WO1993009875A1 - Phase separation apparatus - Google Patents

Phase separation apparatus Download PDF

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Publication number
WO1993009875A1
WO1993009875A1 PCT/GB1992/002089 GB9202089W WO9309875A1 WO 1993009875 A1 WO1993009875 A1 WO 1993009875A1 GB 9202089 W GB9202089 W GB 9202089W WO 9309875 A1 WO9309875 A1 WO 9309875A1
Authority
WO
WIPO (PCT)
Prior art keywords
inlet
phase
chamber
outlet
mixture
Prior art date
Application number
PCT/GB1992/002089
Other languages
French (fr)
Inventor
Emil Gyorgy Arato
Mir Mahmood Sarshar
Original Assignee
B.H.R. Group Limited
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by B.H.R. Group Limited filed Critical B.H.R. Group Limited
Publication of WO1993009875A1 publication Critical patent/WO1993009875A1/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0217—Separation of non-miscible liquids by centrifugal force
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/26—Separation of sediment aided by centrifugal force or centripetal force
    • B01D21/265—Separation of sediment aided by centrifugal force or centripetal force by using a vortex inducer or vortex guide, e.g. coil
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/04—Multiple arrangement thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06—Construction of inlets or outlets to the vortex chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C2003/006—Construction of elements by which the vortex flow is generated or degenerated

Definitions

  • Cyclone phase separators operate by centrifugal action on multiphase material to separate the phases.
  • the material enters a separating chamber through a tangential inlet in order to generate a swirl component of flow.
  • the material flows around the chamber, the heavier material moving to the outside and the lighter material towards the axis of the chamber by centrifugal action.
  • Separate outlets for the two phases are arranged near the periphery and the axis of the chamber.
  • the present invention is concerned with separation of phases, eg a continuous liguid phase from gas or solids.
  • the phase separating apparatus comprises a separating chamber having an inlet for a phase mixture and radially separated outlets for phases of different densities, the inlet being located axially of the chamber.
  • the apparatus comprises means for inducing a swirl in the phase mixture from said inlet, said means including a guide defining a helical flow path along the axis of the chamber.
  • the arrangement of the inlet axially of the separating chamber reguires the apparatus to have separate means for inducing the swirl (previously provided by the tangential arrangement of the inlet) .
  • This means is provided by the guide defining a helical flow path along the axis of the chamber, preferably a multi-start helical flow path, preferably a four start helical flow path.
  • the phases separate out to different radii as a result of the swirl induced by the helical guide.
  • the continuous liguid phase being heavier, moves to the outside of the cylinder and may follow an involute path to a tangential offtake line.
  • the tangential outlet is handed so as to pick up the tangential flow of the heavier phase generated by the helical flow guide.
  • the less dense phase follows a path" closer to the axis to a separate axial exit which may lead to a diffuser and its separation may be assisted by a vortex finder.
  • the phase separation is more efficient if, after the separating chamber, the flow passes into a settling chamber such as a plain cylinder, from which the helical flow guide stops short.
  • the apparatus has the major advantages of compactness, low maintenance as it has no moving parts, and no requirement for liquid level control as in other types of separators. Because the inlet and the diffuser outlet are in line, the apparatus can be inserted in the line of a conduit or pipeline - this arangement is not possible when a tangential inlet for the two-phase mixture is used as in the case of cyclones.
  • FIG 1 is a plan of the apparatus, which is referred to as an inline Free Vortex Separator (IFV),
  • IVF inline Free Vortex Separator
  • Figure 2 is an end elevation of the tangential outlet of the apparatus of Figure 1
  • Figure 3 is a side elevation of the helical guide used in the apparatus of Figure 1,
  • Figure 4 shows a liquid separating system using two IFV units in series
  • Figure 5 shows a liquid separating system using two IFV units in parallel
  • Figure 6 shows a separator system using a conventional separator in conjunction with one IFV unit
  • Figure 7 shows an IFV unit used in conjunction with a primary pump and a jet pump
  • Figure 8 shows an IFV unit for separating liguid and solid phases.
  • the apparatus of Figure 1 is generally cylindrical with its longitudinal axis extending in the direction of arrow A. In this embodiment the axis is horizontal, but it could be vertical or at another orientation.
  • the two phases to be separated from each other enter the cylindrical conduit 11 of the apparatus from an axial inlet 12.
  • Within the inlet end 13 of the apparatus is a four-start helical guide 14 with turns extending from a central shaft 15 with pointed ends 16, as shown in Fig. 3. Each start makes one complete turn along the length of the guide 14.
  • the cylindrical conduit 11 is empty, forming a settling chamber 21.
  • the cylindrical conduit 11 is made up of flanged sections, bolted together by bolts 22 extending over the exterior of the upstream part of the settling chamber 21.
  • a vortex finder 25 in the form of a pipe in the axial region 28 of the chamber 21 extends into its outlet end 26 and leads to a diffuser 27.
  • the mixed phases enter the axial inlet 12. Swirl is induced in the mixture as it passes through the helical guide 14. In the settling chamber 21, the phases continue their swirling motion, becoming separated by centrifugal action, so that the heavier phase moves to the circumference and exits through the tangential outlet 23. The lighter phase (possibly with some of the heavier phase) continues along the axial region 28, where it is collected by the vortex finder 25 and is delivered to the diffuser 27.
  • the apparatus has the advantage of low maintenance because it has no moving parts. Because the inlet 12 and the diffuser outlet 26 are in line, the apparatus can be inserted in the line of a conduit - this arrangement is not possible when a tangential inlet for the two-phase mixture is used.
  • More than one such IFV unit can be used in series to improve the degree of gas liquid separation for the system, as in Fig. 4 when two IFV units 31 and 32 are arranged in series between a system input 33 and a system output 34 for the gas rich phase.
  • the liquid rich outputs are combined in a liquid manifold 35 to a liquid rich output 36.
  • several IFV units 41 and 42 can operate in parallel to handle a wider range of flow rates using a manifolding header 43.
  • Optional isolating valves 44 are provided in the gas rich outlets of the units 41 and 42, leading to a combined gas rich outlet 45; the liquid rich outlets are combined at 46.
  • the manifold system header 43 can then distribute the flow to one or more separators as desired by opening the appropriate valves which link each separator to the header.
  • FIG. 6 An alternative series arrangement is shown in Fig. 6 utilising an IFV unit with a conventional separator. This produces an improved system which could not be fully achieved with either (a) two IFVs in series or (b) two conventional separators in series.
  • the example of Fig. 6 could be used as a slug controller (a slug is a body of liguid flowing through the pipe separated by sections of gas or gas liquid mixture) .
  • the conventional separator is protected from being overloaded by the IFV unit which restricts the flow and partially separates the mixture thus reducing the work of the conventional separator.
  • the conventional separator 51 is a settling tank with a lower inlet for liquid rich mixture and an upper inlet for gas rich mixture.
  • a baffle 52 acts as a weir (there may be more than one baffle and additional baffles may be provided to disturb the gas flow in the upper region and encourage separation of liquid carried by a gas phase) . Additionally the use of the IFV enables the use of a much smaller separator and thus saves space and weight.
  • an IFV can be used to increase the maximum proportion of gas in a liquid gas mixture which can be handled by a pumping system, as illustrated in Fig.7.
  • the IFV 61 enables the pump 62 to operate within its acceptable range of gas void ratio by separating out some of the gas from the mixture so that the gas ratio in the branch 63 in which the pump is located is within the handling capacity of the pump. Excess gas bypasses the pump around the branch 64 and is recombined with the pump output by a jet pump 65 or similar phase combining apparatus.
  • the pump output forms the driving fluid of the jet pump and the branch 64 is connected to its suction input.
  • the IFV can be used to separate suspended solids from liquid solid mixtures such as slurries or sand produced with oil, as shown in Fig. 8.
  • a two phase flow (solid and liquid) is connected to the inlet 12 of the IFV, and its two outlets 23, 26 provide a liquid rich supply, which can be used in a process or pumping system, and solid rich supply which can be handled in a solids handling system.
  • the conventional separator 51 has two liquid outlets, one upstream of the baffle 52 and the other downstream.
  • the upstream outlet 53 is for heavier liquids which fail to flow over the baffle 52 and the downstream outlet 54 is for lighter liquids, such as oil.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Cyclones (AREA)

Abstract

Apparatus for separating phases (gas, liquid, solid) comprises a chamber (11) with an axial inlet (12) and means (14) within the chamber for inducing a swirl in the phase mixture received from the inlet, the means comprising a guide defining a helical flow path along the axis of the apparatus. The mixture will tend to separate with heavier components radially outwardly of the lighter components and separate outlets (23, 26) are provided for the different density components. The apparatus can be used alone or in conjunction with conventional separators and other flow handling apparatus.

Description

PHASE SEPARATION APPARATUS
Cyclone phase separators operate by centrifugal action on multiphase material to separate the phases. Usually the material enters a separating chamber through a tangential inlet in order to generate a swirl component of flow. The material flows around the chamber, the heavier material moving to the outside and the lighter material towards the axis of the chamber by centrifugal action. Separate outlets for the two phases are arranged near the periphery and the axis of the chamber.
The present invention is concerned with separation of phases, eg a continuous liguid phase from gas or solids. The phase separating apparatus comprises a separating chamber having an inlet for a phase mixture and radially separated outlets for phases of different densities, the inlet being located axially of the chamber. The apparatus comprises means for inducing a swirl in the phase mixture from said inlet, said means including a guide defining a helical flow path along the axis of the chamber.
The arrangement of the inlet axially of the separating chamber reguires the apparatus to have separate means for inducing the swirl (previously provided by the tangential arrangement of the inlet) . This means is provided by the guide defining a helical flow path along the axis of the chamber, preferably a multi-start helical flow path, preferably a four start helical flow path.
The phases separate out to different radii as a result of the swirl induced by the helical guide. The continuous liguid phase, being heavier, moves to the outside of the cylinder and may follow an involute path to a tangential offtake line. Clearly the tangential outlet is handed so as to pick up the tangential flow of the heavier phase generated by the helical flow guide. The less dense phase follows a path" closer to the axis to a separate axial exit which may lead to a diffuser and its separation may be assisted by a vortex finder. The phase separation is more efficient if, after the separating chamber, the flow passes into a settling chamber such as a plain cylinder, from which the helical flow guide stops short.
The apparatus has the major advantages of compactness, low maintenance as it has no moving parts, and no requirement for liquid level control as in other types of separators. Because the inlet and the diffuser outlet are in line, the apparatus can be inserted in the line of a conduit or pipeline - this arangement is not possible when a tangential inlet for the two-phase mixture is used as in the case of cyclones.
An example of the invention will now be described with reference to the accompanying drawings in which
Figure 1 is a plan of the apparatus, which is referred to as an inline Free Vortex Separator (IFV),
Figure 2 is an end elevation of the tangential outlet of the apparatus of Figure 1,
Figure 3 is a side elevation of the helical guide used in the apparatus of Figure 1,
Figure 4 shows a liquid separating system using two IFV units in series,
Figure 5 shows a liquid separating system using two IFV units in parallel, Figure 6 shows a separator system using a conventional separator in conjunction with one IFV unit,
Figure 7 shows an IFV unit used in conjunction with a primary pump and a jet pump, and
Figure 8 shows an IFV unit for separating liguid and solid phases.
The apparatus of Figure 1 is generally cylindrical with its longitudinal axis extending in the direction of arrow A. In this embodiment the axis is horizontal, but it could be vertical or at another orientation. The two phases to be separated from each other enter the cylindrical conduit 11 of the apparatus from an axial inlet 12. Within the inlet end 13 of the apparatus is a four-start helical guide 14 with turns extending from a central shaft 15 with pointed ends 16, as shown in Fig. 3. Each start makes one complete turn along the length of the guide 14. Beyond the helical guide 14, the cylindrical conduit 11 is empty, forming a settling chamber 21. In this example the cylindrical conduit 11 is made up of flanged sections, bolted together by bolts 22 extending over the exterior of the upstream part of the settling chamber 21.
Beyond the settling chamber 21 is a tangential outlet 23 leading to a heavy phase outlet pipe 24. A vortex finder 25 in the form of a pipe in the axial region 28 of the chamber 21 extends into its outlet end 26 and leads to a diffuser 27.
The mixed phases enter the axial inlet 12. Swirl is induced in the mixture as it passes through the helical guide 14. In the settling chamber 21, the phases continue their swirling motion, becoming separated by centrifugal action, so that the heavier phase moves to the circumference and exits through the tangential outlet 23. The lighter phase (possibly with some of the heavier phase) continues along the axial region 28, where it is collected by the vortex finder 25 and is delivered to the diffuser 27.
The apparatus has the advantage of low maintenance because it has no moving parts. Because the inlet 12 and the diffuser outlet 26 are in line, the apparatus can be inserted in the line of a conduit - this arrangement is not possible when a tangential inlet for the two-phase mixture is used.
More than one such IFV unit can be used in series to improve the degree of gas liquid separation for the system, as in Fig. 4 when two IFV units 31 and 32 are arranged in series between a system input 33 and a system output 34 for the gas rich phase. The liquid rich outputs are combined in a liquid manifold 35 to a liquid rich output 36. As shown in Fig. 5, several IFV units 41 and 42 can operate in parallel to handle a wider range of flow rates using a manifolding header 43. Optional isolating valves 44 are provided in the gas rich outlets of the units 41 and 42, leading to a combined gas rich outlet 45; the liquid rich outlets are combined at 46. This arrangement particularly suits production conditions with major changes to the flow rate such as turn-down conditions when one or more of the units can be isolated, allowing each separator to operate under its optimum range in all conditions. The manifold system header 43 can then distribute the flow to one or more separators as desired by opening the appropriate valves which link each separator to the header.
An alternative series arrangement is shown in Fig. 6 utilising an IFV unit with a conventional separator. This produces an improved system which could not be fully achieved with either (a) two IFVs in series or (b) two conventional separators in series. The example of Fig. 6 could be used as a slug controller (a slug is a body of liguid flowing through the pipe separated by sections of gas or gas liquid mixture) . The conventional separator is protected from being overloaded by the IFV unit which restricts the flow and partially separates the mixture thus reducing the work of the conventional separator. The conventional separator 51 is a settling tank with a lower inlet for liquid rich mixture and an upper inlet for gas rich mixture. A baffle 52 acts as a weir (there may be more than one baffle and additional baffles may be provided to disturb the gas flow in the upper region and encourage separation of liquid carried by a gas phase) . Additionally the use of the IFV enables the use of a much smaller separator and thus saves space and weight.
As is described in copending application PCT/GB92/01811, an IFV can be used to increase the maximum proportion of gas in a liquid gas mixture which can be handled by a pumping system, as illustrated in Fig.7. The IFV 61 enables the pump 62 to operate within its acceptable range of gas void ratio by separating out some of the gas from the mixture so that the gas ratio in the branch 63 in which the pump is located is within the handling capacity of the pump. Excess gas bypasses the pump around the branch 64 and is recombined with the pump output by a jet pump 65 or similar phase combining apparatus. In this example the pump output forms the driving fluid of the jet pump and the branch 64 is connected to its suction input.
The IFV can be used to separate suspended solids from liquid solid mixtures such as slurries or sand produced with oil, as shown in Fig. 8. A two phase flow (solid and liquid) is connected to the inlet 12 of the IFV, and its two outlets 23, 26 provide a liquid rich supply, which can be used in a process or pumping system, and solid rich supply which can be handled in a solids handling system.
In the arrangement of Figure 6, the conventional separator 51 has two liquid outlets, one upstream of the baffle 52 and the other downstream. The upstream outlet 53 is for heavier liquids which fail to flow over the baffle 52 and the downstream outlet 54 is for lighter liquids, such as oil.

Claims

1. Phase separating apparatus comprising a separating chamber having an inlet for a phase mixture and radially separated outlets for phases of different densities, characterised in that said inlet is located axially of the chamber and the apparatus comprises means for inducing a swirl in the phase mixture from said inlet, said means including a guide defining a helical flow path along the axis of the chamber.
2. Apparatus as claimed in claim 1 wherein said path is a multi-start helical flow path.
3. Apparatus as claimed in claim 2 wherein said path is a four-start helical flow path.
4. Apparatus as claimed in any one of claims 1 to 3 comprising a settling chamber downstream of the separating chamber and upstream of said outlets.
5. Apparatus as claimed in any of claims 1 to 4 wherein the or an inner outlet comprises a vortex finder in the axial region of the apparatus, such apparatus as claimed in claim 5 comprising a diffuser downstream of the said vortex finder.
6. Apparatus as claimed in any one of the preceding claims wherein the or an outer outlet is arranged tangentially of the apparatus.
7. The combination of apparatus as claimed in any one of claims 1 to 6 with a separator having separate inlets for phase mixtures of different densities, the apparatus as claimed in any one of the preceding claims being arranged downstream of said other separator, the two separators acting in series.
8. The combination of apparatus as claimed in any one of claims 1 to 6 with a primary pump and a jet pump having its pressure inlet connected to the outlet of the primary pump, the heavier phase outlet of said apparatus being connected to the inlet of the primary pump and the lighter phase outlet of the said apparatus being connected to the suction inlet of the jet pump.
9. Apparatus as claimed in any one of claims 1 to 6 in combination with means for feeding a liquid solid mixture to the inlet of said apparatus and means for receiving solids from said heavier phase outlet and liquids from said lighter phase outlet.
PCT/GB1992/002089 1991-11-11 1992-11-11 Phase separation apparatus WO1993009875A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9123883A GB9123883D0 (en) 1991-11-11 1991-11-11 Hydrocyclone
GB9123883.2 1991-11-11

Publications (1)

Publication Number Publication Date
WO1993009875A1 true WO1993009875A1 (en) 1993-05-27

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PCT/GB1992/002089 WO1993009875A1 (en) 1991-11-11 1992-11-11 Phase separation apparatus

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WO (1) WO1993009875A1 (en)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5830368A (en) * 1994-04-13 1998-11-03 Centre For Engineering Research Inc. Method for borehole separation of oil and water in an oil well
US6162021A (en) * 1993-09-06 2000-12-19 B.H.R. Group Limited System for pumping liquids using a jet pump and a phase separator
US6189613B1 (en) 1998-09-25 2001-02-20 Pan Canadian Petroleum Limited Downhole oil/water separation system with solids separation
US6398973B1 (en) 1997-11-04 2002-06-04 B.H.R. Group Limited Cyclone separator
US6531066B1 (en) 1997-11-04 2003-03-11 B.H.R. Group Limited Cyclone separator
US6761215B2 (en) * 2002-09-06 2004-07-13 James Eric Morrison Downhole separator and method
WO2004073829A1 (en) * 2003-02-20 2004-09-02 Statoil Asa Slug inhibition
WO2004080566A1 (en) * 2003-03-12 2004-09-23 Statoil Asa Multiphase flow handling
DK177930B1 (en) * 2008-02-28 2015-01-19 Statoil Petroleum As Separation and capture of liquids in a multiphase flow

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE514224A (en) *
FR1019343A (en) * 1950-05-31 1953-01-20 Rechauffeurs D Air Aireco Soc Improvements to the construction of centrifugal dust collection devices
US3517821A (en) * 1968-11-29 1970-06-30 Donaldson Co Inc Deflecting element for centrifugal separators
EP0028996A1 (en) * 1979-11-08 1981-05-20 SOCIETE LAB Société à Responsabilité française Centrifugal separators of the cyclonic type
GB2122923A (en) * 1982-06-24 1984-01-25 Atomic Energy Authority Uk Apparatus for the removal and collection of solids in a gas flow
FR2629371A1 (en) * 1988-03-29 1989-10-06 Stumm Eric Device for separating dust from industrial gases by pneumatic-mechanical separators
EP0344748A2 (en) * 1988-06-02 1989-12-06 Cyclofil (Proprietary) Limited Vortex tube separating device

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE514224A (en) *
FR1019343A (en) * 1950-05-31 1953-01-20 Rechauffeurs D Air Aireco Soc Improvements to the construction of centrifugal dust collection devices
US3517821A (en) * 1968-11-29 1970-06-30 Donaldson Co Inc Deflecting element for centrifugal separators
EP0028996A1 (en) * 1979-11-08 1981-05-20 SOCIETE LAB Société à Responsabilité française Centrifugal separators of the cyclonic type
GB2122923A (en) * 1982-06-24 1984-01-25 Atomic Energy Authority Uk Apparatus for the removal and collection of solids in a gas flow
FR2629371A1 (en) * 1988-03-29 1989-10-06 Stumm Eric Device for separating dust from industrial gases by pneumatic-mechanical separators
EP0344748A2 (en) * 1988-06-02 1989-12-06 Cyclofil (Proprietary) Limited Vortex tube separating device

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6162021A (en) * 1993-09-06 2000-12-19 B.H.R. Group Limited System for pumping liquids using a jet pump and a phase separator
US5830368A (en) * 1994-04-13 1998-11-03 Centre For Engineering Research Inc. Method for borehole separation of oil and water in an oil well
US6398973B1 (en) 1997-11-04 2002-06-04 B.H.R. Group Limited Cyclone separator
US6531066B1 (en) 1997-11-04 2003-03-11 B.H.R. Group Limited Cyclone separator
US6189613B1 (en) 1998-09-25 2001-02-20 Pan Canadian Petroleum Limited Downhole oil/water separation system with solids separation
US6761215B2 (en) * 2002-09-06 2004-07-13 James Eric Morrison Downhole separator and method
WO2004073829A1 (en) * 2003-02-20 2004-09-02 Statoil Asa Slug inhibition
WO2004080566A1 (en) * 2003-03-12 2004-09-23 Statoil Asa Multiphase flow handling
DK177930B1 (en) * 2008-02-28 2015-01-19 Statoil Petroleum As Separation and capture of liquids in a multiphase flow

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