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LIQUID GAS SEPARATION
Presented by:
Mara Catalina Monroy Muoz
Carlos David Perez Ros
Marlon Alfredo Zorro O.
Presented to:
M.Sc Nicols Santos Santos
Escuela de Ingeniera de Petrleos
Universidad Industrial de Santander
2016
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OUTLINE
Introduction
Separators Principles.
Separation Functions.
Separator Types
Vessel Internals
Potential Operating Problems
Separator Design
Conclusions
Bibliography
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INTRODUCTION
WELL FLUID
Gas
Oil
Water
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SEPARATORS
1. Inlet Stream: Changes in
the amount of momentum andcentrifugal force.
2. Gravity Settl ing Section:
Stokes Law, Drag Force,
Gravity Force.
3. Mist Extractor: Drag
Force, Coalescence and
Gravity Force
4. Liquid Collection Section:
Retention Time.
Source:ARNOLD, Ken. Surface Production Operation. Vol
1.2.
3.
4.
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=1,488
,
18 =
This law also defines the relationship between particle size and th
of gravitational settling.
STOKES LAW
SEPARATORS PRINCIPLES
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It is this force that removes the liquid droplets contained in the g
=
2
Where:
FD drag force, lbf (N),
CD drag coefficient,
A cross-sectional area of the droplet, ft2 (m2),
density of the continuous phase, lb/ft3 (kg/m3),
Vt terminal (settling velocity) of the droplet, ft/sec (m/sec),
g gravitational constant, 32.2 lbmft/lbf sec2 (m/sec2).
DRAG FORCE
SEPARATORS PRINCIPLES
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If the flow around the droplet were laminar, then Stokegovern and where Re = Reynolds number is less two.
=24
=1.7810()
Unfortunately, for production facility designs it can be shownlaw does not govern.
34,0Re
3
Re
2421 DC
21
0119,0
D
m
g
gL
tC
dV
DRAG FORCE
SEPARATORS PRINCIPLES
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SEPARATORS PRINCIPLES
Mark Bothamley,
DROPLET SIZE
Gravity settling section collectsdrops to 140 m higher.
Extractor generates fogdroplets coalescence between10-140 m.
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SEPARATORS PRINCIPLES
=
API Gravity
Tiempo de
retencin (min)
35+ 0.5-1
30 2
25 3
20- 4+
For the liquid and gas separator pressure equilibreached, a liquid storage is required. This is defined as "retentio
RETENTION TIME
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Source
SEPARATORS PRINCIPLES
CHANGES IN THE AMOUNT OF MOMENTUM
CENTRIFUGAL FORCE
COALESCENCE
GRAVITY FORCE
OTHERS
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SEPARATORS FUNCTION
Source: w
It makes the first phases separation between
hydrocarbons.
Enhanced the separation process through the
collection of liquid particles trapped in the gas
phase and the gas particles trapped in liquid
phase.
Release the trapped gas phase in the liquid
phase.
Downloaded separately the liquid and gas phase.
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SEPARATION TYPES
HORIZONTALSEPARATORS
VERTICALSEPARATORS
SPHERICALSEPARATORS
OTHERS
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HORIZONTAL SEPARATORS
Source:ARNOLD, Ken. Surface Production Operation. Volumes I & III. Chapter 4. 2008.
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HORIZONTAL SEPARATORS
Source: BOLLAND. Separadores lquidos, gases y slidos. El Medanito, Argentina.
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Efficient handling and processing of high volumliquid.
Suitable for separating emulsions.
Easy maintenance and transportation.
Does not handle solids
Requires more space.
Turbulence limitations.
Variables rates.
HORIZONTAL SEPARATORS
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Source: GPSA. Engineering Data Book. FPS Version. Volumes I & II. Sections 1 - 26. Chapter 7. 2004.
VERTICAL SEPARATORS
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Source: ARRIETA, Mario. Estaciones de flujo.
VERTICAL SEPARATORS
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Efficient solids control.
Less likely to return liquid to gas flow.
Good for low GOR.
Requires less space.
Difficult maintenance.
Little contact area between the phases.
Transport limitations.
VERTICAL SEPARATORS
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Type QGas and
Liquid
Foamy
crude
Gas /Oil
Easy
operation
and
maintenan
ce
Manageme
nt of solids Installation
area
Abso
turb
Horizontal
Vertical
SCREENING
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Source:ARNOLD, Ken. Surface Production Operation. Volumes I & III. Chapter 4. 2008.
SPHERICAL SEPARATORS
HORIZONTAL FILTER
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Solids
Liquid
coalesced
Source:ARNOLD, Ken. Surface Production Operation. Volumes I & III. Chapter 4. 2008.
HORIZONTAL FILTER
SEPARATORS
HORIZONTAL FILTER
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APP
LICATIONS
Entries compressor stations.
High GOR.
Removal of particles larger than 2 microns.
Pressure drop normal of 1 2 psi.
10 psi pressure drop criteria is used for filter change out.
HORIZONTAL FILTER
SEPARATORS
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OTHERS
SLUG CATCHER
A particular separator design
able to handle large liquid
volumes at irregular intervals.
Source:ARNOLD, Ken. Surface Production O2008.
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SLUG CATCHER
OTHERS
Source: Cat
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OTHERS
SCRUBBER
Vessel designed to handle
streams with high gas to liquid
ratios, usually have a small
liquid collection section.
Source: CAMPBELL. Gas Conditioning and processing Vo
O S
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OTHERS
SCRUBBER
Source: Catlogo Exterran.
OTHERS
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OTHERS
SCRUBBER
BER
Source: CarUSA. Gas Scrubber.
OTHERS
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OTHERS
DOUBLE-BARRELHORIZONTAL SEPARATORS
CENTRIFUSEPARATO
Source:ARNOLD, Ken. Surface Production Operation. Volumes I & III. Chapter 4. 2008.
OTHERS
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THREE PHASE SEPARATORS
OTHERS
Source: http://www.fenixchemtech.in/pdf_cat/intsep.pdf
VESSEL INTERNALS
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SEPARATORS ALL HAVE IN COMMON FOURSECTIONS:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
VESSEL INTERNALS
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VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Vertical separator schematic
Mist Extractor
Inlet Diverter
Liquid
Collection
section
Gravity settling
section.
Gas Out
Pressure
Control Valve
Inlet
Gas-Liquid Interface
Liquid Out
Level Control Valve
VESSEL INTERNALS
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Element that abruptly changes the
direction of flow, causing the release of
gas.
Reduce the momentum.
Perform an anitial separation.
THE INLET DEVICE
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operation
Baffle plates
VESSEL INTERNALS
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VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Three views of an example centrifugal inlet diverter
VESSEL INTERNALS
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VESSEL INTERNALS
Source:ARNOLD, K. Surface Production OperationsSource:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Elbow inlet diverter
Centrifugal inlet diverters. (Top) C
Tangential raceway.
VESSEL INTERNALS
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A reduction in flow rate of the
gas stream occurs, allowing
suspended liquid droplets fall by
gravity.
GAS GRAVITY SEPARATION SECTION
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operatio
Third Edition.
VESSEL INTERNALS
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LIQUID COLLECTION SECTION
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
VESSEL INTERNALS
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This device generates numerous
changes in the flow direction of the gas,
causing the liquid droplets ( less than
100 microns ) are caught by
coalescing elements and fall bygravity.
MIST EXTRACTION SECTION:
VESSEL INTERNALS
Source: ARNOLD, K. Surface Production Operations
VESSEL INTERNALS
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BAFFLES:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition. Source:ARNOLD, K. Surface Production Operations. Vo
Typical vane-type mist extractor/ eliminator Vane-type element with corrugated
drainage trays
VESSEL INTERNALS
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BAFFLES:
VESSEL INTERNALS
Source: ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition. Source: ARNOLD, K. Surface Production Operations. Vo
Cutaway view of a vertical separator fitted with a vane- type
mist extractor.
Cutaway view of a horizontal separator fit
mist extractor.
VESSEL INTERNALS
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BAFFLES:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
A vane-type mist extractor made from angle iron
VESSEL INTERNALS
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BAFFLES:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
An arch plate-type mist extractor
VESSEL INTERNALS
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WIRE MESH:
VESSEL INTERNALS
Source: ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Example wire-mesh mist extractor.
VESSEL INTERNALS
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WIRE MESH:
VESSEL INTERNALS
Vertical separators fitted with wire-mesh pads supported by support rings
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
VESSEL INTERNALS
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WIRE MESH:
VESSEL INTERNALS
Horizontal separator fitted with wire-mesh pads supported by a frame.
Source: ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
VESSEL INTERNALS
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OTHER CONFIGURATIONS:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Centrifugal mist extractor Vertical separator fitted with a c
VESSEL INTERNALS
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OTHER CONFIGURATIONS:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
A coalescing pack mist extractor
VESSEL INTERNALS
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WAVE BREAKERS:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Three-dimensional view of a horizontal separator fitted with an inlet diverter, defoaming e
And wave breaker
VESSEL INTERNALS
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DEFOAMING PLATES:
VESSEL INTERNALS
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Defoaming plates
VESSEL INTERNALS
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VORTEX BREAKER:
SS S
Vortex breaker Typical vortex breakers
Source: ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
VESSEL INTERNALS
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SAND JETS AND DRAINS:
Source:ARNOLD, K. Surface Production Operations. Vol.1. Chapter 3 Third Edition.
Schematic of a horizontal separator fitted with sand jets and inverted trou
VESSEL INTERNALS
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EXTERNAL ACCESSORIOS:
SAFETY RELIEF VALVE
CONTROL VALVES BACKPRESSURE
FULL CONTROL VALVES
POTENTIAL OPERATINGPROBLEMS
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PROBLEMS
FOAMY CRUDE
CO2 > 1-2%
1.Mechanical control of liquid level isaggravated.
2. Foam has a large volume-to-weight r
3. An uncontrolled foam bank.
POTENTIAL OPERATINGPROBLEMS
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PARAFAFFIN SAND
Coalescing plates in the liquid section
and mesh pad mist extractors in the
gas section are particularly prone to
plugging by accumulations of paraffin.
Cutout of valve trim.
Plugging of separator i
Accumulation in the
separator.
PROBLEMS
POTENTIAL OPERATINGPROBLEMS
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Source:ARNOLD, Ken. Surface Production Operation. Volumes I & III. Chapter 4. 2008.
Vertical separator with a pressure
containing cone bottom used to
collect solids.
Vertical separator fit te
internal cone bottom
equalizing l in
PROBLEMS
POTENTIAL OPERATINGPROBLEMS
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LIQUID CARRYOVER GAS BLOWY
Occurs when free liquid escapes
with the gas phase.
Occurs when free g
with the liquid phase
an indication of low
vortexing, or level contr
PROBLEMS
POTENTIAL OPERATINGPROBLEMS
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LIQUID SLUGS
Two-phase flow lines and pipelines tend to accumulate liquids
low spots in the lines. When the level of liquid in these low sp
rises high enough to block the gas flow, then the gas will push
liquid along the line as a slug.
PROBLEMS
DESIGN THEORY
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In the design of separators, it must be determined initially the dra
performing a process of trial and error with equations settl
Reynold's number and drag coefficient.
COEFFICIENT OF DRAG
CD =24
3
. 0.34
HORIZONTAL SEPARATORSIZING
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SIZING
GAS CAPACITY CONSTRAINT:
LIQUID CAPACITY CONSTRAINT:
21
420
m
D
gl
gg
effd
C
P
TZQdL
7,0
2 lreff
QtLd
Where:
d= Inches
Leff= ft
Lss= ft
T= R
P= psia
Qg= MMscf
Ql= Bpd
p= lb/ft^3dm= Micro
tr= Minutes
Cd= Drag c
Z= Gas com
HORIZONTAL SEPARATORSIZING
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SELECTION:
SIZING
d
LSR SS
12
d= InchesLss= ft
SR= DimensionSlenderness Ratio=
d (in) Gas Leff (ft) Liquid Leff
(ft)
Lss S
16
20
.
.
36
42
VERTICAL SEPARATORSIZING
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SIZING
GAS CAPACITY CONSTRAINT:
LIQUID CAPACITY CONSTRAINT:
= 5040
=
0,12
12
76h
LSS
12
40
dhLSS
For diameters < 36
For diameters < 36
VERTICAL SEPARATORSIZING
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SELECTION:
dLSR SS12Slenderness Ratio=
d= Inches
Lss= ftSR= Dimensionless
tr (min) d (in) h (in) Lss SR
SIZING
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process (Assu
a CD = 0.34 ).
= 0,0119
.
= 0,0049
CD =24
3
. 0.34
SEPARATORS
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process
(Assume a CD = 0.34 ).
2. Calculate the capacity of the gas.
21
420
m
D
gl
gg
eff
d
C
P
TZQdL
SEPARATORS
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process
(Assume a CD = 0.34 ).
2. Calculate the capacity of the gas.3. Calculate the capacity of the liquid.
7,0
2 lr
eff
Qt
Ld
SEPARATORS
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process
(Assume a CD = 0.34 ).
2. Calculate the capacity of the gas.3. Calculate the capacity of the liquid.
4. Establish relationships between the diameter of the spacer ( d
and the effective length ( Leff ) capabilities for gas and liquid.
d (in) Gas Leff(ft) Liquid Leff(ft)
16
20
24
30
36
42
SEPARATORS
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process (Ass
CD = 0.34 ).
2. Calculate the capacity of the gas.3. Calculate the capacity of the liquid.
4. Establish relationships between the diameter of the spacer ( d
the effective length ( Leff ) capabilities for gas and liquid.
5. Calculate the length between weld beads (LSS ) for each diam
12
dLL effss 5,2 effss LL ss L
4
3
SEPARATORS
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process (Ass
CD = 0.34 ).
2. calculate the capacity of the gas.3. calculate the capacity of the liquid.
4. Establish relationships between the diameter of the spacer ( d
the effective length ( Leff ) capabilities for gas and liquid.
5. Calculate the length between weld beads (LSS ) for each diam
6. Determine the slenderness ratio for each diameter.
d
LSR SS
12
SEPARATORS
DESING TWO-PHASESEPARATORS
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1. Determine the drag coefficient CD by a iterative process (Ass
CD = 0.34 ).
2. Calculate the capacity of the gas.3. Calculate the capacity of the liquid.
4. Establish relationships between the diameter of the spacer ( d
the effective length ( Leff ) capabilities for gas and liquid.
5. Calculate the length between weld beads (LSS ) for each diam
6. Determine the slenderness ratio for each diameter.
7. Select the option that contains a slenderness ratio between 3If two or more options are in that range, you can take the deci
use smaller diameter , it implies a lower cost .
SEPARATORS
DESING TWO-PHASE VERTICALSEPARATORS
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1. The first step in sizing a vertical separator is to establish the de
basis. (CD)
SYMBOL VALOR UNITS
Qg 10 MMSCFD
Qo 2000 BPD
API 40
P 1000 Psia
T 60 F
(SG)g 0,6
Dm 140 Micras
m 0,013 Cp
Z 0,84
Tr 3 min
DESING TWO-PHASE VERTICALSEPARATORS
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1. The first step in sizing a vertical separator is to establish the de
basis. (CD)
= ( ,
,+) = 2,7(
)
= 51,6 /3 = 3,71 /3
DESING TWO-PHASE VERTICALSEPARATORS
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2. Determine the drag coefficient CD by a iterative process (Assu
CD = 0.34).
CD =24
= 0,0119
.
= 0,0049
SYMBOL VALOR UNITS
l 51,6 Lb/ft3
g 3,7 Lb/ft3
dm 140 Micras
m 0,013 Cp
CD 0,340 F
Vt
DESING TWO-PHASE VERTICALSEPARATORS
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2. Determine the drag coefficient CD by a iterative process (Assu
CD = 0.34).
ITERATION Vt Re CD
1 0,867 169,8 0,712
2 0,600 117,3 0,821
3 0,558 109,2 0,847
4 0,550 107,6 0,852
5 0,548 107,2 0,854
DESING TWO-PHASE VERTICALSEPARATORS
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3. Calculate d, may be used to determine the minimum rediameter. Any diameter larger than this value may be used.
21
420
m
D
gl
gg
effd
C
P
TZQdL
indLeff 9,21
DESING TWO-PHASE VERTICALSEPARATORS
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4. For a selected d, may be used to determine h.
5. From d and h, the seam-to-seam length may be estimate
larger value of Lss should be used.
7,0
2 lreff
QtLd =
0,12
=
76
12
= 76
12
36
36
DESING TWO-PHASE VERTICALSEPARATORS
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= (12
)
tr(min) d(in) h(in) Lss(ft) Sg
1 24 28,9 8,7 4,4
1 30 18,5 7,9 3,2
1 36 12,9 7,4 2,5
1 42 9,4 7,6 2,2
1 48 7,2 7,9 2,0
CONCLUSIONS
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While designing the separators, it is essential to keep in
pressure conditions, temperature as well as the properties obeing separated. This is in order to design the proper dimensi
equipment.
The horizontal separators have an are big enough which en
existence of more equilibrium between the phases and enh
liberation of gas towards the zone of the mist extractor.
CONCLUSIONS
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The design of the separators has the end goal of deter
diameter and the optimal longitude, precise to the inch, in ord
the retention time required making the process of separ
efficient.
BIBLIOGRAPHY
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Arnold, K. Surface Production Operations. Volume II. Thir Editio
M.Campbell. Gas conditioning and processing. Volume 2Equipment Modules. 1984.
Gas Processors Suppleters Association. Engineering Data
2004.