBUTION 275 MMSCFDPRODUCTS :
LNG 365 std cargoes
LPG C3 500,657 tons/year
FROM FIELD 3,595 MMSCFD 3,320 MMSCFD LPG C4 477,006 tons/year
HHV 1,109.2 BTU/SCF CONDENSATE 10,849,417 bbl/year
BADAK LNGPLANT
DOMESTICPLANTS
Material Balance
1 LNG std cargo = 125,000 m 3
17
After EPEP Project
Material Balance
LEX PLANT LEAN GAS 150 MMSCFDHHV 1,017.0 BTU/SCF
DELIVERY CONTRACT
457,055 MMBTU/DRESIDUE 304 MMSCFD
HHV 1,000.3 BTU/SCFNGL RECOVERIES :
FEED GAS C2 261,285 tons/year
DISTRIBUTION C3 257,901 tons/yearC4 150,444 tons/year
TO EPEP 385 MMSCFD i-C5+ 1,043,683 bbl/year
(Addition 110 MMSCFD)
PRODUCTS : Net GainLNG 4.37 std cargoes
FROM FIELD 3,705 MMSCFD 3,320 MMSCFD LPG C3 257,901 tons/year
HHV 1,109.2 BTU/SCF LPG C4 150,444 tons/year
CONDENSATE 1,043,683 bbl/year
BADAK LNGPLANT
DOMESTICPLANTS
EPEPPLANT
110 mmscfd additional rich gas to EPEP Plant is req uired for• Makeup for energy shrinkage : 94 mmscfd• EPEP Fuel consumption : 16 mmscfd (4.2% of EPEP Feed)
18
Project Staging
Feb’06
Sep'06Dec'07
EPC
FEED TenderEPC Tender
May’05
Aug ‘05
FEEDJun'06
Prep’n
19
Conclusions
• EPEP Plant will be capable of recovering 99.2% of C 2 and 100% of heavier HC components from rich gas by Turbo-exp ander technology
• EPEP Project will gain additional production up to 4.4 std cargoes LNG, 0.4 mtpa LPG and 1 M bbl condensate by NGL recovery from rich gas delivered to Domestic Plants
• EPEP Plant is energy efficient with fuel consumptio n of 4.2% from its feed
• EPEP Plant will require 110 mmscfd additional gas su pply for residue gas energy shrinkage and plant fuel consump tion
20
Thank You