Three phase separator - Oil and gas processingFull description
this is a spreadsheet for the design calculations for a three phase oil/ water and gas separator. it gives a step by step guide to the userFull description
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CUSTOMER xxxxxxxxx PLANT LOCATION PROJECT / UNIT xxxxxxxxxxxx RATING INPUT
71740.0 9.08 0.0094 1.162 0.9309 44.65
UNIT
xxxxx
ITEM
xxxxxxxxxx
GAS PROPERTIES Mass Flow Rate kg/h Density kg/m3 Viscosity cp Adiabatic Coeff. cp/cv / Compressibility Factor / Z Molecular Weight kg/kmol
JOB
xxxxxxxxx
Sh.
Rev.
of
Separator Type Inlet Distributor Type Demister (See Note 1) Head Type
0
Other Half Open Pipe
Yes Elliptical 2:1
OPERATING CONDITIONS Temperature °C Pressure (gauge) barg
LIGHT LIQUID PHASE PROPERTIES Mass Flow Rate kg/h 35410.0 Density 602.30 kg/m3 Viscosity cp 0.1896
32.22 4.80
HEAVY LIQUID PHASE PROPERTIES Mass Flow Rate kg/h 5361.0 Density 1002.00 kg/m3 Viscosity cp 0.7606
NOZZLES NIN Inlet NG Gas Outlet NLl Light Liquid Outlet NLh Heavy Liquid Outlet Manhole
VESSEL SIZING Vessel Diameter mm D Demister Lenght mm Demister Thickness mm Vessel Lenght mm L
GEOMETRICAL DATA TG-Demister Top Surf. h0 mm Liq-Liq Sep. Lenght L* mm Gas Outlet Nozzle - TL L1 mm Vessel L/D /
450 9000 850 3.43
LIGHT LIQUID PHASE LEVELS h2' HHIL-LLLL mm HII LLLL-LLL mm Hrl LLL-HLL mm HI HLL-HHLL mm
150 150 350 150
HEAVY LIQUID PHASE LEVELS h2 BG-LLIL mm HIIi LLIL-LIL mm Hrli LIL-HIL mm Hii HIL-HHIL mm
GEOMETRICAL DATA Trasversal Area A ∙L A V [m2] [m3] Av Vv 4.81 57.73 Aw Vw 4.81 57.73 At Vt 4.29 51.43 An Vn 3.68 44.16 Au Vu 3.08 37.02 Az' Vz' 2.59 31.07 Awi Vwi 2.11 25.34 Ati Vti 1.66 19.88 Ani Vni 1.16 13.97 Aui Vui 0.72 8.68 Az Vz 0.40 4.79
LIQUID-LIQUID SEPARATION HEAVY FROM LIGHT LIQUID PHASE SEPARATION
Light Liquid Sep. Level Heavy Liq. Drop.Term. Vel. C/Re
/ m/s /
NIL-NILL 5.77E-04 1.42E+04
HHIL-LLLL 5.70E-04 1.48E+04
LIGHT FROM HEAVY LIQUID PHASE SEPARATION
Heavy Liquid Sep. Level Light Liq. Drop. Term. Vel. C/Re
/ m/s /
BG-NIL 8.86E-05 5.68E+06
NOZZLES Gas Sound Velocity m/s Gas Phase Mass Fraction / Mixed Phase Density kg/m3 3 Total Liquid Density kg/m Mixed Phase Critical Vel. m/s
REV
DATE
BG-LLIL 1.24E-04 2.07E+06
248.01 0.64 14.12 635.64 199.64
DESCRIPTION
ISSUED
CHECKED
APPROVED
CUSTOMER xxxxxxxxx PLANT LOCATION ENGINEERING AND DESIGN INSTITUTE FOR OIL REFINERIES AND PETROCHEMICAL PLANTS PLOIESTI - ROMANIA
UNIT
xxxxxxxxx
xxxxx 0
ITEM
xxxxxxxxxx PROJECT / UNIT xxxxxxxxxxxx RATING SKETCH
JOB
Sh.
Rev.
of
0
(See note 6)
L
12000
pe
L0
L1
(See Note 7)
O pe n
Pi
10325
850
al f
NIN= 24
NG= 14
h0 1750
150
450
H
TG
3500
1650
TL
HHLL HLL
D
HI Hrl HIl h2' HIi Hrli HIIi
LLL LLLL
MH= 24
HHIL HIL LIL LLIL
BG NLh= 2
Elliptical 2:1
h1
NLl=
h2
6
B-B
LIQUID LEVELS mm
LLIL LIL NIL HIL HHIL LLLL LLL NLL HLL HHLL
300 450 625 800 950 1100 1250 1425 1600 1750
Av
h1
Az
h2
B-B
REV
DATE
DESCRIPTION
ISSUED
CHECKED
APPROVED
CUSTOMER xxxxxxxxx PLANT LOCATION PROJECT / UNIT
Sh.
xxxxxxxxxxxx NOTES
Note 2: Note 3: Note 4: Note 5: Note 6: Note 7:
UNIT
xxxxx 0
ITEM
xxxxxxxxxx
Note 1:
JOB
xxxxxxxxx
Rev.
of
0
Vessel shall be suitable for removal of 95% of 200÷400 μm liquid particles. Mesh Pad Demister shall be suitable for removal of 99.9% of 10 μm liquid particles. Light Liquid Droplet Separation from Gas @ HHLL For Operating Pressure P<0.1 barg and P>1 barg the 'KR' Demister Factor is extrapoleted. See PRG.PR.VES.0001 Paragraph 4.1.3. Overfilled is referred to Light Liquid Overflow Deleted All sizes are in mm, unless nozzle sizes are in inch. Gravity Separation Lenght (L0) is the distance between TL and Demister.