WO2004073829A1 - Slug inhibition - Google Patents

Slug inhibition Download PDF

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Publication number
WO2004073829A1
WO2004073829A1 PCT/NO2004/000037 NO2004000037W WO2004073829A1 WO 2004073829 A1 WO2004073829 A1 WO 2004073829A1 NO 2004000037 W NO2004000037 W NO 2004000037W WO 2004073829 A1 WO2004073829 A1 WO 2004073829A1
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WO
WIPO (PCT)
Prior art keywords
liquid
control system
gas
deliquidizer
control
Prior art date
Application number
PCT/NO2004/000037
Other languages
French (fr)
Inventor
Alf Reidar Kluge
Original Assignee
Statoil Asa
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 Statoil Asa filed Critical Statoil Asa
Publication of WO2004073829A1 publication Critical patent/WO2004073829A1/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces

Definitions

  • the present invention relates to inhibition of liquid slugs, stabilization of flow and preseparation of liquid from gas from pipelines that in substance conduct gas, such as gas pipelines and wet gas pipelines, wherein a compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator are arranged either at the outlet, inlet or both outlet and inlet of the pipeline. More specifically the invention relates to a control system based on using the compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator, for liquid slug inhibition, flow stabilisation and preseparation of liquid from gas from a pipeline that in substance conducts gas.
  • liquid slugs can be a serious problem, particularly with respect to start-up of the flow or increase of the flow rate. Particularly at low points along the pipeline liquid will accumulate, and particularly after a shutdown where the pipeline contents has been cooled down.
  • a liquid slug is formed when the complete pipeline cross section comprises liquid. Liquid slugs (slugs) flow upon start-up of the pipeline as powerful, pulsating liquid flows that require a powerful dimensioning of downstream arranged separation equipment.
  • a control system for slug inhibition, flow stabilization and preseparation of liquid from gas from a pipeline that in substance conducts gas, wherein a compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator are arranged either at the outlet, inlet or both outlet and inlet of the pipeline, said control system being distinguished in that it comprises; devices for automatic control of liquid drainage from the deliquidizer and inlet separator, devices for automatic control of gas takeoff from the deliquidizer and inlet separator, and protective functions.
  • the control system according to the present invention is particularly preferable if transmitters for flow information in the pipeline are connected, such as transmitters for flow rate, flow composition and flow pressure.
  • control system is particularly preferable if differential pressure is measured over an antispin element located at the outlet of the deliquidizer, since such measurements results in a very quick adaption of the control system to avoid that liquid is passed over the antispin element and further into the gas outlet.
  • FIG. 1 is a schematic illustration of the control system with deliquidizer, inlet separator and field instruments
  • FIG. 2 illustrates the most preferred embodiment of the control system according to the present invention.
  • the inlet separator is in principle a compact separator that is arranged to collect liquid when the draining capacity of the deliquidizer is exceeded, such that liquid is not passed to gas handling equipment arranged downstream, such as compressors.
  • the capacity of the deliquidizer for liquid handling can be exceeded at start-up of a gas pipeline, at commencement of operation after a shutdown, or when the flow rate through the pipeline is increased, which may result in flow transients and problems with liquid slug formation while the flow pattern adapts from one steady state to another.
  • the inlet separator is much smaller than downstream arranged equipment.
  • the dimensioning of the inlet separator is such that the volume is to provide desired residence time for received liquid.
  • the difference in the flow rate of liquid in and out of the inlet separator, times the desired residence time, determines the required volume to handle liquid.
  • liquid is not to be entrained with the gas and the gas is not to be entrained with the liquid, and the volumes of liquid and gas must be sufficient for the response time of the control system to allow the desired functionality.
  • Liquid draining from the deliquidizer is primarily controlled by the valve FV1000, such as illustrated with LC on Figure 1.
  • the liquid drainage from the inlet separator is controlled primarily with the valve FV2000, such as illustrated with LC on Figure 1.
  • the gas takeoff from the inlet separator is primarily controlled by the valve FV3000, such as illustrated with FC on Figure 1.
  • the controlling means are only partly illustrated on Figure 1.
  • protective functions are arranged to hinder passing liquid into the gas outlet and passing gas into the liquid outlet.
  • the main control of the protective functions is to valve XVI 500 for the gas outlet and valve XVI 600 for the liquid outlet, respectively, as illustrated by CF for the respective valves.
  • Liquid separated from the gas that flows through the deliquidizer is collected in the outlet means for liquid in the deliquidizer. Said liquid is drained from the outlet means under level control by LCI 000, that is used to control FV 1000 via FC1000, as illustrated on Figure 2.
  • FT1000 is considered to measure the flow rate of liquid directly. Further, it is considered that the liquid density DTI 000 is available from equipment for measurement of mass flow rate.
  • the density D1000 is used to correct the level measurement LI 000 for deviation because of varying liquid density, given that LT1000 is based on measurement of the differential pressure over and through the upper part of the liquid. In general the liquid that arrives the deliquidizer will contain varying fractions of water, glycol and hydrocarbon components. The correction is illustrated with the function symbol f(x) connected to LCI 000.
  • Level control for liquid drainage from the inlet separator VL1000 takes place by the level L2000 controlled by LC2000A, which is effective on FV2000 via FC2000, as illustrated on Figure 2.
  • LC2000A which is effective on FV2000 via FC2000, as illustrated on Figure 2.
  • FC2000 is arranged to achieve decoupling with L2000 and PI 000.
  • the inlet separator has compensation of level measurements because of prevailing density variations, such as illustrated with f(x) connected to LC2000A.
  • Liquids arriving the inlet separator may vary in density from pure glycol to water to pure condensate, and all mixing ratios in between.
  • the level L2000 will therefore be effected by said variation if the level measurement takes place according to differential pressure.
  • As the residence volume for liquid in the inlet separator is assumed to be small and the density of the liquid is measured at the liquid outlet from the deliquidizer, said density measurement is used for density compensation, as illustrated on Figure 2.
  • Differential pressure DP2000 over the antispin element of the deliquidizer is used as feed forward to the liquid outlet from the inlet separator, as illustrated on Figure 2 by the connection between DPT2000 and FC2000.
  • the control with feed forward is based on the ratio control principle, and will promote an increasing liquid drainage before an increased level L2000 is detected in the inlet separator.
  • the differential pressure signal is manipulated to achieve appropriate linearization.
  • the feed forward functions only when the liquid quantity arriving the deliquidizer exceeds the capacity for liquid handling, such that liquid can be entrained the gas arriving the inlet separator. When liquid is entrained with the gas over the antispin element, a significant pressure increase will result.
  • the fluid that arrives the deliquidizer will contain little liquid, and liquid drained from the deliquidizer as well as gas from the deliquidizer can arrive the inlet separator, as this minimizes the risk for passing gas through the liquid drainage of the deliquidizer to equipment arranged downstream for liquid handling. If by use of DPT2000 it is detected that liquid is entrained with the gas from the deliquidizer, the liquid drain from the deliquidizer can by-pass the inlet separator by closing the valve HV2000 and opening the valve HV1000, which is illustrated on Figure 2 with the connection between the signal from DPT2000 and said valves.
  • the gas takeoff from the inlet separator is controlled automatically.
  • the control is achieved by having the valve FV3000 in the gas outlet from the inlet separator be controlled based on the pressure in the inlet separator, provided by use of the pressure transmitter PT1000.
  • the valve F V3000 in the gas outlet line from the inlet separator is controlled by use of the flow controller FC3000 that is ⁇ Gonnected different equipment for compensation of the control to take into account the mass balance, illustrated by the feed forward connections on Figure 2.
  • the mass balance of the pipeline is in general maintained by adjusting the set point of FC 1000 as required, to keep the variations in the pipeline pressure within acceptable limits.
  • the total mass flow functions as a feed forward to PC 1000, which again is used to adjust the internal mass balance of the pipeline to keep the outlet pressure of the pipeline within limits as defined by the set point of PC 1000.
  • a further stabilization is achieved by installing a pressure controller PC2000 upstream in the pipeline, for example close to the well head or at the bottom of a riser.
  • PC2000 can be connected to PC 1000 as illustrated on Figure 2, or alternatively the connection can be directly to FC3000.
  • the protective functions for the control system comprise protection against overfilling the inlet separator and protection against passing gas into the inlet separator such that gas is not to enter the liquid outlet. Hence, protection of downstream equipment is achieved, protection of the control system per se, in addition to said protective functions being essential to provide automatic control, particularly automatic start-up and shutdown.
  • the feedback functioning level control LC2000B will override FC4000 for choking FV3000 via FC3000.
  • FC4000 By further overfilling of the inlet separator the gas isolation outlet valve XVI 500 will be closed, after which also FV3000 will be commanded closed, to protect the connected units of the control system.
  • a leak proof shutdown valve XVI 600 is arranged in the outlet line for liquid to achieve further safety against passing of gas to the liquid outlet than achievable by the valve FV2000 alone, as illustrated on Figure 2. By closing XVI 600 also FV2000 will be closed to protect connected units of the control system.
  • shutdown valve for gas XVI 500 and/or shutdown valve for liquid XVI 600 will be closed, respectively, such as illustrated with the symbols PSD on Figure 2.
  • control system The most preferred embodiment of the control system according to the present invention is the embodiment illustrated on Figure 2.
  • control system can preferably be adapted to the prevailing process requirements.
  • Preferably all variables are monitored since equipment for such monitoring is standard functionality on commonly used SAS (Safety and Automation System).
  • the cycle time for the control system implemented in SAS is preferably less than 0.5 sec. All control units and control functions are preferably provided with bumpless transfer between the different control modes manual, automatic and cascade.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Cyclones (AREA)
  • Pipeline Systems (AREA)

Abstract

Control system for liquid slug inhibition, flow stabilization and preseparation of liquid from gas from a pipeline that in substance conducts gas, in that a compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator is arranged either at the outlet, inlet or both outlet and inlet of the pipeline. Control system is distinguished in that it is comprising: means for automatic control of liquid drainage from the deliquidizer and inlet separator, means for automatic control of gas take-off from the deliquidizer and inlet separator, and protective functions.

Description

Slug inhibition
Field of the invention
The present invention relates to inhibition of liquid slugs, stabilization of flow and preseparation of liquid from gas from pipelines that in substance conduct gas, such as gas pipelines and wet gas pipelines, wherein a compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator are arranged either at the outlet, inlet or both outlet and inlet of the pipeline. More specifically the invention relates to a control system based on using the compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator, for liquid slug inhibition, flow stabilisation and preseparation of liquid from gas from a pipeline that in substance conducts gas.
Background of the invention and prior art
In multiphase pipelines that in substance conduct gas, or gas pipelines where the gas is not completely dried, liquid slugs can be a serious problem, particularly with respect to start-up of the flow or increase of the flow rate. Particularly at low points along the pipeline liquid will accumulate, and particularly after a shutdown where the pipeline contents has been cooled down. A liquid slug is formed when the complete pipeline cross section comprises liquid. Liquid slugs (slugs) flow upon start-up of the pipeline as powerful, pulsating liquid flows that require a powerful dimensioning of downstream arranged separation equipment.
Known equipment is relatively expensive and require relatively large space, which constitutes a problem, particularly for surface installations off shore.
A demand exists for equipment that substantially reduces the above-mentioned problem.
Compact equipment for liquid separation that would be particularly feasible to use exists. More specifically, in patent publication NO 2000 6656 it is described a particularly preferable deliquidizer in form of a compact in-line cyclone based device for separation of liquid from a multiphase fluid flow that flows through a pipeline, wherein the fluid flow is set into rotation such that it is separated into a central zone that in substance contains gas and an outer annular zone that in substance contains liquid, from which zones gas and liquid can be taken out via respective outlet devices.
Summary of the invention
With the present invention a control system is provided for slug inhibition, flow stabilization and preseparation of liquid from gas from a pipeline that in substance conducts gas, wherein a compact cyclone based deliquidizer with a downstream connected compact multiphase inlet separator are arranged either at the outlet, inlet or both outlet and inlet of the pipeline, said control system being distinguished in that it comprises; devices for automatic control of liquid drainage from the deliquidizer and inlet separator, devices for automatic control of gas takeoff from the deliquidizer and inlet separator, and protective functions.
The control system according to the present invention is particularly preferable if transmitters for flow information in the pipeline are connected, such as transmitters for flow rate, flow composition and flow pressure.
Further, the control system is particularly preferable if differential pressure is measured over an antispin element located at the outlet of the deliquidizer, since such measurements results in a very quick adaption of the control system to avoid that liquid is passed over the antispin element and further into the gas outlet.
Drawings
The invention is illustrated with two figures, of which:
Figure 1 is a schematic illustration of the control system with deliquidizer, inlet separator and field instruments,
Figure 2 illustrates the most preferred embodiment of the control system according to the present invention.
Detailed description
Firstly reference is made to Figure 1, on which the deliquidizer, inlet separator and field instruments are illustrated. The deliquidizer is described further in patent publication NO 2000 6656, and reference is made to said publication. The inlet separator is in principle a compact separator that is arranged to collect liquid when the draining capacity of the deliquidizer is exceeded, such that liquid is not passed to gas handling equipment arranged downstream, such as compressors. The capacity of the deliquidizer for liquid handling can be exceeded at start-up of a gas pipeline, at commencement of operation after a shutdown, or when the flow rate through the pipeline is increased, which may result in flow transients and problems with liquid slug formation while the flow pattern adapts from one steady state to another. The inlet separator is much smaller than downstream arranged equipment. The dimensioning of the inlet separator is such that the volume is to provide desired residence time for received liquid. The difference in the flow rate of liquid in and out of the inlet separator, times the desired residence time, determines the required volume to handle liquid. In addition it is taken into account that liquid is not to be entrained with the gas and the gas is not to be entrained with the liquid, and the volumes of liquid and gas must be sufficient for the response time of the control system to allow the desired functionality.
Liquid draining from the deliquidizer is primarily controlled by the valve FV1000, such as illustrated with LC on Figure 1. The liquid drainage from the inlet separator is controlled primarily with the valve FV2000, such as illustrated with LC on Figure 1. The gas takeoff from the inlet separator is primarily controlled by the valve FV3000, such as illustrated with FC on Figure 1. For clarity the controlling means are only partly illustrated on Figure 1.
To protect downstream arranged equipment and the control system per se, protective functions are arranged to hinder passing liquid into the gas outlet and passing gas into the liquid outlet. The main control of the protective functions is to valve XVI 500 for the gas outlet and valve XVI 600 for the liquid outlet, respectively, as illustrated by CF for the respective valves.
In the following the control system will be described in further detail, and reference is in this connection made to Figure 2 that illustrates a completely equipped embodiment of the control system according to the present invention.
Liquid separated from the gas that flows through the deliquidizer is collected in the outlet means for liquid in the deliquidizer. Said liquid is drained from the outlet means under level control by LCI 000, that is used to control FV 1000 via FC1000, as illustrated on Figure 2. FT1000 is considered to measure the flow rate of liquid directly. Further, it is considered that the liquid density DTI 000 is available from equipment for measurement of mass flow rate. The density D1000 is used to correct the level measurement LI 000 for deviation because of varying liquid density, given that LT1000 is based on measurement of the differential pressure over and through the upper part of the liquid. In general the liquid that arrives the deliquidizer will contain varying fractions of water, glycol and hydrocarbon components. The correction is illustrated with the function symbol f(x) connected to LCI 000.
Level control for liquid drainage from the inlet separator VL1000 takes place by the level L2000 controlled by LC2000A, which is effective on FV2000 via FC2000, as illustrated on Figure 2. As VL1000 is assumed to be small, FC2000 is arranged to achieve decoupling with L2000 and PI 000.
Also the inlet separator has compensation of level measurements because of prevailing density variations, such as illustrated with f(x) connected to LC2000A. Liquids arriving the inlet separator may vary in density from pure glycol to water to pure condensate, and all mixing ratios in between. The level L2000 will therefore be effected by said variation if the level measurement takes place according to differential pressure. As the residence volume for liquid in the inlet separator is assumed to be small and the density of the liquid is measured at the liquid outlet from the deliquidizer, said density measurement is used for density compensation, as illustrated on Figure 2. Differential pressure DP2000 over the antispin element of the deliquidizer is used as feed forward to the liquid outlet from the inlet separator, as illustrated on Figure 2 by the connection between DPT2000 and FC2000. The control with feed forward is based on the ratio control principle, and will promote an increasing liquid drainage before an increased level L2000 is detected in the inlet separator. The differential pressure signal is manipulated to achieve appropriate linearization. The feed forward functions only when the liquid quantity arriving the deliquidizer exceeds the capacity for liquid handling, such that liquid can be entrained the gas arriving the inlet separator. When liquid is entrained with the gas over the antispin element, a significant pressure increase will result.
At normal operational conditions the fluid that arrives the deliquidizer will contain little liquid, and liquid drained from the deliquidizer as well as gas from the deliquidizer can arrive the inlet separator, as this minimizes the risk for passing gas through the liquid drainage of the deliquidizer to equipment arranged downstream for liquid handling. If by use of DPT2000 it is detected that liquid is entrained with the gas from the deliquidizer, the liquid drain from the deliquidizer can by-pass the inlet separator by closing the valve HV2000 and opening the valve HV1000, which is illustrated on Figure 2 with the connection between the signal from DPT2000 and said valves.
The gas takeoff from the inlet separator is controlled automatically. In principle the control is achieved by having the valve FV3000 in the gas outlet from the inlet separator be controlled based on the pressure in the inlet separator, provided by use of the pressure transmitter PT1000. However, the valve F V3000 in the gas outlet line from the inlet separator is controlled by use of the flow controller FC3000 that isΛGonnected different equipment for compensation of the control to take into account the mass balance, illustrated by the feed forward connections on Figure 2. The mass balance of the pipeline is in general maintained by adjusting the set point of FC 1000 as required, to keep the variations in the pipeline pressure within acceptable limits. By summarizing the quantity of liquid arriving the inlet separator with the gas flow rate, and providing said value as a process parameter for FC1000, the total mass flow functions as a feed forward to PC 1000, which again is used to adjust the internal mass balance of the pipeline to keep the outlet pressure of the pipeline within limits as defined by the set point of PC 1000.
In addition to the above-mentioned stabilization of the pipeline flow a further stabilization is achieved by installing a pressure controller PC2000 upstream in the pipeline, for example close to the well head or at the bottom of a riser. PC2000 can be connected to PC 1000 as illustrated on Figure 2, or alternatively the connection can be directly to FC3000.
The protective functions for the control system comprise protection against overfilling the inlet separator and protection against passing gas into the inlet separator such that gas is not to enter the liquid outlet. Hence, protection of downstream equipment is achieved, protection of the control system per se, in addition to said protective functions being essential to provide automatic control, particularly automatic start-up and shutdown.
By overfilling of the inlet separator the feedback functioning level control LC2000B will override FC4000 for choking FV3000 via FC3000. By further overfilling of the inlet separator the gas isolation outlet valve XVI 500 will be closed, after which also FV3000 will be commanded closed, to protect the connected units of the control system.
A leak proof shutdown valve XVI 600 is arranged in the outlet line for liquid to achieve further safety against passing of gas to the liquid outlet than achievable by the valve FV2000 alone, as illustrated on Figure 2. By closing XVI 600 also FV2000 will be closed to protect connected units of the control system.
If downstream arranged equipment has to be shutdown, shutdown valve for gas XVI 500 and/or shutdown valve for liquid XVI 600 will be closed, respectively, such as illustrated with the symbols PSD on Figure 2.
The most preferred embodiment of the control system according to the present invention is the embodiment illustrated on Figure 2. However, the control system can preferably be adapted to the prevailing process requirements. Preferably all variables are monitored since equipment for such monitoring is standard functionality on commonly used SAS (Safety and Automation System).
The cycle time for the control system implemented in SAS is preferably less than 0.5 sec. All control units and control functions are preferably provided with bumpless transfer between the different control modes manual, automatic and cascade.

Claims

C l a i m s
1. Control system for liquid slug inhibition, flow stabilization and preseparation of liquid from gas from a pipeline that in substance conducts gas, wherein a compact cyclor based deliquidizer with a downstream connected compact multiphase inlet separator are arranged either at the outlet, inlet or both outlet and inlet of the pipeline, characterized in that the control system is comprising: means for automatic control of liquid drainage from the deliquidizer and inlet separator, means for automatic control of gas takeoff from the deliquidizer and inlet separator, and protective functions.
2. Control system according to claim 1, characterized in that the means for automatic control of liquid drainage from the deliquidizer and inlet separator both are based on level signals from said units, said control being corrected according to fed forward measured values for density and flow rate.
3. Control system according to claim 1, characterized in that the means for automatic control of gas takeoff from the deliquidizer and inlet separator are based on pressure control corrected according to fed forward measured values for density and flow rate.
4. Control system according to claim 1-3, characterized in that it is comprising at least one automatic protection function against passing liquid through the gas outlet.
5. Control system according to claim 1-4, characterized in that it is comprising at least one automatic protection function against passing gas through the liquid outlet.
6. Control system according to claim 1, characterized in that means are arranged for measuring differential pressure over an antispin element in the outlet for gas from the deliquidizer, which measured differential pressure is fed forward to units that control liquid drainage, to avoid liquid flooding of the inlet separator.
7. Control system according to claim 1-6, characterized in that at least one means for flow rate measurement in the pipeline is connected to the control system, for increased flow stabilization in the pipeline.
8. Control system according to claims 1-7, characterized in that the response time for any control loop of the control system is less than 0.5 sec.
PCT/NO2004/000037 2003-02-20 2004-02-09 Slug inhibition WO2004073829A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO20030797A NO319642B1 (en) 2003-02-20 2003-02-20 Control system for liquid plug prevention, flow stabilization and gas separation from liquid from a pipeline which mainly conducts gas
NO20030797 2003-02-20

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WO2004073829A1 true WO2004073829A1 (en) 2004-09-02

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1297779C (en) * 2005-05-19 2007-01-31 西安交通大学 Valve throttle dynamic control method for eliminating serious slug flow
US9901847B2 (en) 2011-12-22 2018-02-27 Statoil Petroleum As Method and system for fluid separation with an integrated control system

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NO324906B1 (en) * 2005-05-10 2008-01-02 Abb Research Ltd Procedure and system for improved flow line regulation

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993009875A1 (en) * 1991-11-11 1993-05-27 B.H.R. Group Limited Phase separation apparatus
WO2001000296A1 (en) * 1999-06-28 2001-01-04 Statoil Asa An apparatus for separation of a fluid flow, especially into a gas phase and a liquid phase
US6402820B1 (en) * 1997-12-23 2002-06-11 The University Of Sheffield Fluidic level control systems
WO2002056999A1 (en) * 2000-12-22 2002-07-25 Statoil Asa An apparatus for separation of a liquid from a multiphase fluid flow

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993009875A1 (en) * 1991-11-11 1993-05-27 B.H.R. Group Limited Phase separation apparatus
US6402820B1 (en) * 1997-12-23 2002-06-11 The University Of Sheffield Fluidic level control systems
WO2001000296A1 (en) * 1999-06-28 2001-01-04 Statoil Asa An apparatus for separation of a fluid flow, especially into a gas phase and a liquid phase
WO2002056999A1 (en) * 2000-12-22 2002-07-25 Statoil Asa An apparatus for separation of a liquid from a multiphase fluid flow

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1297779C (en) * 2005-05-19 2007-01-31 西安交通大学 Valve throttle dynamic control method for eliminating serious slug flow
US9901847B2 (en) 2011-12-22 2018-02-27 Statoil Petroleum As Method and system for fluid separation with an integrated control system

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Publication number Publication date
NO319642B1 (en) 2005-09-05
NO20030797L (en) 2004-08-23
NO20030797D0 (en) 2003-02-20

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