drl toolsequipment list 106 8060 : living quarters - hd & shop 107 living quarters & hd...
TRANSCRIPT
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
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 – 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)
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
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(
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oil
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eff
oilohoil
ohoiloiloheff
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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
33
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