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US20110265993A1 - Sand decanter - Google Patents

Sand decanter Download PDF

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Publication number
US20110265993A1
US20110265993A1 US13/143,390 US201013143390A US2011265993A1 US 20110265993 A1 US20110265993 A1 US 20110265993A1 US 201013143390 A US201013143390 A US 201013143390A US 2011265993 A1 US2011265993 A1 US 2011265993A1
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US
United States
Prior art keywords
sand
fraction
water
heavy hydrocarbons
screw conveyor
Prior art date
Legal status (The legal status 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 status listed.)
Abandoned
Application number
US13/143,390
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English (en)
Inventor
Steve Williams
David Aldus
Gary E. Fout
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
MI Drilling Fluids Canada Inc
MI Drilling Fluids UK Ltd
MI LLC
Original Assignee
MI Drilling Fluids Canada Inc
MI Drilling Fluids UK Ltd
MI LLC
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 MI Drilling Fluids Canada Inc, MI Drilling Fluids UK Ltd, MI LLC filed Critical MI Drilling Fluids Canada Inc
Priority to US13/143,390 priority Critical patent/US20110265993A1/en
Assigned to M-I L.L.C. reassignment M-I L.L.C. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FOUT, GARY E.
Assigned to M-I DRILLING FLUIDS CANADA, INC. reassignment M-I DRILLING FLUIDS CANADA, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ALDUS, DAVID
Assigned to M-I DRILLING FLUIDS UK LIMITED reassignment M-I DRILLING FLUIDS UK LIMITED ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WILLIAMS, STEVE
Publication of US20110265993A1 publication Critical patent/US20110265993A1/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • C10G1/045—Separation of insoluble materials
    • 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
    • B01D21/009—Heating or cooling mechanisms specially adapted for settling tanks
    • 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
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/245—Discharge mechanisms for the sediments
    • B01D21/2461—Positive-displacement pumps; Screw feeders; Trough conveyors
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • C10G1/047—Hot water or cold water extraction processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/80—Additives
    • C10G2300/805—Water

Definitions

  • Embodiments disclosed herein relate generally to processing hydrocarbons recovered from a subterranean formation. More specifically, embodiments disclosed herein relate to processing heavy hydrocarbons, such as viscous oils, oil shale, tar sands, and other heavy hydrocarbons.
  • heavy hydrocarbons such as viscous oils, oil shale, tar sands, and other heavy hydrocarbons.
  • Heavy hydrocarbons e.g., heavy oil and/or tar
  • relatively permeable formations e.g., in tar sands
  • Tar can be surface-mined and upgraded to lighter hydrocarbons such as crude oil, naphtha, kerosene, and/or gas oil.
  • Surface milling processes may further separate the bitumen from sand.
  • the separated bitumen may be converted to light hydrocarbons using conventional refinery methods. Mining and upgrading tar sand is usually substantially more expensive than producing lighter hydrocarbons from conventional oil reservoirs.
  • In situ production of hydrocarbons from tar sand may be accomplished by heating and/or injecting a gas into the formation.
  • U.S. Pat. Nos. 5,211,230 and 5,339,897 for example, describe a horizontal production well located in an oil-bearing reservoir. A vertical conduit may be used to inject an oxidant gas into the reservoir for in situ combustion.
  • a relatively permeable formation may be predominantly heavy hydrocarbons and/or tar with no supporting mineral grain framework and only floating (or no) mineral matter (e.g., asphalt lakes).
  • the relatively permeable formations may also include heavy hydrocarbons entrained in, for example, sand or carbonate.
  • a tar sands formation for example, is a formation in which hydrocarbons are predominantly present in the form of heavy hydrocarbons and/or tar entrained in a mineral grain framework or other host lithology (e.g., sand or carbonate).
  • the high viscosity of the heavy hydrocarbons may result in co-production of sand or carbonate when recovering the heavy hydrocarbons from a well or a mine.
  • Produced heavy hydrocarbons as a result, generally include a combination of clay, sand, water, and bitumen or other heavy hydrocarbons.
  • the co-produced solid materials such as sand, must be separated from the heavy hydrocarbons before the hydrocarbons are further processed or upgraded.
  • One such process is to feed the co-produced mixture to a settling vessel, wherein the mixture is heated, decreasing the viscosity of a portion of the hydrocarbons.
  • the lower viscosity hydrocarbons float to the top of the settling vessel and are recovered, and the sand and a portion of the heavy hydrocarbons settle to the bottom of the vessel and are allowed to accumulate.
  • the sands, having solidified in the bottom of the settling vessel must then be periodically hydroblasted to regain the settling volume for further production.
  • a production site using this hydrocarbon recovery technique may require several settling vessels, where service is continually rotated allowing for production and cleaning cycles. Further, the sand recovered from the settling vessels during cleaning contains a significant amount of hydrocarbons, requiring the sands to be disposed of in hazardous waste sites or otherwise processed before disposal. This type of separation process thus incurs a very large operating expense.
  • embodiments disclosed herein relate to a method for processing hydrocarbons recovered from a subterranean formation, including: feeding a stream comprising water, sand, and heavy hydrocarbons produced from a subterranean formation to a separation vessel; concurrently in the separation vessel: heating the stream components to an elevated temperature to reduce a viscosity of the heavy hydrocarbons; and separating the sand, the heavy hydrocarbon, and the water to form a water fraction, a hydrocarbon fraction, and a sand fraction comprising sand and at least one of water and heavy hydrocarbons; and recovering the water fraction from the separation vessel; recovering the hydrocarbon fraction from the separation vessel; and withdrawing the sand fraction from the separation vessel.
  • embodiments disclosed herein relate to a system for processing hydrocarbons recovered from a subterranean formation, including: a separation vessel comprising: a vertical portion on top of an angled portion; at least one inlet nozzle for feeding a stream comprising water, sand, and heavy hydrocarbons produced from a subterranean formation into the vessel for separation into a hydrocarbon fraction, a water fraction, and a sand fraction comprising sand and at least one of water and heavy hydrocarbons; an indirect heat exchange device disposed within at least one of the vertical portion and the angled portion for heating the water, sand, and heavy hydrocarbons; at least one outlet nozzle for recovering the hydrocarbon fraction; at least one outlet nozzle for recovering the water fraction; a screw conveyor located at a bottom of the angled portion to concurrently transport the sand fraction from the bottom of the angled portion to a screw conveyor outlet and separate the sand fraction from at least a portion of the at least one of water and heavy hydrocarbons; and at least one outlet
  • FIG. 1 is a schematic diagram of a sand decanter according to embodiments disclosed herein.
  • FIG. 2 is a schematic diagram of a sand decanter according to embodiments disclosed herein.
  • FIG. 3 is a schematic diagram of a helical auger useful in sand decanters according to embodiments disclosed herein.
  • embodiments disclosed herein relate to processing hydrocarbons recovered from a subterranean formation. More specifically, embodiments disclosed herein relate to processing heavy hydrocarbons, such as viscous oils, oil shale, tar sands, and other heavy hydrocarbons.
  • Embodiments disclosed herein provide for apparatus and methods for the separation of the heavy hydrocarbons from the co-produced water and sand.
  • Heavy hydrocarbons refers to viscous hydrocarbon fluids. Heavy hydrocarbons may include highly viscous hydrocarbon fluids such as heavy oil, tar, and/or asphalt. Heavy hydrocarbons may include carbon and hydrogen, as well as smaller concentrations of sulfur, oxygen, and nitrogen. Additional elements may also be present in heavy hydrocarbons in trace amounts. Heavy hydrocarbons may be classified by API gravity. Heavy hydrocarbons generally have an API gravity below about 20° C. Heavy oil, for example, generally has an API gravity of about 10-20° C., whereas tar generally has an API gravity below about 10° C. The viscosity of heavy hydrocarbons is generally greater than about 100 centipoise at 15° C. Heavy hydrocarbons may also include aromatics or other complex ring hydrocarbons.
  • Tar generally refers to a viscous hydrocarbon that generally has a viscosity greater than about 10,000 centipoise at 15° C.
  • the specific gravity of tar generally is greater than 1.
  • Tar may have an API gravity less than 10° C.
  • Certain types of formations that include heavy hydrocarbons may also be, but are not limited to, natural mineral waxes, or natural asphaltites.
  • Natural mineral waxes typically occur in substantially tubular veins that may be several meters wide, several kilometers long, and hundreds of meters deep.
  • Natural asphaltites include solid hydrocarbons of an aromatic composition and typically occur in large veins.
  • Heavy hydrocarbons may be produced from formations including various mineral matrices.
  • Sand refers to sedimentary rock, sands, silicilytes, clays, carbonates, and other media that may be co-produced with heavy hydrocarbons, such as heavy hydrocarbons co-produced with sand as a slurry.
  • a produced fluid including water, sand, and heavy hydrocarbons may be fed to a sand decanter according to embodiments disclosed herein, in which the produced fluid is concurrently i) heated to an elevated temperature to reduce the viscosity of the heavy hydrocarbon and ii) separated to form a water fraction, a hydrocarbon fraction, and a sand fraction.
  • the sand fraction recovered may also include water and/or hydrocarbons, due to immersion in the liquid phases present (the hydrocarbon and/or the water being separated). The water fraction, the hydrocarbon fraction, and the sand fraction may then be separately recovered from the sand decanter.
  • the water fraction and the hydrocarbon fraction may be withdrawn from the sand decanter via a liquid draw.
  • the sand fraction may be withdrawn from the sand decanter via a helical auger or screw conveyor.
  • the sand fraction may be fed from a lower portion of the sand decanter to an inlet of a screw conveyor.
  • the screw conveyor may concurrently i) transport the sand fraction from the inlet of the screw conveyor to the outlet of the screw conveyor, and ii) separate the sand fraction from at least a portion of the water and/or hydrocarbons present.
  • Heating of the co-produced heavy hydrocarbons, water, and sand within the sand decanter may be performed via indirect heat exchange. Heat exchange may be performed using various heat exchange media, including steam/water, hot oil, and hot gases. In some embodiments, hot gases produced from a burner, such as a natural gas burner, may be used. Combustion fuels used to produce gases for use in heat exchange may also include, for example, a portion of the heavy hydrocarbons recovered from the sand decanter or other hydrocarbons that may be present in the fluid produced from the subterranean formation. In other embodiments, electrical heating coils may be used for the heating.
  • heat exchange medium may depend upon the availability of each at the production site. For example, high pressure steam or other heat exchange medium may not be readily available. Natural gas, however, is often a readily available fuel at most production sites, and may be used to perform the desired separations within the sand decanter.
  • the sand, water, and heavy hydrocarbons in the fluids produced from a well may be heated to an elevated temperature sufficient to reduce the viscosity of the heavy hydrocarbon to promote separation of the fractions by gravity.
  • the fluid produced from the subterranean formation may have a temperature of 25° C. or less, such as about 15° C. or less. Heating of the produced fluid may increase the temperature of the mixture to a temperature in the range from about 50° C. to less than about 100° C., such as a temperature in the range from about 60° C. to 90° C. in some embodiments, and a temperature in the range from about 70° C. to about 80° C. in other embodiments.
  • the heavy hydrocarbons may be of a sufficiently high viscosity such that it adheres to the sand.
  • the lower viscosity of the heavy hydrocarbon allows the sand to settle out of solution, resulting in separation of the sand from the heavy hydrocarbon and the water.
  • the lower viscosity of the hydrocarbon additionally facilitates separation of the hydrocarbon from any water present, resulting in the production of two or three phases within the sand decanter (water/hydrocarbon and sand or water, hydrocarbon, and sand, depending upon the quantity of water produced and the solubility of water within the hydrocarbon phase).
  • the resulting phases, sand (solids), hydrocarbons, and/or water may then be recovered from the sand decanter as described above.
  • Separation and recovery of the heavy hydrocarbons from the co-produced sand may be performed in a sand decanter as disclosed herein, one embodiment of which is illustrated in FIG. 1 .
  • the produced fluid from the subterranean formation may be fed via flow line 10 to an inlet 12 of sand decanter 14 .
  • Sand decanter 14 may include a vertical portion 16 on top of an angled portion 18 .
  • Vertical portion 16 may be open to the atmosphere or may include a top 20 , enclosing the vessel and allowing for insulation of the vessel top and retention of heat.
  • the co-produced fluids may be heated within the vessel via indirect heat exchange with a heat exchange medium passed through heating coils 22 .
  • heating coils 22 may be referred to as a fire tube.
  • a feed port 30 to a screw conveyor 32 may be provided to continuously or intermittently remove sand from bottom portion 26 .
  • Screw conveyor 32 may include a helical auger 34 , rotation of which may result in the transport of sand from feed port 30 toward screw conveyor outlet 36 .
  • Rotation of helical auger 34 may be performed, for example, via coupling of shaft 38 to a drive unit 40 , including a motor.
  • a liquid level 42 may result within screw conveyor 32 , and may have a height similar to that of the fluid level 44 within sand decanter 14 .
  • Screw conveyor 32 may have a height extending above fluid levels 42 , 44 , allowing for the sand to be separated from at least a portion of the fluid, which may include water and/or hydrocarbons, during transport of the sand to outlet 36 .
  • Subterranean formations co-producing heavy hydrocarbons and sand may be located in regions having sub-zero temperatures for at least a portion of the year. Due to fluids, including hydrocarbons and/or water, remaining with the sand during transport via screw conveyor 32 , insulation of screw conveyor 32 or heating of the sand during transport within screw conveyor 32 may be required to ensure transportability of the sand when ambient conditions may result in an unacceptable increase in hydrocarbon viscosity or freezing of water, each of which may result in undesired buildup within screw conveyor 32 or blockage of outlet 36 .
  • Heating of screw conveyor 32 may be performed using heat tracing (electrical or heat exchange tubing or jacketing for flow of a heat exchange medium) around at least a portion of an exterior surface 46 of screw conveyor 32 .
  • heat tracing electrical or heat exchange tubing or jacketing for flow of a heat exchange medium
  • the flue gas passed through fire tubes 22 may be fed to jacket 48 for heating of the contents in screw conveyor 32 .
  • the flue gas may then be recovered from jacket outlet 50 for exhaust to the atmosphere or for further processing.
  • the exterior of sand decanter 14 may additionally be insulated or jacketed to promote efficient heat transfer (not illustrated).
  • a portion 32 A of screw conveyor 32 may be positioned horizontally along the length of bottom portion 26 for transport of the sand fraction from sand decanter 14 .
  • Screw conveyor 32 may also include transverse portion 32 B for concurrently transporting the sand and separating the sand from at least a portion of the hydrocarbons and/or water that may be present.
  • the helical auger located in portions 32 A and 32 B may be coupled for use with a single drive unit 40 or may be rotated using separate drive units (not illustrated).
  • screw conveyor inlet 30 may extend the length of horizontal portion 32 A.
  • liquids such as hydrocarbons, water, or both
  • screw conveyor 32 may be initially conveyed with the sand by screw conveyor 32 .
  • the length of the screw conveyor between liquid level 44 and outlet 36 may be sufficient to only remove a portion of the water and/or hydrocarbons from the sand. Further, wetting of the surface area of the sand may result in carryover of a significant amount of fluids.
  • screw conveyor 32 may be a drying auger unit, allowing for the concurrent transportation of the sand and separation of a greater portion of the water and/or hydrocarbons from the sand fraction. Separation of hydrocarbons and water from sand during transport may be facilitated as shown in FIG. 3 , which may be a cross-sectional view of a drying auger unit 60 , such as taken from section 3 - 3 shown in FIG. 1 .
  • a drying auger unit 60 may include an inclined housing 62 having side walls 64 joined by a bottom 66 .
  • a sand fraction including sand, water and/or hydrocarbons, may be fed to drying auger unit 60 as described above.
  • a helical auger 34 located at least partially within housing 62 , may be used to transport the sand from feed port 30 toward outlet 36 .
  • Helical auger 34 may include multiple flights 68 .
  • Elevated pan 70 is disposed in and extends along at least a portion of the length of housing 62 . Due to liquid head requirements, a drying auger unit 60 may be located only at an upper portion of screw conveyor 30 . Elevated pan 70 may have an arcuate cross section with an effective radius R greater than a radius r of helical auger 34 . For example, elevated pan 70 may have a general half-u shaped cross-section.
  • Elevated pan 70 may be located proximate a lower quadrant of the helical auger 34 , preferably along the lower quadrant proximate the upward rotation U of flights 68 . In some embodiments, elevated pan 70 may extend at least 90°, such as from a lowermost portion P, in the direction of rotation U of helical auger 34 .
  • compression may be used in conjunction with gravity to separate the drilling fluid from the drill cuttings.
  • flights 68 of helical auger 34 may be evenly spaced in some embodiments, thus using primarily gravitational forces to separate the drilling fluid.
  • flights 68 may have a decreasing spacing along the length of elevated pan 70 , thus compressing the cuttings slurry as it traverses from inlet end 30 toward outlet end 36 , facilitating additional separation of drilling fluid from the cuttings slurry.
  • two or more augers may be used.
  • Hydrocarbon fractions recovered from sand decanters according to embodiments disclosed herein may be forwarded for storage, transport, or further processing, such as to convert the heavy hydrocarbons to lighter hydrocarbons, such as light hydrocarbons (C1 to C6 hydrocarbons, including olefins), gasoline range hydrocarbons (C6 to C10 hydrocarbons, for example), diesel range hydrocarbons, light cycle oils, and he like, as known to those skilled in the art.
  • lighter hydrocarbons such as light hydrocarbons (C1 to C6 hydrocarbons, including olefins), gasoline range hydrocarbons (C6 to C10 hydrocarbons, for example), diesel range hydrocarbons, light cycle oils, and he like, as known to those skilled in the art.
  • a water fraction recovered from sand decanters according to embodiments disclosed herein may contain some hydrocarbons. Thus, water fractions recovered may be further processed to remove the hydrocarbons, resulting in a water fraction suitable for disposal or reuse within the production facilities.
  • the sand fraction recovered from sand decanters according to embodiments disclosed herein may contain some hydrocarbons, as mentioned above.
  • hydrocarbons such as due to adhesion or insufficient increase of viscosity, may result in the sand being unsuitable for non-hazardous disposal.
  • Sand fractions recovered according to embodiments disclosed herein may be rendered suitable for non-hazardous disposal using a sand cleaning system, such as that disclosed in U.S. Provisional Patent Application Ser. No. 61/014,262, filed on Dec. 17, 2007, which is hererby incorporated by reference.
  • the cleaning of the sand may result in recovery of additional hydrocarbons that may be further processed as described above.
  • Sand, having been cleaned to meet various regulations for non-hazardous disposal may then be landfilled, re-injected into a well, or otherwise used or disposed of, on site or at a remote facility.
  • embodiments disclosed herein provide for the separation and recovery of sand from heavy hydrocarbons, such as bitumen or other heavy hydrocarbons produced from a low-pressure well.
  • embodiments disclosed herein may provide for concurrently heating the heavy hydrocarbons to reduce a viscosity thereof and separating of the heavy hydrocarbons from co-produced sand.
  • the separations performed using sand decanters according to embodiments disclosed herein may allow for the continuous separation of sand, in contrast to current processes. Due to the continuous or intermittent withdrawal of a sand fraction from the sand decanters, buildup of sand in the separation vessel is reduced, requiring less intensive maintenance and the associated costs. Further, continuous separations according to embodiments disclosed herein may reduce the number of separation vessels required to perform the separations.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US13/143,390 2009-01-07 2010-01-06 Sand decanter Abandoned US20110265993A1 (en)

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Application Number Priority Date Filing Date Title
US13/143,390 US20110265993A1 (en) 2009-01-07 2010-01-06 Sand decanter

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US14305209P 2009-01-07 2009-01-07
US13/143,390 US20110265993A1 (en) 2009-01-07 2010-01-06 Sand decanter
PCT/US2010/020182 WO2010080780A2 (fr) 2009-01-07 2010-01-06 Décanteur de sable

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US20110265993A1 true US20110265993A1 (en) 2011-11-03

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US (1) US20110265993A1 (fr)
EP (1) EP2386012A4 (fr)
BR (1) BRPI1006071A2 (fr)
CA (1) CA2748959C (fr)
EA (1) EA201170918A1 (fr)
MX (1) MX2011007283A (fr)
WO (1) WO2010080780A2 (fr)

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US20120318583A1 (en) * 2009-11-30 2012-12-20 Tyco Flow Services Ag Cutting wash apparatus and method
US20170252674A1 (en) * 2009-01-09 2017-09-07 Granbury Thompson Group, Llc Backflow collection system and method for reclaiming the same
US20210047571A1 (en) * 2016-03-29 2021-02-18 3P Technology Corp. Methods for separating hydrocarbons from particulates
US11173427B2 (en) 2017-09-25 2021-11-16 Sand Separation Technologies Inc. Device for separating solids from a fluid stream
WO2022263978A3 (fr) * 2021-06-17 2023-01-26 Walter Sisulu University Appareil portatif de préparation d'asphalte tiède et procédé de production d'asphalte tiède
US11839884B2 (en) 2018-09-06 2023-12-12 Sand Separation Technologies Inc. Counterflow vortex breaker
US12064714B1 (en) * 2020-07-16 2024-08-20 Thomas Jason Rich Sand drying system and method of use

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CN104420860A (zh) * 2013-08-19 2015-03-18 国润金华（北京）国际能源投资有限公司 一种油砂分离器

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20170252674A1 (en) * 2009-01-09 2017-09-07 Granbury Thompson Group, Llc Backflow collection system and method for reclaiming the same
US20120318583A1 (en) * 2009-11-30 2012-12-20 Tyco Flow Services Ag Cutting wash apparatus and method
US20210047571A1 (en) * 2016-03-29 2021-02-18 3P Technology Corp. Methods for separating hydrocarbons from particulates
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
US12064714B1 (en) * 2020-07-16 2024-08-20 Thomas Jason Rich Sand drying system and method of use
WO2022263978A3 (fr) * 2021-06-17 2023-01-26 Walter Sisulu University Appareil portatif de préparation d'asphalte tiède et procédé de production d'asphalte tiède
US12428790B2 (en) 2021-06-17 2025-09-30 Walter Sisulu University Portable warm asphalt preparation apparatus and process for the production of warm asphalt

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EA201170918A1 (ru) 2012-02-28
EP2386012A2 (fr) 2011-11-16
CA2748959C (fr) 2014-03-11
EP2386012A4 (fr) 2014-03-12
WO2010080780A3 (fr) 2010-10-28
BRPI1006071A2 (pt) 2016-04-19
WO2010080780A2 (fr) 2010-07-15
MX2011007283A (es) 2011-09-27
CA2748959A1 (fr) 2010-07-15

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