DRL Tools

DRL Toolbox & Templates

Example Functional Basis

TABLE OF CONTENTS 1 GENERAL ....................................................................................................................... 5

1.1 PURPOSE OF DOCUMENT ................................................................................ 5 1.2 AREA OVERVIEW ............................................................................................... 5

1.2.1 PASCA Field ........................................................................................ 5 2 CONCEPT STUDY OBJECTIVES................................................................................... 6

2.1 PASCA DEVELOPMENT OBJECTIVES .............................................................. 6 3 SITE DATA ..................................................................................................................... 6

3.1 APPROXIMATE DISTANCES AND WATER DEPTHS ........................................ 6 3.2 GENERAL METEOROLOGY ............................................................................... 6

3.2.1 General Meteorology ............................................................................ 6 3.2.2 EQUATORIAL TROUGH ...................................................................... 7 3.2.3 TROPICAL CYCLONES ....................................................................... 7

3.3 METOCEAN DATA .............................................................................................. 7 3.3.1 Survey Area .......................................................................................... 7 3.3.2 Assumptions ......................................................................................... 7 3.3.3 Ambient CLIMATOLOGICAL Conditions .............................................. 8 3.3.4 Rainfall ................................................................................................. 8 3.3.5 Solar radiation ...................................................................................... 9 3.3.6 wind, wave and current conditions ...................................................... 10

3.4 BATHYMETRY .................................................................................................. 11 3.5 GEOTECHNICAL ............................................................................................... 12

4 RESERVOIR WELL FLUID DATA ................................................................................ 13 4.1 SEPARATOR TEST ........................................................................................... 13 4.2 BINARY INTERACTION PARAMETERS ........................................................... 14 4.3 FLUID COMPOSITION ...................................................................................... 15 4.4 PHASE ENVELOPE........................................................................................... 16 4.5 RESERVOIR PROPERTIES .............................................................................. 17 4.6 RESERVOIR DEPLETION AND SUPPORT MECHANISM ................................ 17 4.7 RECOVERABLE RESERVES ESTIMATE ......................................................... 17 4.8 WELL LOCATIONS ........................................................................................... 17 4.9 WELL DATA & DELIVERABILITY ...................................................................... 17 4.10 FLOW ASSURANCE ......................................................................................... 18

5 PRODUCTION TARGETS ............................................................................................ 18 5.1 FIRST GAS AND PROJECT LIFE ...................................................................... 18 5.2 GAS PRODUCTION .......................................................................................... 18

5.2.1 Corrosivity .......................................................................................... 18 5.2.2 condensate & lpg sales specifications ................................................ 19

6 OTHER REQUIREMENTS ............................................................................................ 19 6.1 DRILLING REQUIREMENTS ............................................................................. 19 6.2 PRODUCTION AVAILABILITY REQS AND CONTRACT OBLIGATIONS .......... 19 6.3 FACILITY RELIABILITY ..................................................................................... 19 6.4 OPERATIONS PHILOSOPHY (HUC, SIMOPS) ................................................. 19 6.5 CONTINUOUS FLARING .................................................................................. 19 6.6 FUTURE FACILITIES / DEVELOPMENTS – GAS EXPORT .............................. 19 6.7 INFRASTRUCTURE AVAILABLE ...................................................................... 19 6.8 OFFTAKES. ....................................................................................................... 19

REFERENCES ......................................................................................................................... 20

Fluid Characterization

Lab Test Data

Fluid Characterisation

PFD - Overall

PFD – Sectional

PFD – Control

Process Flow Schematic

Equipment List

106 8060 : LIVING QUARTERS - HD & SHOP107 LIVING QUARTERS & HD A-8010 TBA TBA 10 430.0 500.0 175.0 24 / 32 MAN Cost included separately108 TELECOMS $250,000 109 TRASH COMPACTOR 1.0 4.0 $50,000 110 WAREHOUSE / SHOP 9,000 9,000 11,000 25.000 40.000 Bi Level $500,000 111 XXX : GAS COMPRESSOR GT SKID 14,300.0 2,900.0 65.00 25 T70 2 Stage Compressor Set Solar $9,000,000

112 XXX : GAS COMPRESSOR GT SKID 14,300.0 2,900.0 65.00 25 Solar $9,000,000 113

114 XXX : GAS COOLER / SCRUBBER SKID 14,300.0 6,000.0 70.00 80 $4,000,000

115 XXX : GAS COOLER / SCRUBBER SKID 14,300.0 6,000.0 70.00 80 $4,000,000

Phase 1 & 2 $55,350,363 WP DRL

EQUIPMENT DRY WEIGHT 1,401 936 $59,141 1,312.000 LQ DRY WEIGHT 800 430 $ per Tonne

20.0% FLARE BOOM WEIGHT 961,574 TOTAL 2,297 1,366

ABSORBED POWER

TOTAL ABSORBED POWER

Contingency

HYSYS – Heat & Material Balance

HYSYS – Utility Balance

Cooling Water Summ ary

Equipment Design Case Supply Return FlowNo Duty Temp. Temp.

kW C C BPD

23-HG-1320 3852 130.3 45 2274823-HG-2320 3852 130.3 45 2274823-HG-1340 3054 125.2 45 1803323-HG-2340 3054 125.2 45 1803323-HG-1430 1576 114.2 45 930423-HG-2430 1576 114.2 45 930423-HG-1450 1153 105.9 60 680923-HG-2450 1153 105.9 60 6809

19270 113788

19270 113788

Sea Water Sum mary

40-HG-1610 9701 32.03 52.36 59269Sea Water Cross Exchanger B 40-HG-1620 9701 32.03 52.36 59269

19402 118538

Total

Sea Water Cross Exchanger A

Total

Process Coolers

1st Stage Booster Compressor Discharge Cooler (Train 1)1st Stage Booster Compressor Discharge Cooler (Train 2)2nd Stage Booster Compressor Discharge Cooler (Train 1)

Sub-total

2nd Stage Booster Compressor Discharge Cooler (Train 2)1st Stage Gaslif t Compressor Discharge Cooler (Train 1)1st Stage Gaslif t Compressor Discharge Cooler (Train 2)2nd Stage Gaslif t Compressor Discharge Cooler (Train 1)2nd Stage Gaslif t Compressor Discharge Cooler (Train 2)

Fuel Gas System

1 Generators

2011 hpRunning 2 (2 x 50 %) Total Load 4022 hpHeat Rate 9116 BTU/hp-hFuel Gas LHV 1300 BTU/scf

0.68 MMscfd

2 Main Gas (Booster) Compressors

Load each 6543 hpRunning 2 (2 x 50 %) Total Load 13086 hpHeat Rate 7205 BTU/hp-hFuel Gas LHV 1300 BTU/scf

1.74 MMscfd

3 Gas Lift Compressors

Load each 2805 hpRunning 2 (2 x 50 %) Total Load 5610 hpHeat Rate 9125 BTU/hp-hFuel Gas LHV 1300 BTU/scf

0.95 MMscfd

4 Sea Water Injection

Load each 2042 hpRunning 1 (1 x 100 %) Total Load 2042 hpHeat Rate 9125 BTU/hp-hFuel Gas LHV 1300 BTU/scf

0.34 MMscfd

5 Gas Stripping 9 scf/bbl, MMscfd 0.7 MMscfd6 Miscellaneous Consumption, MMscfd 1 MMscfd

5.41 MMscfd

Notes1. Design Case: 25,000 BOPD, 80,000 BWPD, 60 MMscfd Gas Lift & 1600 G

Fuel Consumption

Fuel Consumption

(3 - Centaur 40, 4,692 hp - ISO)Load each

Fuel Consumption

(2- Taurus 70, 10,912 hp - ISO)

Total Fuel gas Consumption

(2- Centaur 40, 4692 hp - ISO)

Fuel Consumption

(2- Centaur 40, 4692 hp - ISO)

12

Dynamic Simulation

• Dynamic Simulation

13

Dynamic Simulation

• Dynamic Simulation

14

Flow Assurance Studies

• ProjectsFluid Characterization & Flow Assurance

15

Flow Assurance Studies

• ProjectsHydraulic & Corrosion Study

Equipment Sizing Basis

MP Separator (411-V-01) A 24-Oct-12

Quantity 1x100%Configuration 2-Phase VerticalDesign Condition

Pressure psig 943/FV bar 65/FVTemperature ºF 149 ºC 65Liquid Retention Time min 2Total Liquid Flow blpd 7,000Gas Flow MMscfd 447.00Condensate Flow bopd 800Max Water Flow bw pd 6,200Normal Operation Level in 36 mm 914.4Surge Factor % 20Maximum Liquid Carryover gal/MMscf 0.1Recovery of 50 micron droplets % 99

Operation ConditionPressure psig 290 bar 20.0Temperature ºF 104.0 ºC 40.3

Notes:1. High CO2 Case

Main Compressor A 24-Oct -12Booster Compressor (413-C-01/ 02/ 03)Export Gas Compressor (462-C-01/ 02/ 03)

Quantity 3 x 50% Configuration Gas Turbine Driven 2-Stage CentrifugalDesign Condition Booster Compressor Export Gas

Gas Flow rate (ea) MMscfd 227.00 215.00Surge Factor % 0 0

Operation ConditionSuction Pressure psig 261 715 bar 18.0Discharge Pressure psig 798 1944 bar 55.0Suction Temperature ºF 88.0 91.0 ºC 31.4Discharge Temperature ºF 258.0 252.0 ºC 125.9BHP (ea) hp 15940 12800 MW 11.9

Total hp 28740 Total MW 21.4Notes1) LM2500+ gas-turbine driver

Project: Talisman KNDPALocation: Offshore Pennisular MalaysiaClient: TalismanDoc No.: KNDP-DRL-CP-PR-PHI-0007Author: KAP / TRRRev. No.: A Date 24-Oct-12

Value Comments Rev Date

KNDP-DRL-CP-PR-PHI-0007 PROCESS REQUIREMENTS OF EQUIPMENT

AND SYSTEMS

TITLE: PROCESS REQUIREMENTS OF EQUIPMENT AND SYSTEMS

Systems / Equipment

API 14C Compliance

Process Line Sizing Report

9. THE PROCESS DATA CAN BE CREATED BY XXX/XXX. ASK XXX FOR DETAILS.10. FOR QUESTION OR SUGGESTION, PLEASE CALL XXX @ XXX.

8. THE LIQUID PHASE MIXING (EMULSION) RULE FOR VISCOSITY IS REFERENCING TO HYSYS OPERATION MANUAL, NOT IN API OR GPSA.

7. PIPE PRESSURE DROP DUE TO FRICTION FOR TWO-PHASE FLOW IS ESTIMATED USING THE FOLLOWING EQUATION AS SUGGESTED BY API 14E:

used. is viscositymixture gas/liquid edbut weight phase single in the as method same using calculatedfactor friction Moody ;lbm/ft pressure, and re temperatuflowingat density mixture Gas/liquid

inch; diameter, internal Pipelbm/hr; rate, flow liquid) (gas fluid Total

psi/100ft; drop, Pressure:

000336.0

3

2

m

m

in

min

m

f

dW

Pwhere

dWfP

cp. phase, Aqueous of viscosity phase oilfraction volume cp; phase, oil of viscosity

cp; mixture, oil/water of viscosity apparent :where

Equations. wobetween t average weighteda using calculated is phase liquid combinedfor viscosityeffective the0.5, and 0.33between is phase oil theof volume theIf

)33.0()4.0

(25.01

)5.0(

H2O

oil

2

22

)1(6.3

oil

eff

oilohoil

ohoiloiloheff

oilv

oileff

v

vforv

vfore oil

Pump SizingPump Calculation Sheet

Input values required: blue numbers. Calculated values: black numbers

Item no.: P-3001 No. of: Type:Service: LPG pumps Case: NPSHA calc.

F Fluid LPG NL Fluid Temperature 37 deg.C OU TI (1) Density (@ T & P) 800 kg/m3 ED Viscosity (@ T & P) 0.12 cP S

(2) Normal Flowrate 120 m3/h(3) Design Flowrate Note1 120 m3/h

S (4) Normal pressure 10.00 barg D (12) Termination Pressure 17.00 bargU (5) Set Pressure Note 1 15.00 barg IC S (13) Static Head 0.0 m = 0.00 baraT (6) Vapour pressure 4.01 bara C (14) Loss, Pipe & Fittings 1.60 baraI (7) Static Head 10.0 m = 0.78 bar H (15) Loss, Other 3.10 baraO (8) Max. Static Head Not 12.0 m = 0.94 bar AN R

(9) Line Loss 0.30 bar G(10) Loss, Equipment 1.50 bar E(11) Loss, Other/Fittings 1.00 bar (16) Pump Shut-in Diff.Pressure Note1 15.00 bara

(17) Pump Suction Pressure = (4)+(7)-(9)-(10)-(11) 7.98 bargP (18) Pump Discharge Pressure = (12)+(13)+(14)+(15) 21.70 bargU (19) Pump Differential Pressure = (18)-(17) 13.72 barMP Maximum Discharge Press. = (5)+(8)+(16) 30.94 barg

NPSHA= [(17)-(6)+1 ATM]*100000/[(1)*9,81] 63.52 m

(20) Hydraulic Power = (19)*(3) / 36 45.7 kW(21) Estimated Efficiency 80 %

Estimated Power = (20) / (21) 57.1 kW

Note1: Optional input for calculation of maximum discharge pressure and estimated power consumption.

SYSTEM SKETCH

P2Reference point 2

Hst2P1 Reference point 1

Hst1 Hf2

Hf1

Psuction P1-Hst1-HfPdischarge P2+Hst2+Hf2

P1 normal operating pressure upstream pumpHst1 height difference between reference point 1 and pump suction Hf1 friction loss upstream pumpPsuction pump suction pressure

P2 termination pressureHst2 height difference between reference point 2 and pump discharge Hf2 friction loss downstream pumpPdischarge pump discharge pressure

Prelim Compressor Sizing Gas Compressor

150 Total gas1 no. of compressors

UNITS NAME Case 1Capacity

Gas Flow MMSCFD MSCF 150.00 Input from process data sheet.Mass Flow lb/min m 5,461.73 Check calc. with process data sheet.

kg/h 148,618 Calculate for each sectionGas Properties

molecular Weight MW 19.90Specific Heat Ratio k 1.464 Use Cp/Cv from Gas Analysis

Compressibility z 0.838 Use avg. Z from Gas Analysis

Inlet ConditionsSuction Pressure psia P1 435.0 Allow interstage pressure drop.

Suction Temperature °F T1 113.0 Use Cooler Outlet Temp. in °FSuction Specific Volume cu.ft./lb V1 0.60

Actual Volume Flow ACFM Q1 3,251 ACFM selects casing frame size.Actual Volume Flow Nm3/h 5,526 ACFM selects casing frame size.

Discharge ConditionsDischarge Pressure psia P2 1,815.0 Input in psia.

Discharge Temperature °F T2 549.1 If T2 > 350 °F Use Intercooler.Discharge Specific Volume cu.ft./lb V2 0.25

Discharge Volume Flow ACFM Q2 1,372Stage Parameters

Pressure Ratio PR 4.17Polytropic Efficiency % EP 80.0% Input from flow coefficient chart.

Polytropic Head ft pH 71,618Power Requirements

Brake Horsepower bhp BHP 14,817 Without recirc., gear & bearing lossBrake Horsepower bkW kW 11,053 Without recirc., gear & bearing lossDriver Horsepower hp HP 15,261 BHP + 3% gearloss + 0% margin

Driver Kilowatts KW 11,385Driver Megawatts mW 11

Design Analysis mW 14 with 25% allowance

3/7/2013

REMARKS

Separator SizingLP SEPARATOR 20-VA-1001

Horizontal Separator Data Sheet INPUTSwith Demister Pad OUTPUT III. New Capacities:

I. Vessel Conditions : Case ONE Case TWO Case THREEHLLSD sw itch (from bott. of vessel) 97.6 in. 102.4 in. 107.2 in.

Vessel Length S/S: 35 ft. Use 0.9 for Cyclonics NLL to HLLSD Surge Capacity: 104 BBl 114 BBl 125 BBlEstimated K value (using EXX Nominal Vapor Capacity: 150.6 MMSCFD 165.8 MMSCFD 181.7Specs. GSC-5-21 iss. 7/94 {pg.10/13}) Nominal Total Liq. Capacity: 101049 BPD 111232 BPD 121905User K value override: 0.9 ft/secK Value being used in calcs. 0.9000 ft/sec IV. Sizing ParametersCritical Velocity: 12.081 ft/sec Chosen Internal Diameter: 122.0 in.Gas Over Design Factor: 1.1 <---e.g. entry '1.1' means 10% safety factor Chosen Liquid Height 73.2 in.Calculated Design Velocity: 10.873 ft/sec Nominal Total Liq. Capacity: 101049BPD

Min. Liquid Residence time, min 4 min. Vessel Length 35 ft.Est. Liquid Level (% Diameter) 60.00% Slenderness Ratio: 3.44

Shell thickness 1.000 in.II. Pre-sizing Calcs. : User Override Shell thickness

Nozzle Weight Multiplier 1.25 stdMin. I. D. if liquid controlled 117.2 in. Estimated Weight (empty) 65248 lb.Min. I. D. if gas controlled 108.4 in. Estimated Weight (operating) 170947 lb.

Two Phase Separators: Case ONE Case TWO Case THREE Vessel Design SummaryDesired Internal Diameter of Vessel: 122.00 in. 128 in. 134 in. V. Rates & Parameters:Liquid Height: 73.2 in. 76.8 in. 80.4 in. Conditions Flow RatesCross-sectional area occ. by liquid 50.8 ft² 56.0 ft² 61.3 ft² Operating Pressure: 72.519 psig Vapor 119.1 MMSCF/DTotal Crossectional Area: 81.2 ft² 89.3 ft² 97.9 ft² Operating Temp. 134.6 °F Oil/Condensate 25126 BPDCross-sectional area occupied by gas 30.32 ft² 33.38 ft² 36.58 ft² Gas Viscosity: 0.012 cP Water/Heavy 80272 BPDRequired Effective length 3.2 ft. 3.1 ft. 2.9 ft.Liquid Containment (BBL) : 316.9 348.8 382.3 Design Properties Nozzle DiametersActual Retention Time: 4.3 min. 4.8 min. 5.2 min. Design Pressure: 217.557 psig Inlet Diameter 34 in.Shell Thickness 1.000 in. 1.000 in. 1.000 in. Design Temp. 200 ° F Vapor Outlet 30 in.Vapor Velocity: (f t/sec) 8.59 7.81 7.12 Corrosion Allowance .118 in. Oil/Condensate 6 in.

Design Tensile Stress: 17500 psi Water/Heavy 10 in.Three Phase Separators:Water Level (% of diameter) 40.00% Oil Section (w eir to outlet-seam) 4 ft. Vessel Summary

Oil section, percent of diam. full: 20.0%Case ONE Case TWO Case THREE Internal Diameter 122.0 in. <4.5m MAX 3.098806 m

Weir Height, (f rom bottom of tank) 73.2 in. 76.8 in. 80.4 in. Shell thickness 1.000 in. < 6 in MAX 25.4 mmInlet Section Residence time 3.8 min. 4.2 min. 4.6 min. Vessel Length 35 ft. 10.67073 mWater Height: 48.8 in. 51.2 in. 53.6 in. Estimated Weight (empty) 65248 lb. < 100 T MAX 29.5911 mTCross-sectional area occ. by w ater 30.3 ft² 33.4 ft² 36.6 ft² Estimated Weight (operating) 170947 lb. 77.52684 mTWater Containment: 167 BBL 184 BBL 202 BBLWater Retention time 3.0 min. 3.3 min. 3.6 min. Comments:Cross-sectional area occ. by oil 20.5 ft² 22.6 ft² 24.8 ft²Oil Containment (BBL): 116.3 128.0 140.3Oil Retention time 6.7 min. 7.3 min. 8.0 min.Total Liq. Retention time 3.9 min. 4.3 min. 4.7 min.

0.53 ft/sec-EXX Specs. use K=0.67*(L/20).5 for scrubbers, and K=0.4*(L/20).5 for separators.

Example Separator

LP Separator 3-Phase Conversion

Sand Flush SystemSettled sand/solids will flushedtowards the PW outlet and separated byinline desanding system

Perforated BafflesReduce turbulence and set upeven liquid velocity profile

New PW outlet nozzle

Vane TypeInlet Device

Oil Outlet(existing)

Vane TypeDemister

New Weir

Scrubber Sizing23-VG-1310/23101ST STAGE SUCTION SCRUBBER A/B

Vertical Separator Data Sheet INPUTS Vessel Design SummaryI. Vessel Conditions: with Demister Pad OUTPUT IV. Liquid Capacity (For Specified Vessel)

Nom. Liquid Capacity 0 BPD I. Rates & Parameters:Calculated K value (using Max. Liquid Capacity 4079 BPD Conditions Flow Rates GPSA Ch.7 pg.7-7, fig. 7-9) Min. Liquid Capacity: 0 BPD Operating Pressure: 68.17 psig Vapor 59.7 MMSCF/DUser K value override: 0.9 Use 0.9 for Cyclonics Slug Capacity: 2.8 Barrels Operating Temp. 134.42 °F Oil/Condensate 0 BPDK value being used in calc.: 0.9 Actual Retention time: #DIV/0! min. Gas Viscosity: 0.012 cP Water/Heavy 0 BPDCritical Velocity: 10.8876 ft/secGas Over Design Factor: 1.13 (e.g. entry '1.1'=10% safety facto r) Design Properties Nozzle DiametersCalculated Design Velocity: 9.472 ft/sec Design Pressure: 261.07 Psig Inlet Diameter 22.0 in.Liquid Retention Time recomm. 1.00 min. Typical Retention Times: V. Max. Gas Capacity (For specified Vessel) Design Temp. 200 °F Vapor Outlet 22.0 in.User override: 1 min. Oil Gravities Minutes New Vapor Velocity 8.641 ft/sec Corrosion Allowance .118 in. Oil/Condensate 2.0 in.Liquid Retention Time used: 1.00 min. above 35° API 1 Critical>Nominal? YES Design Tensile Stress: 17500 Psig Water/Heavy 2.0 in.

20-30° API 1 to 2 Max Vapor 65.414 MMSCFD10-20° API 2 to 4 Vessel Summary

II. Pre-Sizing Calcs. VI. Vessel Summary Inside Diameter 54.0 in.A) Min. Dimensions (in.): Shell thickness, inches .625 in.

Min. demister pad clearance 12 Inlet Nozzle to HLL 23 23 Inside Diameter 54.0 in. 1.371599 m Calc. Vertical Dimensions (in.)Demister Pad thickness 6 HLL to NLL 12 Shell thickness, inches .625 in. <=== rounded up to nearest 1/8 inch. 1) Minimum Extractor Clearance- 11.3 in.

Demister Pad to Inlet Nozzle 36 35 User Override Shell thickness 2) Demister Pad thickness 6.0 in.Calc. Vertical Dimensions (in.) 3) Inlet Nozzle to Demister Pad 36.0 in.

B) Min. Vessel Internal Diameter: 51.57 in. --------------------> 54 rounded to nearest half-foo t 1) Minimum Extractor Clearance- 11.3 in. 4) Inlet Nozzle Diameter 22.0 in.C) Vessel Height, est. using LRT: 111 in. using an I.D.= 30 2) Demister Pad thickness 6.0 in. Cyclone has greater thickness 5) Above NLL 23.0 in.D) Vessel Height, est. using LRT: 111 in. using an I.D.= 36 3) Inlet Nozzle to Demister Pad 36.0 in. 6) NLL to HLL 12.0 in.E) Vessel Height, est. using LRT: 111 in. using an I.D.= 42 4) Inlet Nozzle Diameter 22.0 in. 7) Liquid Retention, in, 12.0 in.

5) Inlet Nozzle to HLL 23.0 in. Total Vessel Height: 10 ft.III. Final Dimensions, inches. 6) NLL to HLL 12.0 in. Nozzle Weight Multiplier: 1.25

7) Liquid Retention, in, 12.0 in. Weight Estimation: 5630 lbs.Desired I.D.(in.) 54 User Overrides (in.) 55.12 m->in Total Vessel Height: 10.2 ft. 3.106765 ft->mMinimum extractor clearance: 11.3 in. ------------- User Override Vessel Height: 10.2 ft. 10.82677 m-> ft (Genesis)Demister Pad thickness- 6.0 in. ------------- Nozzle Weight Multiplier: 1.25 stdInlet to Demister Pad: 36.0 in. ------------- 36 Weight Estimation: 5630 lb. 2.553357 lb->TonneInlet Nozzle Daimeter- 22.0 in. 2.2 Tonne (Genesis)Inlet Nozzle to HLL 23.0 in. -------------NLL to HLL 12.0 in. -------------LLL to NLL 12Liquid Height .0 in. -------------

Total Height: 110.3 in. Comments:Slenderness Ratio: 2.04 (GPSA and API recommend ratio be betw een 3-5)

*Chart data taken from API 12-J spec. fo r Oil & Gas Separato rs, pg. 14 section C.1.7*

0.35

Genesis D: 1.4m = 55.12 in. Minimum calculated D: 54 in. Genesis H = 3.3m, Calc H = 3.1m. Genesis wt = 2.2 Tonnes. Calc wt = 2.5 Tonnes.

Flare Drum Sizing (Horizontal)Equipment: CLO SED DRAIN/LP FLARE KO DRUM (Horizontal) Equipment ID: 43-VD-1730Client: TML By: DanialProject: KNDP B O ption 1A Date : 29/4/2013Project No.: XXX

HORIZONTAL SCRUBBER SIZING CALCULATION(Based on API RP 521) Vessel Design Summary

Case2:Peak Rate to FlareINPUT DATA: INTERMEDIATE VALUES: I. Rates & Parameters:

Conditions Flow RatesOperating Temperature (°F) 135 Operating Temperature (°R) 595 Operating Pressure: 30 psig Vapor 5 MMSCF/DOperating Pressure (psig) 30 Operating Pressure (psia) 44.7 Operating Temp. 135 °F Oil/Condensate 18000 BPDDroplet Diameter (microns) (API521: 400 - 600) 600 Particle Diameter (ft) 0.001968 Gas Viscosity: 0.012 cP Water/Heavy 54000 BPDLiquid Specific Gravity 0.7238 Liquid Density (lbs/ft3) 45.2Gas Molecular Weight 23.12 Gas Density (lbs/ft3) 0.1651 Design Properties Nozzle DiametersGas Compressibility Factor (z) 0.9803 C(Re)^2 3.74E+04 Design Pressure: 50 Psig Inlet Diameter 18.0 in.Design Gas Flowrate (mmscfd) 5 Gas Flowrate (acfs) 21 Design Temp. 200 °F Vapor Outlet 10.0 in.Gas Viscosity (cP) 0.012 Corrosion Allowance 0.11811 in Oil/Condensate 6.0 in.Vessel Max Operating Level (% full) 70 Design Tensile Stress: 17500 Psig Water/Heavy 10.0 in.Vessel Inner Diameter (ft) 5 shouldbe 5 1.524 m <12

Vessel SummaryRESULTS:

Internal Diameter 60.0 in. <4.5m MAX 1.524003 mDrag Coefficient (refer to API521, Fig20) 0.70 ( for C(Re)^2= 3.74E+04 ) Shell thickness .250 in. < 6 in MAX 6.35 mmDropout Velocity (ft/sec) 5.71 Vessel Length 15 ft. 4.573171 mLiquid Dropout Time (sec) 0.26 Estimated Weight (empty) 3507 lb. < 100 T MAX 1.590692 mTZc 0.30 Estimated Weight (operating) 14298 lb. 6.484158 mT 1.98F(Zc) [Vapor Section Area Fraction] 0.252 Comments:Cross secional area for gas flow (sq ft) 4.94Velocity of vapor (ft/sec) 4.32Minimum Required length of vessel by liquid droping(ft) 1.13

OVERALL VESSEL DIMENSIONS SELECTED:

60 " I.D x 15 ' S/S (Length)in ft

SLUG HANDLING: 3 < L/D < 6 L/D = 3Normal Operation Liquid Level (%) 30 stdRequired Slug Handling (bbl) 50 1.16F(Zc) [Normal Liquid Section Area Fraction] 0.252Normal Operation Liquid Volume (ft3) 74 (bbl) 13Max Operation level (%) 70Max Operarion Liquid Volume (bbl) 39Slug Handling (bbl) 26

Genesis D: 2.4 m = 7.9 ft. Minimum calculated D: 5 ft = 1.53 m. Genesis L = 7.2m (23.6 ft), Calc L = 4.6m (15 ft). Genesis wt (dry) = 6.7 Tonnes. Calc wt = 1.6 Tonnes.

Tag No.Service (Vertical)

1. Operation Condition Case1

Vessel Design SummaryGas Flow rate MMscfd 120Operation Pressure psig 50 I. Rates & Parameters:Operation Temp F 135 Conditions Flow RatesGas Z 0.9803 Operating Pressure: 73 psig Vapor 120 MMSCF/DGas S.G 0.797241379 Operating Temp. 135 °F Oil/Condensate 25126 BPDGas Viscosity cP 0.0120 A Gas Viscosity: 0.012 cP Water/Heavy 80272 BPDLiquid S.G 0.7238Liquid Slug Size BBL 76 Design Properties Nozzle Diameters

Design Pressure: 145 Psig Inlet Diameter 34.0 in. Design Temp. 200 °F Vapor Outlet 30.0 in.

ACFM 21287 Corrosion Allowance .118 in. Oil/Condensate 6.0 in.Gas Density lb/f t3 0.24 Design Tensile Stress: 17500 Psig Water/Heavy 10.0 in.Liquid Density lb/f t3 45.14 H

Vessel Summary 2.8448 m

110 k BPD @ 1 min bpd = 110,000 Inside Diameter 112.0 in. 9.333333 ftmin = 1 Shell thickness, inches .625 in.bbl = 76.38888889 Calc. Vertical Dimensions (in.)

1) Minimum Extractor Clearance- 29.0 in.3. Gravity Separation 2) Demister Pad thickness 6.0 in.

3) Inlet Nozzle to Demister Pad 36.0 in.Dp, Particle Diameter Microns 600 4) Inlet Nozzle Diameter 34.0 in.C(Re)^2 5.38E+04 5) Above NLL 29.0 in.C, From Fig.7-3 of GPSA 0.59 6) NLL to HLL 12.0 in.V, Critical gas velocity ft/s 5.20 7) Liquid Retention, in, 12.0 in.A, Vessel Cross Area ft2 68.28 Total Vessel Height: 14.0 ft. 4.2672 mD, Vessel ID inches 112 Selected ID= 112.00 Nozzle Weight Multiplier: 1.25

Weight Estimation: 17626 lbs. 7.993496 Tonnes4. Configuration

ID inches 112.00 in->ft 9.3333333 2.8447999 m ~10ft (3.1m) height standard for scrubberA ft 2B ft 2C ft 2 Ratio 3< L/D < 6 1.5D ft 4.5E ft 0.42F ft 2.17H ft 13.1 Selected H= 14 ft 4.2671999 m

Comments:Genesis D: 3.0m = 118.12 in. Minimum calculated D: 112 in. Genesis L = 7.5m, Calc H = 4.3m. Genesis wt = 17.5 Tonnes. Calc wt = 8 Tonnes.

HP Flare KO Drum43-VD-1700

B

C

D

E

HHL

HL

NL

F

ID

Flare Drum Sizing (Vertical)

Electrical Load ListLoad on Turbine Generators (1) Load on Turbine Generators (1) Ship Service Generation Capacity (2)

(N + 1, Full Production Included, Electric Drive VRU) (N + 1, Full Production Included, Electric Drive VRU) One Turbine Generator running, one idle.Full Production Load 4190 kW Full Production Load 5419 kW Non-Production Load 1889 kW

4376 kW 4376 kW 4376 kW

Quantity of Turbines Running 1 Quantity of Turbines Running 2 Percent Loading on One Turbine 43%

Load on One Turbine 4190 kW Load on Each Turbine 2709 kW

Ship Service Transformer Capacity (3)

Percent Loading on One Turbine 96% Percent Loading on Each Turbine 62% One Main Transform er in service, one idle.Non-Production Load 1766 kVA

Available Capacity With One Turbine Running 4376 kW Available Capacity With Tw o Turbines Running 8752 kWMain Transformer Rating at 55º C 2500 kVA

Remaining Capacity 186 kW Remaining Capacity 3333 kWPercent Loading on One Transformer 71%

Load on 5 kV Switchgear Bus Load on 5 kV Switchgear BusRated Amps 2000 Rated Amps 2000 Load on Emergency Diesel Generator (4)

kW kVA Amps kW kVA AmpsConnected Load 8429 9521 1321 Connected Load 8429 9521 1321 Connected Load 565 kW

Percent of Rated Amps 66% Percent of Rated Amps 66%kW kVA Amps kW kVA Amps Emergency Diesel Engine Rating 725 kW

Full Production Load 4190 4749 659 Full Production Load 5419 6147 853Percent of Rated Amps 33% Percent of Rated Amps 43% Percent Loading on Emerg Diesel Engine 78%

Load on 480V Switchgear - Bus A Load on 480V Switchgear - Bus A Load on Auxiliary Diesel GeneratorRated Amps 4000 Rated Amps 4000

kW kVA Amps kW kVA Amps Black Start Load 492 kWConnected Load 2063 2310 2779 Connected Load 2063 2310 2779

Percent of Rated Amps 69% Percent of Rated Amps 69% Aux Diesel Engine Rating 725 kWkW kVA Amps kW kVA Amps

Full Production Load 652 720 866 Full Production Load 855 949 1142 Percent Loading on Aux Diesel Engine 68%Percent of Rated Amps 22% Percent of Rated Amps 29%

Load on Main TransformerLoad 480V Switchgear - Bus B Load 480V Switchgear - Bus B One Main Transform er in service, one idle.

Rated Amps 4000 Rated Amps 4000 Full Production Load 1731 kVAkW kVA Amps kW kVA Amps

Connected Load 2082 2261 2720 Connected Load 2082 2261 2720 Main Transformer Rating at 55º C 2500 kVAPercent of Rated Amps 68% Percent of Rated Amps 68%

kW kVA Amps kW kVA Amps Percent Loading on Main Transformer 69%Full Production Load 928 1011 1216 Full Production Load 998 1077 1295

Percent of Rated Amps 30% Percent of Rated Amps 32%Capacity of 5 kV Main Generation Bus (10)

Tw o Turbine Generators Connected.Load on 480V Emergency Switchgear Load on 480V Emergency Switchgear 5 kV Bus Rating 2000 Amps

Rated Amp 1600 Rated Amps 1600 Maximum Generator Rating (2 Gen's) 1666 AmpskW kVA Amps kW kVA Amps Percent of Bus Rating 83%

Connected Load 565 614 738 Connected Load 565 614 738Percent of Rated Amps 46% Percent of Rated Amps 46% Capacity of 480V Switchgear Bus (10)

kW kVA Amps kW kVA Amps One Main Transform er Connected.Full Production Load 300 327 393 Full Production Load 300 327 393 480V Bus Rating 4000 Amps

Percent of Rated Amps 25% Percent of Rated Amps 25% Maximum Transformer Rating (1 Trans) 3368 AmpsPercent of Bus rating 84%

Verif iciation Against ABS & USCG Rules, Other AnalysisFull Production 30,000 BPD, 34.5 MSCFD Full Production 45,000 BPD, 51.7 MSCFD

Rating of Taurus 60 (T-7901) Turbine Generator, Dual Fuel, Using NG, Site Rating at

95ºF, Inlet & Exhaust Duct Loss: 10" WC

Rating of Taurus 60 (T-7901) Turbine Generator, Dual Fuel, Using NG, Site Rating at

95ºF, Inlet & Exhaust Duct Loss: 10" WC

T-60 (T-7901) Turbine Generator, Dual Fuel, Using NG, Site Rating at 95ºF,

Inlet & Exhaust Duct Losses 10" WC

XXXXXX Field Development

Topsides FEED

Electrical Load Analysis

Document No.XXX

JOB NO. XXX

CHECK APPROVED DATE

A XXX XXX 28/6/2005

REV NO. DESCRIPTION AUTHOR

FOR CLIENT COMMENT XXX

Integrated LER & CR Modular Building Example

Layout - MOPU FE Studies

Flare Isopleths

Weight Estimation Model

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Cost Estimating – Facilities Cost Output 1 of 2

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Cost Estimating – Facilities Cost Output 2 of 2

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Cost Estimating – Brownfield Tool Structure

• Offshore Brownfield Estimating Tools

• Cost Estimating– Level 1 - Capacity Basis– Level 2 - Tonnage Basis– Level 3 - Composite Quantity

Norms– Level 4 - Detailed Job Card

Norms

END