nicolas separación gas-líquido

7/26/2019 Nicolas Separacin Gas-Lquido

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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



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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



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Mark Bothamley,

DROPLET SIZE

Gravity settling section collectsdrops to 140 m higher.

Extractor generates fogdroplets coalescence between10-140 m.


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=

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


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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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.



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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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SPHERICAL SEPARATORS

HORIZONTAL FILTER


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Solids

Liquid

coalesced


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


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


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


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


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


A vane-type mist extractor made from angle iron

VESSEL INTERNALS


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BAFFLES:

VESSEL INTERNALS


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


VESSEL INTERNALS


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WIRE MESH:

VESSEL INTERNALS

Horizontal separator fitted with wire-mesh pads supported by a frame.


VESSEL INTERNALS


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OTHER CONFIGURATIONS:

VESSEL INTERNALS


Centrifugal mist extractor Vertical separator fitted with a c

VESSEL INTERNALS


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OTHER CONFIGURATIONS:

VESSEL INTERNALS


A coalescing pack mist extractor

VESSEL INTERNALS


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WAVE BREAKERS:

VESSEL INTERNALS


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


Defoaming plates

VESSEL INTERNALS


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VORTEX BREAKER:

SS S

Vortex breaker Typical vortex breakers


VESSEL INTERNALS


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SAND JETS AND DRAINS:


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.



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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



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Vertical separator with a pressure

containing cone bottom used to

collect solids.

Vertical separator fit te

internal cone bottom

equalizing l in

PROBLEMS



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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



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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



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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



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2. Calculate the capacity of the gas.3. Calculate the capacity of the liquid.

7,0

2 lr

eff

Qt

Ld

SEPARATORS



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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



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1. Determine the drag coefficient CD by a iterative process (Ass

CD = 0.34 ).



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



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CD = 0.34 ).

2. calculate the capacity of the gas.3. calculate the capacity of the liquid.




6. Determine the slenderness ratio for each diameter.

d

LSR SS

12

SEPARATORS



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CD = 0.34 ).





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



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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



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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



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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



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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



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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



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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.

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