separation technologyAn Technologies Subsidiary
l e a d i n g i n
SEPARATIONtechnology
TABLE OF CONTENTS
Introduction 1
Information Bulletins
SPIRAFLOWTM Cyclone 2
CDS-Gasunie Inlet CycloneTM 3
CDS-Gasunie Cyclone ScrubberTM 4
CDS-Statoil DegasserTM 5
Vane Pack 6
Miscellaneous Internals 7
R&D and Flow Visualisation 9
Computational Fluid Dynamics 10
Case Studies
SPIRAFLOWTM Demisting Cyclone 11
Vane Pack vs Cyclone 13
CDS-Gasunie Inlet CycloneTM (Liquid/liquid separation) 15
CDS-Gasunie Inlet CycloneTM (Defoaming) 16
CDS-Gasunie Cyclone ScrubberTM 17
CDS-Statoil DegasserTM 18
Contact Details 19
CDS Separation Technology in a nutshell
CDS designs and develops state-of-the-art separators.
Over the years, we have established a reputation for
supplying highly innovative separation solutions to the
offshore industry. A reputation that reflects our ability to
increase separator throughput, reduce extraction costs
and prolong the profitable exploration of depleted
oil fields.
Our objective is to make the oil extraction process more
efficient and less expensive. In pursuit of this objective,
we are able to draw on unparalleled expertise, advanced
in-house test facilities, the latest CFD tools and funda-
mental research. As you might expect, CDS has also
implemented a comprehensive quality management
system that complies with ISO 9001:2000 standards.
In September 2003 FMC Technologies acquired a
controlling interest in CDS.
As quality separation solutions are based on a thorough
understanding of your process parameters, we make
every effort to encourage and facilitate a close working
relationship with our customers. Moreover, as hundreds
of customers around the world will testify, we are
dedicated to providing you with a highly efficient and
cost-effective solution, no matter how diverse your
requirements may be.
This brochure describes our technology, research
capabilities and products. Should you require additional
information, please feel free to contact us. Our contact
details are found on the back of this brochure.
INTRODUCTIONpage one
SPIRAFLOWTM CYCLONEpage two
The CDS SPIRAFLOWTM cyclone provides a high separation efficiency of fine droplets and foam even at high operating
pressures. It can be positioned either vertically or horizontally within a vessel and due to its high capacity it is ideal for
the revamping of vessels. For new built applications the vessel size with these internals can be
substantially reduced leading to considerable vessel cost and weight savings. The SPIRAFLOWTM
cyclone is very efficient for low and high pressure applications and with low surface tension liquids.
Operating Principle
Mist enters the cyclone and flows through the stationary
swirl element causing an intense gas rotation. Droplets are
separated by the subsequent centrifugal action and are
coalesced into a
liquid film on the
cyclone inner wall.
This liquid film is purged out of the cyclone by a combination
of the rotating flow and the secondary gas flow.
The secondary gas flow is then recombined with the main
flow through a pipe leading to the centre of the cyclone.
Operating Characteristics
Separates all mist droplets > 5µm (Atmospheric conditions).
Vane/SPIRAFLOW 80 Efficiency Comparison
Atm. Cond. Gas 60 kg/m3 - Liquid 600 kg/m3
CDS 350 Vane CDS 250 Vane SPIRAFLOW cyclone
Dro
plet
Siz
e fo
r 10
0% s
epar
atio
n(m
icro
ns)
CDS-GASUNIE INLET CYCLONETM
page three
Operating Principle
The optimised blade geometry brings the combined phase
into rotation with minimum shear. The resulting centrifugal
force moves the liquid and solid particles towards the cyclone
wall, where they form a liquid film that flows to the bottom
of the cyclone. The gas leaves the cyclone through the central
vortex finder. The baffles in the bottom of the cyclone stop
the rotation of the liquid, and a blocking plate prevents
liquids from being entrained into the gas. In this way it is
ensured, that no gas carryunder or liquid carryover can occur.
Advantages
• Enables the debottlenecking of both liquid and gas
constrained vessels.
• Not susceptible to fouling.
• Excellent slug handling capabilities.
• High turndown.
The CDS-Gasunie Inlet CycloneTM can be used for the following services:
• Foam breaking. • Degassing.
• High liquid / liquid separation efficiency. • High inlet momentums.
Even at high inlet momentums (up to 65,000 kg/ms2) field trials have proved that both liquid / liquid separation and
defoaming capabilities are improved using this device making it ideal for
retrofit applications. For new built vessels both the size of the inlet piping
and vessel can be reduced thus providing an overall compact solution.
CDS-GASUNIE CYCLONE SCRUBBERTM
page four
The CDS-GasunieCyclone ScrubberTM can be used for separation
of liquids (water, hydrocarbon, glycol, etc.) from gases (natural
gas and other), for the protection of downstream equipment
(compressors, gas turbines, flow meters, etc.). Solid particles
(dust, sand, etc.) will also be removed, making the scrubber
suitable for use as a gas wellhead separator.
Operating Principle
The optimised blade geometry brings the combined phase
into rotation. The resulting centrifugal force moves the liquid
and solid particles towards the vessel wall, where they form
a liquid film that flows to the bottom of the vessel.
The gas leaves the vessel through the central vortex finder
connected to the gas outlet nozzle. The baffles in the bottom
of the vessel stop the rotation of the liquid, and a blocking
plate prevents liquids from being entrained into the gas.
In this way it is ensured, that no gas carryunder or liquid
carryover can occur.
Advantages
• Results in small size and low weight as a result of high
allowable gas load factor. It is therefore especially
attractive for offshore applications.
• Maintenance friendly: No small channels or downcomer
pipes that are prone to fouling.
• Excellent slug handling capabilities.
• High turndown.
• Available as retrofit package.
• Over 200 references in a wide variety of applications.
Demister Gas Capacity Comparison
Gas
Loa
d Fa
ctor
(m
/s)
Gas 60 kg/m3 - Liquid 600 kg/m3
Mesh CDS 350 CDS 250 SPIRAFLOW CDS-GasunieVane Vane Cyclone Cyclone
CDS-STATOIL DEGASSERTM
page five
The CDS-Statoil DegasserTM is an inline device that separates
gas from liquid. It has no moving parts and requires no power.
Due to a very effective but simple control system it has a very
high separation efficiency regardless of flow fluctuations.
The separation efficiency is above 99.5% of gas from liquid,
while the separated gas is 100% free of liquid.
The diameter of the Degasser is generally the same as the line
into which it will be installed. Due to this and the fact that it
can be certified as a piece of pipe as opposed to a pressure
vessel the installation cost is low and maintenance is minimal.
In the Degasser gas and liquid are separated when the
multiphase fluid enters the separator where a stationary
swirl element causes the flow to rotate. This rotation forces
the liquid to flow along the outer wall and the gas to flow
in the centre. The gas is removed from the centre into a
scrubber section along with a portion of the liquid for control
purposes. This ‘control’ liquid subsequently rejoins the main
liquid flow leaving the Degasser after the main flow has
passed through an antiswirl element, intended to provide
pressure recovery and to prevent downstream vibrations.
Applications:
• Increases the capacity of existing separators by taking
out the gas upstream of them.
• Reduces the size of new separator vessels.
• Debottlenecking of multiphase lines.
• Debottlenecking of gas limited facilities.
Advantages:
• In-line.
• No (big) vessels necessary.
• Low installation costs.
• Minimal maintenance costs.
• Very flexible to flow fluctuations.
• Separation of gas from liquid > 99.5%.
• Separated gas is 100% free of liquid.
• The gas can go straight to compression or
to flare without further processing.
An 18-inch degasser for a produced water line.Capacity water 60,000 Sm3/d; gas 98,000 Sm3/d
An 11-inch test degasser.Capacity water 9,600 Sm3/d; gas 15,700 Sm3/d
VANE PACK page six
CDS offers a complete range of efficient vane packs including
the single and double pocket 200 series vanes for horizontal
flow and 300 series vanes for vertical flow.
Operating Principle
The mist laden gas passes through the parallel vane plates
and is forced to change direction several times. The mist
droplets are separated by the subsequent centrifugal forces
and are collected on the vane blades. This coalesced liquid
film is then removed through slits or pockets into a liquid
sump and drained to the liquid compartment of the vessel.
Operating Characteristics
Separates all mist droplets > 8µm (Atmospheric conditions).
Maximum pressure drop = 9 mbar.
CDS 350 CDS 250
CDS 230
Demister Gas Capacity Comparison
Gas
Loa
d Fa
ctor
(m
/s)
Gas 60 kg/m3 - Liquid 600 kg/m3
Mesh CDS 350 CDS 250 SPIRAFLOW CDS-GasunieVane Vane Cyclone Cyclone
MISCELLANEOUS INTERNALSpage seven
Perforated Distribution Baffle
In order to achieve an efficient gas / liquid and liquid / liquid
separation in horizontal vessels it is important to have a
quiescent flow regime along the length of the vessel.
This is accomplished by use of perforated baffles that have
shown both in tests, CFD models and more importantly
in the field that without these internals the separation
process can be adversely affected. The baffles can be
installed singularly, in a double arrangement and both full
and part diameter depending upon the intended duty.
Mesh Type Agglomerator
If a very high degree of gas / liquid separation is required or
if the separation duty is arduous either due to the presence of
small droplets or a high liquid load then use can be made of
mesh type agglomerators. They can be used both in horizontal
and vertical orientations and are intended to capture and
agglomerate the droplets and to seperate some of the liquid
prior to it entering the final mist eliminating device. Internal
drainage channels in the mesh ensure the efficient removal of
this separated liquid.
Sand Jetting System
Where sand or solid deposition in vertical or horizontal
vessels is expected, jetting systems can be installed.
Sand jetting systems fluidise the solids by use of pressurised
water introduced through spray nozzles for draining through
sand drains located down the length of the vessel.
The system can be arranged to flush the complete
length of the vessel at the same time or if the supply
is limited the system can be sectioned for the
flushing of smaller lengths.
MISCELLANEOUS INTERNALSpage eight
The EVENFLOW TYPE HE
The EVENFLOW TYPE HE inlet device is used to decrease the
momentum of the incoming feed stream, allowing removal of
any bulk liquids and solids that may be present and to evenly
distribute the gas flow over the vessel cross section. The even
distribution is necessary in order to minimise any chance of
channelling occurring through downstream devices and to
maximise gravity separation. Since it does not direct the fluids
downwards directly onto the liquid surface, re-entrainment
effects are minimised.
DEMISTER® Mist Eliminator
CDS can supply the complete range of standard and
traditional wire mesh mist eliminators. Through our
alliance partner Koch-Otto York we can offer reliable
quality and short delivery times
Plate Pack Coalescer
Plate pack coalescers are used in the liquid section of a
separator in order to maximise the amount of liquid / liquid
separation. The operating principle of plate packs relies on
the fact that the flow through the narrowly spaced plates
will be laminar and since the distance the dispersed phases
have to travel to the interface is much smaller, smaller
droplets will be separated.
R&D AND FLOW VISUALISATIONpage nine
CDS continually strives to develop new separation devices
and techniques for general and/or specific uses. In this way
we lead the market in the development and use of innovative
technology. Additionally we can verify and test internals,
either part or fullscale, to ensure that they will be sufficient
for their intended service.
In order to accomplish this we extensively make use of the
following methods:
• Computational Fluid Dynamics.
• Atmospheric test rigs using air and a multitude of liquids.
Maximum flow rates are 2,000 Nm3/hr of air and
100 m3/hr of liquid.
• High-pressure test rig using natural gas to a pressure of
40 barg and a multitude of liquids.
• "See through" high-pressure test rig (3-phases) with the
following characteristics:
- Gas: 4,000 am3/hr up to 60 kg/m3.
- Liquid: 800 m3/hr (2-phases).
• Equipment to perform flow visualisations.
• Comprehensive literature searches and theoretical analysis.
We also actively participate in joint industry projects and
partnerships. Examples of operators and universities with
which we participate are: Statoil, NAM, Shell, Norsk Hydro,
Technical University of Delft, Eindhoven University of
Technology.
Major projects to date include:
• Development of a vertical 3-phase separator concept
used on the Tune development for Norsk Hydro.
• Development of a novel liquid/liquid cyclone for both
water-oil cleanup and bulk separation.
• Development of a novel inline degassing cyclone leading
to a substantial reduction in gas loading of downstream
equipment.
• Deliquidiser for inline separation of bulk liquids
from the gas stream.
• Separation-turbine that can be used as a
replacement of the Joule-Thomson valve.
COMPUTATIONAL FLUID DYNAMICSpage ten
Flow distribution is critical in all gas / liquid and liquid /
liquid separation processes. As vessel sizes are reduced, or
more capacity is required from existing equipment, traditional
rules for the layout of vessel internals must be reviewed.
Flow velocities through inlet nozzles, outlet nozzles, internals
and over liquid levels can affect the separation performance.
A tool used by CDS to investigate this is Computational Fluid
Dynamics, which provides an accurate representation of the
flow profiles inside a separator.
CFD can also be used to model time dependent applications
like floating separators to ensure that the proposed slosh
mitigation technique is adequate for both 2- and 3-phase
separators. Two examples of this are shown below.
CFD is not only limited to individual vessels but can also
be used to evaluate flows in piping systems, or flow
distributions in manifolds as shown below.
CFD can be used for steady state cases,
for instance when looking at the flow profile through a
scrubber vessel as shown above.
SPIRAFLOWTM DEMISTING CYCLONEpage eleven
In recent years CDS Engineering has performed a series of
upgrades of the Feed Gas Scrubber and 2nd Stage
Recompressor Scrubber upstream of the Amine Absorbers
on a North Sea production platform.
Process Scheme
As shown in the figure, the gas streams from both scrubbers
are combined together prior to entering the Amine Absorbers
for CO2 removal.
The thought behind the design was that in order to avoid
liquid entering the absorbers, due to condensation in the
piping and carryover, the gas from the Feed Gas Scrubber
would be mixed with the relatively hot gas from the 2nd Stage
Compressor resulting in superheated gas entering the
absorbers. However, due to substantial liquid carryover from
the scrubbers, a superheated state of the gas was not
achieved. This meant that liquid entered the absorbers,
resulting in poor CO2 removal performance and operational
difficulties.
To tackle this problem the 2nd Stage Recompressor Scrubber
went through a series of retrofits in order to reduce liquid
carryover.
1) Feed Gas Scrubber
2) Amine Absorbers
3) 2nd Stage Recompressor Scrubber
4) 2nd Stage Compressor
1 2
2
3
4
4
▼
▼
▼
▼
▼
▼
▼
SPIRAFLOWTM DEMISTING CYCLONEpage twelve
In order to determine the effectiveness of the retrofits a
comparative C6+ analysis was used. This involved taking a
sample of gas before it entered the absorbers. This gas was
then analysed and the amount of C6+ components was
recorded. As more liquid entered the absorbers the C6+
value increased.
The original internals in the vessel comprised a type of half
open pipe inlet device and a vane pack. Due to shutdown
time limitations, initially only the inlet device was replaced
by a vane type inlet device, which reduced the C6+ by 20%.
The following year the vane pack was replaced with
AXIFLOWTM cyclones, the forerunner of the SPIRAFLOWTM
cyclone, which showed a 44% reduction in C6+.
The problem with the operation of the Amine Absorber as
described above was finally tackled in 1999 by replacing
the AXIFLOWTM cyclones with SPIRAFLOWTM cyclones.
The installation of the SPIRAFLOWTM cyclones resulted in
a substantial improvement in performance of the vessel
with a 68% reduction in C6+. The table below shows a
summary of these retrofits.
2nd Stage Recompression ScrubberOperating Pressure: 44.7 bara
Year Retrofit Summary Internals C6+ Performance
(%) Improvement
1996 Old Configuration Cowcatcher Inlet + Vane Pack 0.8 to 2.0 Base
1997 Quick Fix Vane Inlet + Vane Pack 0.7 to 1.6 13 to 20 %
1998 AXIFLOWTM Upgrade Vane Inlet + AXIFLOWTM Cyclones 0.4 to 0.9 43 to 44 %
1999 SPIRAFLOWTM Upgrade Vane Inlet + SPIRAFLOWTM Cyclones 0.13 to 0.3 67 to 68 %
VANE PACK VS CYCLONEpage thirteen
Referring to the SPIRAFLOWTM Case Study, it is seen that
after the 1998 retrofit, when the vane pack was replaced
by cyclones, there was less liquid carryover from the vessel
(44% decrease in C6+). This substantial reduction in carryover
with cyclones is explained by two mechanisms:
1) Droplet removal characteristics
For both cyclones and vane packs, droplets are removed as a
result of a change in direction of the gas flow. With this
change in direction, the droplets are subjected to forces,
moving them towards a surface onto which they coalesce,
thus establishing separation. In a cyclone a highly swirling gas
flow is generated through a static swirl element whereas in a
vane pack the flow of the gas only changes direction due to
the bends in the corrugated parallel plates. Due to the
mechanism of swirl generation, higher acceleration forces are
established in a cyclone. This means it is far more efficient
than a vane pack at removing droplets. This becomes more
apparent at increased operating pressures where separation
becomes difficult due to the decreased density difference
between the gas and the liquid and re-entrainment effects,
which are discussed later. CDS Engineering has performed
extensive tests at a pressure of 40 bar, which show that vane
packs fail to separate the small droplets that cyclones
efficiently remove. It should be noted that at lower than
design gas throughputs, the droplet removal capabilities of
vane packs drop substantially faster than with cyclones.
2) Re-entrainment of liquids
For both vane packs and cyclones the limiting factor in
terms of maximum capacity of the unit is the occurrence
of liquid film re-entrainment. This sets the allowable gas
throughputs and therefore limits the velocity and hence
accelerations within the body of the unit.
VANE PACK VS CYCLONEpage fourteen
Ultimately this will therefore limit the droplet size that can be
removed by the device. After all it is pointless to separate
something that is going to re-entrain and be carried-over.
The re-entrainment mechanism in vane packs essentially
occurs at the end or tip of the corrugated plates. Here,
separated liquid that runs along the plate gets torn off due to
the shear forces exerted by the gas onto the liquid. For the
maximum shear force, which is determined by liquid
properties, the gas velocity has to decrease for high gas
densities. This is because shear force is proportional to ρv2.
One of the liquid properties that limits the allowable shear
stress in a vane is the surface tension. As the surface tension
reduces, the allowable shear stress also drops. This is why
separation problems are generally seen with vane packs at
higher operating pressures when gas densities are high and
liquid surface tensions are low.
Within axial flow cyclones, this effect is suppressed because
of the centrifugal stabilisation caused by the swirling flow of
the gas, keeping the liquid film in contact with the cyclone
wall. In this way cyclones can process far more gas than vane
packs before re-entrainment occurs and therefore still separate
the smaller droplets.
For the SPIRAFLOWTM cyclone, the re-entrainment
mechanism is different to that of vanes since the liquid is
contained inside the cyclone tube as a continuous spinning
film, i.e. there is no end or tip at the outlet from which liquid
gets torn off. A pressure force acting on the liquid discharge
slots in the cyclones causes re-entrainment. In operation this
pressure force is opposed by the centrifugal force generated
by the spinning liquid. For each application it is ensured that
the centrifugal force is greater than the pressure force so that
no re-entrainment occurs. Since the centrifugal forces in the
cyclone are higher than in a vane more gas can be processed
before re-entrainment becomes a problem.
A further benefit is that the re-entrainment mechanism of
the SPIRAFLOWTM cyclone is not affected by surface tension.
The figure above shows the maximum velocity for a vane
pack (v max) that is dictated by the re-entrainment ρv2 limit.
The other lines show the minimum velocities required within
the vane in order to remove 20, 35 and 70 micron droplets.
As can be seen 20 micron droplets cannot be removed at gas
densities greater than around 10 kg/m2 since the required gas
velocity would exceed the re-entrainment limit.
The figure above shows the maximum throughput for a
cyclone (Q max) that is dictated by the re-entrainment limit.
The other lines show the minimum throughputs required
within the cyclone in order to remove 12, 15 and 20 micron
droplets. As can be seen all droplets can be removed, even
at the higher gas densities, without exceeding the re-
entrainment limit.
v (m
/s)
Gas Density (kg/m3)
Thro
ughp
ut/C
yclo
ne (
m3 /
h)
Gas Density (kg/m3)
Q
Q
Q
Q
page fifteen
Liquid / Liquid Separation
On Statfjord C, a Statoil operated platform
in the North Sea, a CDS-Gasunie Inlet
CycloneTM was tested in the Test
Separator. The purpose of this test was to
evaluate the liquid / liquid separation
performance in order to check the
feasibility of revamping the main
production separator on the platform.
In order to evaluate the liquid / liquid separation performance
the Test Separator was modified to provide 17 extraction
points for liquid samples at various distances from the
cyclone and at various heights.
The actual test conditions were very challenging especially
considering possible phase inversion due to the water cut
range of 42% to 76% and droplet shearing within the inlet
piping due to the high momentum values of up to
65,000 kg/ms2.
It was found that the inlet cyclone arrangement operated
very well with an oil in water quality that in the majority of
cases was below 40 mg/l meaning that it could be disposed
of to sea without further treatment. In all cases the water in
oil quality was below 5%. These results were maintained up
to an inlet momentum of 65,000 kg/ms2 whereas the normal
separator inlet nozzle design criteria is between 6,000 kg/ms2
and 10,000 kg/ms2. The complete set of results are shown
above together with the water in oil results that
were achieved with a simple deflector plate
inlet device.
% Water in oil inlet cyclone
% Water in oil deflector plate
Oil in water (ppm) inlet cyclone
Water cut (%)
Field Test at Statfjord CJanuary 1999
Inlet Momentum (kg/ms )
% W
ater
in o
il
2
Oil
in w
ater
(pp
m)
Wat
er c
ut (
%)
CDS-GASUNIE INLET CYCLONETM
Defoaming
High injection rates of defoaming chemicals
had been required to operate the production
and test separators on the Mars TLP, a Shell
operated platform in the Gulf of Mexico.
In an effort to reduce the chemical
consumption, different means of
mechanically breaking the foam were
investigated in the Test Separator including
AXIFLOWTM demisting cyclones and a
CDS-Gasunie Inlet CycloneTM. The result was
that for two different wells, the chemical
consumption was reduced by 20% and 80% respectively.
On the basis of the successful test results with the Test
Separator, the four main production separators were
retrofitted with new internals. Chemical consumption has
been reduced in the order of 50%. Other operational
problems due to foaming listed below were also reduced:
• Poor level control that led to platform shutdowns.
• Liquid carryover in the gas outlet that led to flooding
of downstream scrubbers and compressors.
• Gas carryunder in the liquid outlet that led to increased
downstream compression requirements.
The figure above indicates increasing total production rates
(red line) while reducing the defoamer consumption
(blue line). The CDS internals were installed in June 1998.
Chemical Scorecard Defoamer5 Month Rolling Average
Oil,
MB
bl
Gal
/MB
blCDS-GASUNIE INLET CYCLONETM
page sixteen
production rate
defoamer consumption
CDS-GASUNIE CYCLONE SCRUBBERTM
page seventeen
In a development project performed by CDS Engineering in
association with Gasunie Research, the conventional Gasunie
type cyclone scrubber was analysed and points for improvement
were identified. With the use of CFD and high-pressure tests
at the Gasunie Research facility, several geometrical
improvements regarding the fluid flow inside the separator
were tested. It was found that by optimising the separator
internals, the pressure drop could be reduced by 50%.
During further high-pressure tests it was verified that the
separation efficiency remained the same.
The benefit of the optimised design is that when designing
for the same pressure drop and separation efficiency, the
separator vessel can be reduced in size, leading to savings
on capital investment cost.
A case study was carried out for a gas-liquid separation
section of a gas production plant. The gas comes straight
from the wellhead and enters a CDS-Gasunie type separator.
Liquids (hydrocarbon and water), as well as sand, are
separated from the gas. After cooling, the gas runs through a
second CDS-Gasunie type separator, before entering a
compression module and the downstream gas treating plant.
Taking the conventional Gasunie cyclone as a base case, the
vessel ID and Tan/Tan length could both be reduced to 84%
for the new CDS-Gasunie design. This led to a lower
investment cost for the combined pressure vessel and
internal.
Results of case study
Conventional Design Optimised Design
ID 835 mm 700 mm
Tan/Tan 4,100 mm 3,438 mm
Relative Cost 1.00 0.85
CDS-STATOIL DEGASSERTM
page eighteen
Produced water from an inlet separator, test separator and
flash drum of a platform in the North Sea contains dissolved
hydrocarbon gas. The water is being cleaned of oil through
a set of hydrocyclones prior to pressure let down and
discharge to sea via the produced water-degassing drum.
Due to the pressure drop through the hydrocyclones, piping
and level control valves, gas will evolve from the produced
water. As a result of a combination of unfavourable pipe
routing together with an unacceptable ratio between gas and
water, the fluid flow in the 18" pipe from the hydrocyclones
to the produced water-degassing drum is in the slug flow
regime. These slugs result in strong vibrations in the piping
leading to the produced water flash drum in addition to
creating surge conditions in the flare system. This problem
puts a limitation to the capacity of the system as well as being
a safety concern due to the vibrations.
The goals for the installation of an 18-inch degasser were:
• Stop vibrations in the piping system to remove the risk of
mechanical fatigue and increase the capacity of the
system.
• Avoid pulsations and instability in the gas flow system.
• Reroute the separated gas to the recompression system
instead of flaring it as before. This is good for the
environment as well as giving a huge saving in CO2 taxes.
Design Data of the 18" Degasser
Operating Pressure (barg) 3-6
Operating Temperature (°C) 84
Max Water Flowrate (Sm3/d) 60,000
Max Gas Flowrate (Sm3/d) 98,000
Gas Fraction (%) 20 – 45
NOTESpage nineteen
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separation technologyAn Technologies Subsidiary
NOTESpage twenty
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separation technologyAn Technologies Subsidiary
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