WO1996009895A1 - Traitement de materiau particulaire - Google Patents

Traitement de materiau particulaire Download PDF

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Publication number
WO1996009895A1
WO1996009895A1 PCT/GB1995/002315 GB9502315W WO9609895A1 WO 1996009895 A1 WO1996009895 A1 WO 1996009895A1 GB 9502315 W GB9502315 W GB 9502315W WO 9609895 A1 WO9609895 A1 WO 9609895A1
Authority
WO
WIPO (PCT)
Prior art keywords
sand
hydrocyclone
vessel
water
slurry
Prior art date
Application number
PCT/GB1995/002315
Other languages
English (en)
Inventor
Neville Ernest Lange
Original Assignee
Serck Baker 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 Serck Baker Limited filed Critical Serck Baker Limited
Publication of WO1996009895A1 publication Critical patent/WO1996009895A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B9/00—General arrangement of separating plant, e.g. flow sheets
    • B03B9/02—General arrangement of separating plant, e.g. flow sheets specially adapted for oil-sand, oil-chalk, oil-shales, ozokerite, bitumen, or the like
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/34—Arrangements for separating materials produced by the well
    • E21B43/35—Arrangements for separating materials produced by the well specially adapted for separating solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/02—Extraction using liquids, e.g. washing, leaching, flotation

Definitions

  • This invention relates to the treatment of paniculate material.
  • it relates to a method and an apparatus for removing paniculate material from a vessel, cleaning oil or other loosely adhering material from the surface thereof and conveying the material to a point of collection or discharge and optionally treating the water into which the removed oil has been taken.
  • the invention particularly relates to the treatment of the paniculate material such as sand and scale that accumulates in the various separation and residence vessels that are found in oil production facilities, and particularly offshore oil production facilities.
  • the separations achieved in such vessels are primarily as a result of the gravity separation occurring during the time that the fluids are resident in the vessel and the vessels are carefully designed so that the flows of the fluids therein are such as to minimise the distances over which the gravity separation must occur and to minimise turbulence and high velocities within the fluids which would tend to re-entrain separated materials.
  • the accumulation of the paniculate material in a particular vessel will reduce the residence time and the flow paths of the fluid in the vessel, both effects thus tending to reduce the efficiency of the separation achieved.
  • paniculate material can also lead to malfunction of and damage to instrumentation fitted to the separator vessel that are necessary to control its operation, and make it safe to operate.
  • Paniculate material will also collect by gravity separation in any vessel in which the fluids reside for any length of time and the present invention may be advantageously applied thereto.
  • the particulate material may be removed from the separator vessels by a process known as "jetting" whereby high velocity jets of fluid are directed into the accumulations of particulates to fluidise them, and this fluidised material is allowed to flow from the vessel via a connection adjacent the zone of fluidisation.
  • jetting a process known as "jetting" whereby high velocity jets of fluid are directed into the accumulations of particulates to fluidise them, and this fluidised material is allowed to flow from the vessel via a connection adjacent the zone of fluidisation.
  • This allows material to be removed from the vessel without human contact.
  • this material may be directed immediately to the sea but because the water conveying the material, and the material itself may contain quantities of oil that would cause undesirable pollution of the sea, this practise is seldom acceptable.
  • an apparatus for the treatment of particulate material having contaminating material mixed therewith comprising means for mixing fluid with the contaminated particulate material, hydrocyclone means, having an underflow outlet and an overflow outlet, for receiving the mixture of fluid and contaminated particulate material, collecting means connected to the underflow outlet of the hydrocyclone for collecting the particulate material from which at least some of the contaminating material has been removed from the hydrocyclone means, and discharge means for safe disposal of said particulate material.
  • an apparatus for cleaning sand contaminated with contaminants comprising water jetting means to separate the sand from the interior surface of a vessel wherein the sand is situated to form a slurry, hydrocyclone means, having an inlet, an overflow outlet and an underflow outlet, into which inlet the slurry from the vessel is fed at high velocity to form a vortex and thereby separating the contaminants from the sand, a collecting vessel for receiving mainly clean sand and some water from the underflow outlet, water removing means for removing excess water from the collecting vessel, and disposal means for disposing the clean sand safely.
  • a method for the treatment of particulate material having contaminating material mixed therewith comprising mixing fluid with the contaminated particulate material, feeding the mixture of fluid and contaminated particulate material to a hydrocyclone, means at high pressure to form a vortex, feeding the particulate material from which at least some of the contaminated material has been removed in the hydrocyclone means to a collecting means, and discharging the material therefrom safely.
  • a method for cleaning sand contaminated with contaminants comprising jetting water against the interior surface of a vessel wherein the sand is situated, to separate the sand therefrom, forming a slurry of water and said separated sand, feeding the slurry to a hydrocyclone means at high velocity to form a vortex, thereby separating the contaminants from the sand, feeding the mainly clean sand to a collecting vessel, removing excess water from the collecting vessel, and disposing of the clean sand safely.
  • the system shown comprises several separator vessels 1 (four shown), a first hydrocyclone unit 2, a collection vessel 3, and a second hydrocyclone unit 4.
  • the removal and treatment of the sand from one separator vessel 1 will be considered.
  • clean water i.e. water which should contain less than the maximum amount of oil that it is permitted to discharge into the sea
  • this clean water comes from a degasser vessel 5 - a part of this facility.
  • the separator vessel 1 is fitted with a jetting system 6 that enables the accumulated sand to be fluidised and removed from it via one or more slurry outlet connections 7 on the vessel 1.
  • the pressurised water source used to provide the flow of fluid to jet the separator vessel 1 may be provided by a pump 8 as shown in Figure 1. This pump 8 is termed the “jetting pump” and the pressurised water it provides is termed the "jetting water”.
  • the jetting water is raised to a pressure greater than the pressure in the separator vessel 1 so that it will flow into the vessel.
  • the flow of jetting water is controlled by a jetting water control valve set 25.
  • the system includes a first hydrocyclone unit, which contains one or more hydrocyclones designed for the separation of solid particles from liquids, which can discharge material into a collection vessel 3, the collection vessel being a further part of the facility.
  • the hydrocyclone unit 2 is designed and operated so that it separates the sand from the incoming sand and water slurry, and passes the bulk of the sand with sufficient water to enable it to be conveyed in to the collection vessel 3 from its underflow outlet 9, and the bulk of the water containing some residual sand from its overflow outlet 10.
  • the particles that emerge from the underflow have in almost all cases been thrown to the interior wall of the hydrocyclone by the centrifugal forces some distance from the underflow outlet 9 and have been pushed and spun along the interior wall to the underflow port by the fluid flows inside the hydrocyclone.
  • the action of the particles being pushed along the wall of the hydrocyclone serves to scrub and abrade oils, waxes and other loosely adhering materials (termed the "contaminants") from the surface of the particles.
  • the size and design of a hydrocyclone affects the size of the particles it will separate and the severity and duration of the scrubbing that the particles are subjected to and hence the size and design of the one or more hydrocyclones incorporated in the hydrocyclone unit 2 must be chosen to suit the sizes of the particles and their adhering contaminants that it is anticipated will collect in the separator 1.
  • the contaminants that are removed from the incoming particles will be separately transported by the liquid in the hydrocyclone. Those contaminants that are more dense than water will tend to emerge from the underflow outlet of the hydrocyclone unit, and those that are less dense, i.e. oils and waxes, than water will tend to emerge from the overflow outlet.
  • the system includes a second hydrocyclone unit 4, which contains one or more hydrocyclones designed for the separation of materials less dense than the water from the water.
  • This unit is located so that it receives the water from the overflow outlet 10 of the first hydrocyclone unit, and acts to separate the water entering it into two streams, a smaller flow rate stream from the overflow outlet of the second unit 4 containing the majority of the contaminants that are less dense than water i.e. waxes and oils, and a larger flow rate stream from the underflow which consists of water from which the majority of the oils and waxes have been removed.
  • the underflow will also contain the majority of the contaminants that are more dense than water.
  • the overflow stream from the second hydrocyclone unit 4 could, because of its small flowrate, be treated in an existing oily water treatment process on the platform, for example the drains system.
  • the piping feeding fluid to the first hydrocyclone unit 2 is arranged so that this hydrocyclone can be fed with fluids jetted from the separator vessel 1 or with fluids from the collection vessel 3. Fluids taken from the collection vessel 3 are delivered to the first hydrocyclone unit 2 via a slurry recirculation pump 1 1 .
  • the slurry recirculation pump 1 1 need only generate sufficient pressure to cause the fluids to flow through the first hydrocyclone unit 2 and therefore wear of the pump by the slurry is minimised.
  • the collection vessel 3 may have one or more connections that are used to deliver fluid to the positioned at the lowest point of the vessel for fully draining the vessel and the second 13 positioned high up the vessel at a position where it would not be covered by the settled accumulated sand.
  • a tapping 14 is taken from the jetting water source into the collection vessel 3, which via a set of internal fitments, is used to fluidise sand that has accumulated in the vessel to form a slurry so that it may be drawn into the slurry recirculation pump 11 through the upper connection 13 on the vessel 3.
  • the lower connection 12 to the slurry recirculation pump 1 1 may also be opened to allow some sand slurry to be drawn from the bottom of the vessel 3.
  • Other arrangements may be used to produce a pumpable slurry from the accumulated sand in the collection vessel 3.
  • the first hydrocyclone unit 2 separates most of the water from the slurry and directs towards the degassing vessel 5 via the second hydrocyclone unit 4 and the sand and remainder of the water pass from the underflow outlet 9 of the first hydrocyclone unit 2 back into the collection vessel 3.
  • the flowrate of the water coming form the jetting water source 8 must be set of match the flowrate of water passing from the overflow of the first hydrocyclone unit 3 via the second hydrocyclone overflow control valve set 23 towards the degasser 5.
  • FIG. 1 shows that the water from the overflow outlet 10 of the first hydrocyclone unit 2 may alternatively be directed to the intake of the jetting pump rather than to the degasser by bypass line 15. This may be done to avoid disturbing the internal flows in the degasser, or if it is desirable to avoid mixing the two waters.
  • An alternative method of discharging the sand is as follows. While running in recirculation mode jetting water is introduced into the intake of the slurry recirculation pump 11. As the flow of this jetting water is increased it will prevent slurry being drawn into the pump 1 1 and circulated to the first hydrocyclone unit 2 and will purge sand out of those parts of the system. The pump 11 may then be stopped and the flow of jetting water into the pump suction stopped. The sand in the collection vessel 3 may then be fluidised and directed overboard as described previously in the jetting of separators.
  • some of the water that has conveyed the slurry into the collection vessel 3 from the first hydrocyclone unit 2 may be drained from the vessel 3. This may be performed if that water contained a large quantity of oil (which could easily occur during the jetting of a separator 1 ) to reduce the amount of oil that would be recirculated with the slurry.
  • the valve 16 between the hydrocyclone unit underflow outlet 9 and the collection vessel 3 is closed.
  • the collection vessel 3 is drained down to the level set by the drain connections on the vessel and then the vessel is pressurised with gas to a pressure somewhat below that of the separator 1 that is to be jetted.
  • the jetting pump 8 is switched on and initially the jetting water is injected into the slurry line 18 after the slurry outlet valve 17 on the vessel to be jetted via the conveying water control valve set 19 and attached piping. This water then flows through the slurry line 18 to the first hydrocyclone unit 2 from which it exits via the overflow outlet 10.
  • the flow of water through the first hydrocyclone unit 2 generates a differential pressure in the same manner as an orifice plate, and a differential pressure transmitter which measures this pressure drop is used in conjunction with a flow control valve and flow controller to control the flowrate through the first hydrocyclone unit 2.
  • a flow control valve and flow controller which measures this pressure drop is used in conjunction with a flow control valve and flow controller to control the flowrate through the first hydrocyclone unit 2.
  • a flow of water into the vessel occurs equal to the difference in set points of the conveying water control valve set 19 and the first hydrocyclone unit 2. This causes the pressure at the inlet 20 to the first hydrocyclone unit 2 to equalise with the pressure in the separator vessel 1 , minus the line losses between the two.
  • the flow into the jetting water manifolds 6 on the separator vessel 1 is then established to as to fluidise the sand within the vessel to form a slurry.
  • the isolation valve 6 between the hydrocyclone unit 2 and the collection vessel 3 is then opened so that the sand separated by the hydrocyclone can be collected, and the flowrate of water introduced after the slurry outlet valve reduced.
  • the first hydrocyclone unit 2 is drawing a constant amount of fluid from the vessel, reducing the flowrate of the conveying water below the flowrate of the hydrocyclone unit 2 causes the slurry to be drawn from the vessel 1 via the slurry outlet valves 17 to the first hydrocyclone unit 2 where it undergoes cleaning and separation.
  • the conveying water also dilutes the slurry and so adjustment of the conveying water flowrate may be used to control the sand content of the slurry sent to the first hydrocyclone unit 2. It may be desirable to do this to reduce the initially high sand concentration that occurs at the beginning of a conventional jetting cycle to reduce the risks of blockage of the slurry line or the hydrocyclone unit 2.
  • a density measuring device (not shown) may be fitted to the slurry line 18 after the point at which the conveying water is injected, that is connected to a density control system that adjusts the flowrate of the conveying water to maintain the density of the slurry at a selected value.
  • the flowrate of fluid into the collection vessel 3 from the underflow outlet 9 of the hydrocyclone unit 2 is controlled by the pressure within the collection vessel 3, previously set somewhat below the pressure of the separator 1 to be jetted. As fluid enters the collection vessel 3 the pressure in the vessel is maintained at the appropriate value by the control valve venting the gas displaced from the vessel so as to maintain the desired flowrate from the underflow of the first hydrocyclone unit 2 into the vessel 3.
  • the gas outlet control valve closes and after a short period the underflow from the first hydrocyclone unit 2 ceases as the remaining gas in the vessel is compressed to the pressure at the inlet of the first cyclone.
  • the isolation valve 16 between the first hydrocyclone unit 2 and the collection vessel 3 is then closed.
  • the volume of the collection vessel 3 may be such that it can accept the underflow from the first hydrocyclone unit 2 for a long enough period to complete the jetting of the separator 1 , or alternatively it may be of a lesser volume which would require the separator to be jetted in two or more stages. In the latter case just prior to stopping the underflow of the first hydrocyclone unit 2 the flowrate of the conveying water injected after the slurry isolation valve 17 may be increased to stop slurry being withdrawn from the vessel 1 and to purge the sand from the slurry line which might otherwise block the line when the flow was stopped. The supernatant liquid in the collection vessel 3 could then be drained off and the separator jetting cycle could be repeated.
  • the slurry can be introduced to the inlet of the slurry recirculation pump 1 1 to boost its pressure prior to entering the hydrocyclone units.
  • An enhancement to the system is to fit an instrument to measure the density of the slurry entering the first hydrocyclone unit 2 or exiting its underflow and to use this measurement to adjust the underflow flowrate by adjusting the pressure in the collection vessel.
  • This allows the minimum quantity of water to be taken into the collection vessel 3 with the separated sand and will increase the period that a separator 1 can be jetted before the collection vessel 3 fills with slurry.
  • Density measurement can also be used to sense when a vessel 1 has been fully jetted: this may be taken to be when the concentration of sand in the slurry entering the first hydrocyclone unit 2 drops below a predetermined value, and to then stop the jetting of the vessel 1. It is desirable to minimise the time of jetting because jetting usually has an adverse affect on the separation efficiency of the separator, and to minimise the cycle time of the jetting and sand cleaning operation.
  • Another control strategy to enhance the operation of the system is to vary the pressure in the collection vessel 3 as a function of the time since the beginning of the jetting process, the vessel being at a lower pressure in the early stages of jetting when a high slurry sand concentration is expected and a larger underflow flowrate is required to convey the sand to the collecting vessel, and raising the pressure in the vessel in the later stages of the jetting to reduce the underflow flowrate when the slurry sand concentration is lower.
  • This method of control would not bring as great an improvement as using the density measurement of the slurry to control the underflow flowrate because the fiowrates would have to be set to be larger to allow the unit to cope with unexpected surges in slurry concentration that may occur.

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  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Engineering & Computer Science (AREA)
  • Mining & Mineral Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Fluid Mechanics (AREA)
  • Physics & Mathematics (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Soil Sciences (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Cyclones (AREA)

Abstract

On effectue le traitement de matériau particulaire mélangé à des contaminants par mélange du matériau avec un fluide et par introduction du mélange dans un séparateur hydrocyclone (2), de façon à séparer les contaminants du matériau, à les évacuer avec le fluide à travers le trop-plein du séparateur hydrocyclone (10) et à enlever le matériau particulaire du trop-plein (9). On peut introduire le matériau particulaire dans le séparateur hydrocyclone (2), afin de supprimer davantage de matériau contaminant. Ce traitement permet, en particulier, de supprimer les huiles et les paraffines du sable aggloméré sur différents types de navires (1) utilisés pour le forage du pétrole en mer. Le sable est mélangé à de l'eau sous pression, afin d'obtenir une boue liquide qu'on introduit dans le séparateur hydrocyclone (2).
PCT/GB1995/002315 1994-09-28 1995-09-27 Traitement de materiau particulaire WO1996009895A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9419484A GB9419484D0 (en) 1994-09-28 1994-09-28 Treatment of particulate material
GB9419484.2 1994-09-28

Publications (1)

Publication Number Publication Date
WO1996009895A1 true WO1996009895A1 (fr) 1996-04-04

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PCT/GB1995/002315 WO1996009895A1 (fr) 1994-09-28 1995-09-27 Traitement de materiau particulaire

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GB (2) GB9419484D0 (fr)
WO (1) WO1996009895A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999038617A1 (fr) * 1998-02-02 1999-08-05 Axsia Serck Baker Limited Ameliorations relatives a la separation des sables petroliferes
US11173427B2 (en) 2017-09-25 2021-11-16 Sand Separation Technologies Inc. Device for separating solids from a fluid stream
US11839884B2 (en) 2018-09-06 2023-12-12 Sand Separation Technologies Inc. Counterflow vortex breaker

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19621892A1 (de) * 1996-05-31 1997-12-04 Ulrich Dipl Ing Franze Verfahren und Vorrichtung zur In-Situ-Reinigung von Spiel- und Strandsanden
DE60211701D1 (de) * 2001-06-04 2006-06-29 Axsia Serck Baker Ltd Verfahren zum ableiten von sand aus einer behälter unter erhöhtem druck
GB0215343D0 (en) * 2002-07-03 2002-08-14 Kvaerner Process Systems As Sand transport system
GB2488160A (en) * 2011-02-18 2012-08-22 Vws Westgarth Ltd Separation and Sand Cleaning System
GB2529729B (en) * 2014-11-14 2016-09-14 Dwc As Solids separation, washing and sampling system

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3723309A (en) * 1971-09-20 1973-03-27 Exxon Production Research Co System and method for cleaning oily solid material
US4519848A (en) * 1982-06-11 1985-05-28 Underwood Gene E Separator
EP0273463A1 (fr) * 1987-01-02 1988-07-06 Arfaz Equipment Méthode de nettoyage des réservoirs de stockage pour des produits de champ pétrolifère
US4859323A (en) * 1988-05-16 1989-08-22 Theodore Rolfvondenbaumen Oil sand cleaning apparatus
US5306351A (en) * 1993-05-21 1994-04-26 Anderson William J Waste oil removal composition and method
US5350525A (en) * 1992-09-11 1994-09-27 Conoco Specialty Products Inc. System and process for hydrocyclone separation of particulate solids and at least one liquid phase from a multiphase liquid mixture

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3869559A (en) * 1970-04-13 1975-03-04 Thomas P Clark Process for separation and cleaning of edible vegetable products
DE2645137C2 (de) * 1976-10-06 1978-05-03 Kraftwerk Union Ag, 4330 Muelheim Einrichtung zur Gewinnung von Ölprodukten aus ölsanden
JPS5512831A (en) * 1978-07-06 1980-01-29 Oishi Kikai Seisakusho Kk Debris sorting apparatus from paper making stock
US4282088A (en) * 1980-03-03 1981-08-04 Linatex Corporation Of America Process for cleaning fine coal
US4405453A (en) * 1982-02-23 1983-09-20 Envirotech Corporation Process for cleaning undeslimed coal
US4795037A (en) * 1986-05-07 1989-01-03 Rich Jr John W Process for separating high ash coal from refuse
WO1993007967A1 (fr) * 1991-10-15 1993-04-29 Genesis Research Corporation Procede d'epuration de charbon

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3723309A (en) * 1971-09-20 1973-03-27 Exxon Production Research Co System and method for cleaning oily solid material
US4519848A (en) * 1982-06-11 1985-05-28 Underwood Gene E Separator
EP0273463A1 (fr) * 1987-01-02 1988-07-06 Arfaz Equipment Méthode de nettoyage des réservoirs de stockage pour des produits de champ pétrolifère
US4859323A (en) * 1988-05-16 1989-08-22 Theodore Rolfvondenbaumen Oil sand cleaning apparatus
US5350525A (en) * 1992-09-11 1994-09-27 Conoco Specialty Products Inc. System and process for hydrocyclone separation of particulate solids and at least one liquid phase from a multiphase liquid mixture
US5306351A (en) * 1993-05-21 1994-04-26 Anderson William J Waste oil removal composition and method

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999038617A1 (fr) * 1998-02-02 1999-08-05 Axsia Serck Baker Limited Ameliorations relatives a la separation des sables petroliferes
GB2338193A (en) * 1998-02-02 1999-12-15 Axsia Serck Baker Ltd Improvements relating to oil-sand separation
GB2338193B (en) * 1998-02-02 2001-10-10 Axsia Serck Baker Ltd Improvements relating to oil-sand separation
US6315837B1 (en) 1998-02-02 2001-11-13 Axsia Serck Baker Limited Oil-sand separation
US11173427B2 (en) 2017-09-25 2021-11-16 Sand Separation Technologies Inc. Device for separating solids from a fluid stream
US11839884B2 (en) 2018-09-06 2023-12-12 Sand Separation Technologies Inc. Counterflow vortex breaker

Also Published As

Publication number Publication date
GB9419484D0 (en) 1994-11-16
GB2293992A (en) 1996-04-17
GB9519710D0 (en) 1995-11-29

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