US3864251A - Treatment of middlings stream from hot water process for recovering bitumen from tar sand - Google Patents

Treatment of middlings stream from hot water process for recovering bitumen from tar sand Download PDF

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US3864251A
US3864251A US435515A US43551574A US3864251A US 3864251 A US3864251 A US 3864251A US 435515 A US435515 A US 435515A US 43551574 A US43551574 A US 43551574A US 3864251 A US3864251 A US 3864251A
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stream
bitumen
water
hot water
middlings
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Lubomyr M O Cymbalisty
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Petro Canada Exploration Inc
Gulf Canada Ltd
Canada Cities Service Ltd
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Canada Cities Service Ltd
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Assigned to GULF CANADA LIMITED reassignment GULF CANADA LIMITED CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). 06/02/78 Assignors: GULF OIL CANADA LIMITED
Assigned to PETRO-CANADA EXPLORATION, INC. reassignment PETRO-CANADA EXPLORATION, INC. CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). EFFECTIVE DATE 10-25-76 Assignors: ATLANTIC RICHFIELD CANADA LTD.
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    • 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
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/24—Pneumatic
    • 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
    • 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
    • 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
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/1468—Discharge mechanisms for the sediments

Definitions

  • Froth is formed in the settler; this [51] I t Cl Bold 2mm froth is surprisingly low in solids and water.
  • the tail- [58] 5O 56 63 ings stream from the settler is recycled to the front 84 f i end of the extraction process, thereby conserving water.
  • the invention provides an alternative to the conventional sub-aeration cell used for treatment of the [56] References Cited middlln s stream.
  • the invention has been developed using tar sand from the Athabasca deposit at Fort McMurray, Alberta, Can. While it is described with reference to that feed stock, the invention may find beneficial application to tar sands present in other deposits.
  • Athabasca tar sands comprises sand grains which are each sheathed in a thin layer of water. Bitumen is trapped in the void space between the water-wet grains.
  • the composition of the tar sand might be percent by weight bitumen, 4 percent water, and 86 percent solids.
  • Athabasca tar sands are presently processed using a method commonly referred to as the hot water method.
  • tar sand is mixed in a conditioning drum or tumbler with hot water and steam. While in the tumbler, the tar sand disintegrates and at the same time liberated bitumen is aerated.
  • disintegrate is meant that the sand and bitumen particles are dispersed one from another in preliminary way.
  • the tumbler product is a porridge-like slurry which typically might comprise 9.5 percent bitumen, 22.00 percent water and 68.5 percent solids, at a temperature of l85l90F.
  • the slurry is flooded with additional hot water to further disperse the sand and bitumen.
  • This flooding operation is usually carried out at a screen positioned at the outlet from the tumbler.
  • the flooded slurry typically might have a composition of7 percent bitumen, 43 percent water, and 50 percent solids, and a temperature of 160F.
  • the flooded slurry is introduced into a separation cell at about its longitudinal midpoint; this cell is a cylindrical vessel having a conical bottom.
  • This cell is a cylindrical vessel having a conical bottom.
  • the sand leaves the vessel through a bottom outlet and is discarded as tailings.
  • the froth overflows the vessel wall into a launder and is removed for further treatment.
  • a middlings stream is continuously withdrawn from the separation cell at a point intermediate its upper and lower ends. This is done for two reasons. Firstly, a relatively large quantity of water must be added in the flooding stage to ensure that the bitumen and solids particles are sufficiently dispersed from one another in the separation cell to obtain reasonable froth product quality and bitumen recovery. Some of this water must be removed from the cell in the form of a middlings drag streamotherwise it will report to the bottom tailings stream. If too much water leaves with the sand tailings, bitumen is carried out with it and oil recoveries drop accordingly. Secondly, the solids known as fines (i.e., 325 mesh), present in the tar sands, tend to accumulate in the central portion of the cell.
  • fines i.e., 325 mesh
  • fines are present in too high a concentration, they tend to form a thick blanket, through which the aerated bitumen particles have difficulty in passing to reach the froth layer. It is therefore conventional to withdraw some of these fines in the middlings stream to relieve the congestion within the cell.
  • the middlings stream typically comprises 2 percent bitumen, 15 percent solids and 83 percent water.
  • bitumen particles in the middlings stream are a mixed lot some are non-buoyant, perhaps because they are non-aerated or because they are attached to both solids and air; others are buoyant but were withdrawn through the middlings outlet before reaching the froth layer.
  • the middlings stream from the separator cell is passed through a sub-aeration cell to recover contained bitumen.
  • the middlings are turbulently mixed with air to bring the bitumen to the surface of the cell as a froth.
  • This froth is badly contaminated with solids and water a typical composition might be 16 percent weight solids, 54 percent water and 31 percent bitumen.
  • the primary and secondary froths are combined, diluted with a specific gravity-altering diluent, such as naphtha, and treated in a centrifuge circuit to separate the solids and water from the bitumen.
  • a specific gravity-altering diluent such as naphtha
  • the middlings stream is diluted with hot water, preferably contacted with minute air bubbles to aerate non-buoyant bitumen, and introduced into a settler vessel.
  • the buoyant bitumen forms a froth product which is reduced in solids and water content in comparison to the prior art secondary recovery froth obtained by subaeration flotation.
  • Solids, water and traces of bitumen are withdrawn from the vessel through the tailings outlet. Part of this tailings stream may be recycled to the front end of the process for repeated treatment in the separation cell. In this manner, hot water is conserved within the process.
  • the remainder of the tailings stream may be discarded or otherwise processed for recovery of contained bitumen.
  • the froth product from the settler is preferably combined with the primary froth from the separation cell and forwarded on to the froth treatment circuit.
  • FIG. 1 is a block diagram illustrating the steps of the process.
  • FIG. 2 is a schematic illustration of the equipment used in the process.
  • Athabasca tar sand comprising l 1 percent by weight bitumen, 4 percent water, and 85 percent solids, including l2 percent fines, is fed to a tumbler l.
  • Sufficient fresh hot water approximately 290 pounds per hour, is added to the tar sand in the tumbler l to produce a slurry containing 22 percent by weight water.
  • the product slurry is observed to have a temperature of l60F.
  • the residence time in the tumbler is approximately 3 /2minutes.
  • the slurry is fed from the tumbler 1 into a separation cell 3. Water at 180F is added to the slurry at the screen 4 to raise the water content to approximately 42 percent.
  • the separation cell 3 and settler 5 are both filled with clear water at l80F at the time that the test run is initiated. Froth, comprising 70 percent bitumen, 6 percent solids, 24 percent water, is produced at the surface of the separation cell at a rate of I70 pounds per hour.
  • a tailings stream comprising 70 percent solids, 0.8 percent bitumen and 29.2 percent water, is produced from the cell at a rate of l,l80 pounds per hour.
  • a middlings stream comprising 2 percent bitumen, percent solids, and 83 percent water, is withdrawn from the separation cell by a pump 6 at a rate of 900 pounds per hour. This stream is mixed with 200 pounds per hour of water and approximately 0.1 CFH air in a mixer 7 and is then pumped to the settler.
  • the diluted middlings stream is introduced to the central portion of the settler through a rotating, perforated distribution pipe 8.
  • a froth product is continuously formed and withdrawn at the rate of 19 lbs. per hour from the settler.
  • This froth product comprises 77 percent bitumen, 5 percent solids, and 18 percent water.
  • a stream of dilute solids and water is continuously withdrawn through the tailings outlet of the settler vessel and is recycled to the front end of extraction.
  • the same middlings stream when fed directly to a sub-aeration secondary recovery cell, gives a froth product comprising 52 percent bitumen, 13 percent solids and 35 percent water.
  • tailings stream withdrawing a tailings stream from the base of the vessel, said tailings stream comprising the major portion of the fine solids and water introduced into the vessel.
  • At least part of the tailings stream from the settler vessel is recycled for repeated treatment in the separation cell.
  • the middlings stream is aerated prior to entry into the settler vessel to facilitate bitumen flotation.

Abstract

This process relates to treating the middlings stream from the primary separation cell used in the hot water process for extracting bitumen from tar sand. The middlings stream is diluted with hot water and settled in a quiescent zone. Froth is formed in the settler; this froth is surprisingly low in solids and water. The tailings stream from the settler is recycled to the front end of the extraction process, thereby conserving water. The invention provides an alternative to the conventional subaeration cell used for treatment of the middlings stream.

Description

United States Patent [191 [111 3,864,251 Cymbalisty Feb. 4, 1975 [5 TREATMENT OF MIDDLINGS STREAM 3,661,774 5/1972 Masologites 210/83 x FROM HOT WATER PROCESS O 3,707,464 12/1972 Burns et al 210/44 RECOVERING BITUMEN FROM TAR SAND 3,723,309 3/1973 Garcia 210/44 [75] Inventor: Lubomyr M. 0. Cymbalisty,
Edmonton, Alberta, Canada Z;; g E tp t J h orne gen or lrm rnes e er 0 nson [73] Assignees: Canada-Cities Service, Ltd.; Atlantic Richfield Canada, Ltd.; Imperial Oil Llmlted 57 ABSTRACT [22] F'led: 1974 This process relates to treating the middlings stream [21] Appl. No.: 435,515 from the primary separation cell used in the hot water process for extracting bitumen from tar sand. The middlings stream is diluted with hot water and settled [52] Cl 210/44 210/56 347 in a quiescent zone. Froth is formed in the settler; this [51] I t Cl Bold 2mm froth is surprisingly low in solids and water. The tail- [58] 5O 56 63 ings stream from the settler is recycled to the front 84 f i end of the extraction process, thereby conserving water. The invention provides an alternative to the conventional sub-aeration cell used for treatment of the [56] References Cited middlln s stream. UNITED STATES PATENTS g 3,526,585 9/1970 Camp 210/44 X 3 Claims, 2 Drawing Figures 32, 5 nor WATER HOT WATER PRIMARY FROTH TUMBLER SCREEN 4 6 MIXER L HOT WATER 3/ AIR FLOTATION SETTER CELL FROTH SAND TAIL INGS SETTER SAND TAIL INGS PAIEN TED 5 TAR SAND F, HOT wATER TUMBLING STEAM HOT SLURRY IFLOODING HOT WATER DILUTE HOT SLURRY BITUMEN PRIMARY SEPARATION FROTH BY RECYLE SAND SETTLING TAILINGS MIDDLINGS HOT wATER T M EA SECONDARY SEPARATION av SETTLING FINES AND WATER] I TAILINGS @256 HOT WATER HOT wATER I TUMBLER PRIMARY FROTH MIXER Q GE JOIWL AIR 3 f i FLOTATION SETTER CELL FROTH SAND TAILINGS SETTER SAND TAIL INGS TREATMENT OF MIDDLINGS STREAM FROM HOT WATER PROCESS FOR RECOVERING BITUMEN FROM TAR SAND BACKGROUND OF THE INVENTION This invention relates to a hot water process for recovering bitumen frorn tar sand.
The invention has been developed using tar sand from the Athabasca deposit at Fort McMurray, Alberta, Can. While it is described with reference to that feed stock, the invention may find beneficial application to tar sands present in other deposits.
Athabasca tar sands comprises sand grains which are each sheathed in a thin layer of water. Bitumen is trapped in the void space between the water-wet grains. By way of example, the composition of the tar sand might be percent by weight bitumen, 4 percent water, and 86 percent solids.
Athabasca tar sands are presently processed using a method commonly referred to as the hot water method. In accordance with this process, tar sand is mixed in a conditioning drum or tumbler with hot water and steam. While in the tumbler, the tar sand disintegrates and at the same time liberated bitumen is aerated. By disintegrate is meant that the sand and bitumen particles are dispersed one from another in preliminary way. The tumbler product is a porridge-like slurry which typically might comprise 9.5 percent bitumen, 22.00 percent water and 68.5 percent solids, at a temperature of l85l90F.
The slurry is flooded with additional hot water to further disperse the sand and bitumen. This flooding operation is usually carried out at a screen positioned at the outlet from the tumbler. The flooded slurry typically might have a composition of7 percent bitumen, 43 percent water, and 50 percent solids, and a temperature of 160F.
The flooded slurry is introduced into a separation cell at about its longitudinal midpoint; this cell is a cylindrical vessel having a conical bottom. The major portion of the solids, particularly the coarse sand particles, settle to the bottom of the cell; most of the bitumen particles, which have preferentially become attached to bubbles of air, rise to the top surface of the cell contents, where they collect in the form of a froth. The sand leaves the vessel through a bottom outlet and is discarded as tailings. The froth overflows the vessel wall into a launder and is removed for further treatment.
A middlings stream is continuously withdrawn from the separation cell at a point intermediate its upper and lower ends. This is done for two reasons. Firstly, a relatively large quantity of water must be added in the flooding stage to ensure that the bitumen and solids particles are sufficiently dispersed from one another in the separation cell to obtain reasonable froth product quality and bitumen recovery. Some of this water must be removed from the cell in the form of a middlings drag streamotherwise it will report to the bottom tailings stream. If too much water leaves with the sand tailings, bitumen is carried out with it and oil recoveries drop accordingly. Secondly, the solids known as fines (i.e., 325 mesh), present in the tar sands, tend to accumulate in the central portion of the cell. If the fines are present in too high a concentration, they tend to form a thick blanket, through which the aerated bitumen particles have difficulty in passing to reach the froth layer. It is therefore conventional to withdraw some of these fines in the middlings stream to relieve the congestion within the cell.
The middlings stream typically comprises 2 percent bitumen, 15 percent solids and 83 percent water.
The bitumen particles in the middlings stream are a mixed lot some are non-buoyant, perhaps because they are non-aerated or because they are attached to both solids and air; others are buoyant but were withdrawn through the middlings outlet before reaching the froth layer.
conventionally, the middlings stream from the separator cell is passed through a sub-aeration cell to recover contained bitumen. In this latter secondary recovery cell, the middlings are turbulently mixed with air to bring the bitumen to the surface of the cell as a froth. This froth is badly contaminated with solids and water a typical composition might be 16 percent weight solids, 54 percent water and 31 percent bitumen.
Once the bitumen has been extracted from the tar sand in this fashion, the primary and secondary froths are combined, diluted with a specific gravity-altering diluent, such as naphtha, and treated in a centrifuge circuit to separate the solids and water from the bitumen. Erosion of these centrifuges, particularly by the fines present in the froth, is a serious problem. Therefore any reduction in fines content in the feed to the centrifuge circuit is desirable.
SUMMARY OF THE INVENTION It is therefore one object of this invention to provide a process for treating middlings whereby a product which is comparatively lower in solids content is obtained.
It is another object to provide a process wherein the middlings are diluted by the addition of hot water, to improve secondary froth quality and in which the water added is conserved by recycling to the front end of the process.
In accordance with the invention, the middlings stream is diluted with hot water, preferably contacted with minute air bubbles to aerate non-buoyant bitumen, and introduced into a settler vessel. In the quiescent and dilute environment within this vessel, the buoyant bitumen forms a froth product which is reduced in solids and water content in comparison to the prior art secondary recovery froth obtained by subaeration flotation. Solids, water and traces of bitumen are withdrawn from the vessel through the tailings outlet. Part of this tailings stream may be recycled to the front end of the process for repeated treatment in the separation cell. In this manner, hot water is conserved within the process. The remainder of the tailings stream may be discarded or otherwise processed for recovery of contained bitumen. The froth product from the settler is preferably combined with the primary froth from the separation cell and forwarded on to the froth treatment circuit.
DESCRIPTION OF THE DRAWINGS FIG. 1 is a block diagram illustrating the steps of the process; and
FIG. 2 is a schematic illustration of the equipment used in the process.
DESCRIPTION OF THE PREFERRED EMBODIMENT The invention and its benefits are illustrated in the following example;
1360 pounds per hour of Athabasca tar sand, comprising l 1 percent by weight bitumen, 4 percent water, and 85 percent solids, including l2 percent fines, is fed to a tumbler l. Sufficient fresh hot water, approximately 290 pounds per hour, is added to the tar sand in the tumbler l to produce a slurry containing 22 percent by weight water. The product slurry is observed to have a temperature of l60F. The residence time in the tumbler is approximately 3 /2minutes.
The slurry is fed from the tumbler 1 into a separation cell 3. Water at 180F is added to the slurry at the screen 4 to raise the water content to approximately 42 percent. The separation cell 3 and settler 5 are both filled with clear water at l80F at the time that the test run is initiated. Froth, comprising 70 percent bitumen, 6 percent solids, 24 percent water, is produced at the surface of the separation cell at a rate of I70 pounds per hour. A tailings stream, comprising 70 percent solids, 0.8 percent bitumen and 29.2 percent water, is produced from the cell at a rate of l,l80 pounds per hour.
A middlings stream, comprising 2 percent bitumen, percent solids, and 83 percent water, is withdrawn from the separation cell by a pump 6 at a rate of 900 pounds per hour. This stream is mixed with 200 pounds per hour of water and approximately 0.1 CFH air in a mixer 7 and is then pumped to the settler.
The diluted middlings stream is introduced to the central portion of the settler through a rotating, perforated distribution pipe 8. A froth product is continuously formed and withdrawn at the rate of 19 lbs. per hour from the settler. This froth product comprises 77 percent bitumen, 5 percent solids, and 18 percent water. A stream of dilute solids and water is continuously withdrawn through the tailings outlet of the settler vessel and is recycled to the front end of extraction.
By way of comparison, the same middlings stream, when fed directly to a sub-aeration secondary recovery cell, gives a froth product comprising 52 percent bitumen, 13 percent solids and 35 percent water.
Obvious variations in the specific details described may be made without departing from the spirit of the invention and such embodiments of the invention as come within the scope and perview of the appended claims are to be considered as part of this invention.
What is claimed is:
1. In a continuous process for recovering bitumen from tar sand comprising combining the tar sand with air and hot water in a tumbler to disintegrate the tar sand and produce a hot slurry. diluting the slurry with water, introducing the dilute slurry into a separation cell wherein coarse solids settle out to form a tailings product, aerated bitumen rises to the surface of the cell contents and forms a froth product, and a middlings stream is withdrawn from the cell, said stream comprising bitumen, fine solids and water, the improvement which comprises:
diluting the middlings stream with hot water; and
introducing the diluted middlings stream into a settler vessel and holding it therein for a sufficient period of time to allow the major portion of the bitumen in the stream to rise to the surface of the vessel contents and form a froth product;
withdrawing the froth product; and
withdrawing a tailings stream from the base of the vessel, said tailings stream comprising the major portion of the fine solids and water introduced into the vessel.
2. The process as set forth in claim 1 wherein:
at least part of the tailings stream from the settler vessel is recycled for repeated treatment in the separation cell.
3. The process as set forth in claim 1 wherein:
the middlings stream is aerated prior to entry into the settler vessel to facilitate bitumen flotation.

Claims (3)

1. IN A CONTINUOUS PROCESS FOR RECOVERING BITUMEN FROM TAR SAND COMPRISING COMBINING THE TAR SAND WITH AIR AND HOT WATER IN A TUMBLER TO DISINTERGRATE THE TAR SAND AND PRODUCE A HOT SLURRY, DILUTING THE SLURRY WITH WATER, INTRODUCING THE DILUTE SLURRY INTO A SEPARATION CELL WHEREIN COARSE SOLIDS SETTLE OUT TO FORM A TAILINGS PRODUCT, AERATED BITUMEN RISES TO THE SURFACE OF THE CELL CONTENTS AND FORMS A FROTH PRODUCT, AND A MIDDLINGS STREAM IS WITHDRAWN FROM THE CELL, SAID STREAM COMPRISING BITUMEN, FINE SOLIDS AND WATER, THE IMPROVEMENT WHICH COMPRISES: DILUTING THE MIDDLINGS STREAM WITH HOT WATER; AND INTRODUCING THE DILUTED MIDDLINGS STREAM INTO A SETTLER VESSEL AND HOLDING IT THEREIN FOR A SUFFICIENT PERIOD OF TIME TO ALLOW THE MAJOR PORTION OF THE BITUMEN IN THE STREAM TO RISE TO THE SURFACE OF THE VESSEL CONTENTS AND FORM A FROTH PRODUCT; WITHDRAWING THE FROTH PRODUCT; AND WITHDRAWING A TAILINGS STREAM FROM THE BASE OF THE VESSEL, SAID TAILINGS STREAM COMPRISING THE MAJOR PORTION OF THE FINE SOLIDS AND WATER INTRODUCED INTO THE VESSEL.
2. The process as set forth in claim 1 wherein: at least part of the tailings stream from the settler vessel is recycled for repeated treatment in the separation cell.
3. The process as set forth in claim 1 wherein: the middlings stream is aerated prior to entry into the settler vessel to facilitate bitumen flotation.
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Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4033853A (en) * 1976-01-16 1977-07-05 Great Canadian Oil Sands Limited Process and apparatus for heating and deaerating raw bituminous froth
US4040961A (en) * 1975-06-26 1977-08-09 Coaltek Associates Separation of solids from a liquid
FR2340133A1 (en) * 1976-02-09 1977-09-02 Still Carl PROCESS AND INSTALLATION FOR SEPARATING TAR AND AMMONIACAL WATER CONTAINED IN THE EFFLUENTS OF COKE OVENS
US4086144A (en) * 1974-11-16 1978-04-25 Bergwerksverband Gmbh Process and apparatus for the separation of float tars in the tar separator of a coking installation
US4193869A (en) * 1974-11-21 1980-03-18 Milton Brucker Wastewater and wastewater solid processing system
JPS55129167A (en) * 1979-03-27 1980-10-06 Chevron Res Separating method
US4269693A (en) * 1978-05-30 1981-05-26 Hastie Anthony M B Process for recovering bitumen from waste bituminous products
US4395337A (en) * 1980-07-01 1983-07-26 Francis Hankin & Co. Limited Treatment of brackish water
US4783268A (en) * 1987-12-28 1988-11-08 Alberta Energy Company, Ltd. Microbubble flotation process for the separation of bitumen from an oil sands slurry
US4851123A (en) * 1986-11-20 1989-07-25 Tetra Resources, Inc. Separation process for treatment of oily sludge
GB2213400A (en) * 1987-12-14 1989-08-16 Hydro Int Ltd Separating grit from sewage
US5006239A (en) * 1986-11-20 1991-04-09 Tetra Technologies, Inc. apparatus for treatment of oily sludge
US5264118A (en) * 1989-11-24 1993-11-23 Alberta Energy Company, Ltd. Pipeline conditioning process for mined oil-sand
US5316664A (en) * 1986-11-24 1994-05-31 Canadian Occidental Petroleum, Ltd. Process for recovery of hydrocarbons and rejection of sand
US5340467A (en) * 1986-11-24 1994-08-23 Canadian Occidental Petroleum Ltd. Process for recovery of hydrocarbons and rejection of sand
US5460270A (en) * 1993-08-20 1995-10-24 Alberta Energy Company Ltd. Oil sand extraction process with in-line middlings aeration and recycle
GB2316333A (en) * 1996-08-14 1998-02-25 Ecc Int Ltd Process for treating a waste material
US6254771B1 (en) * 1997-02-05 2001-07-03 Mitsubishi Heavy Industries, Ltd. Method of processing desulfurization absorption liquid and apparatus therefor

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3526585A (en) * 1968-01-22 1970-09-01 Great Canadian Oil Sands Removing suspended solids from a liquid
US3661774A (en) * 1970-10-28 1972-05-09 Atlantic Richfield Co Separation of solids from a liquid
US3707464A (en) * 1971-07-15 1972-12-26 Petrolite Corp Process for clarifying an oil-solids contaminated aqueous stream
US3723309A (en) * 1971-09-20 1973-03-27 Exxon Production Research Co System and method for cleaning oily solid material

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3526585A (en) * 1968-01-22 1970-09-01 Great Canadian Oil Sands Removing suspended solids from a liquid
US3661774A (en) * 1970-10-28 1972-05-09 Atlantic Richfield Co Separation of solids from a liquid
US3707464A (en) * 1971-07-15 1972-12-26 Petrolite Corp Process for clarifying an oil-solids contaminated aqueous stream
US3723309A (en) * 1971-09-20 1973-03-27 Exxon Production Research Co System and method for cleaning oily solid material

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4086144A (en) * 1974-11-16 1978-04-25 Bergwerksverband Gmbh Process and apparatus for the separation of float tars in the tar separator of a coking installation
US4193869A (en) * 1974-11-21 1980-03-18 Milton Brucker Wastewater and wastewater solid processing system
US4040961A (en) * 1975-06-26 1977-08-09 Coaltek Associates Separation of solids from a liquid
US4033853A (en) * 1976-01-16 1977-07-05 Great Canadian Oil Sands Limited Process and apparatus for heating and deaerating raw bituminous froth
FR2340133A1 (en) * 1976-02-09 1977-09-02 Still Carl PROCESS AND INSTALLATION FOR SEPARATING TAR AND AMMONIACAL WATER CONTAINED IN THE EFFLUENTS OF COKE OVENS
US4269693A (en) * 1978-05-30 1981-05-26 Hastie Anthony M B Process for recovering bitumen from waste bituminous products
JPS55129167A (en) * 1979-03-27 1980-10-06 Chevron Res Separating method
JPS6240064B2 (en) * 1979-03-27 1987-08-26 Chevron Res
US4395337A (en) * 1980-07-01 1983-07-26 Francis Hankin & Co. Limited Treatment of brackish water
US4851123A (en) * 1986-11-20 1989-07-25 Tetra Resources, Inc. Separation process for treatment of oily sludge
US5006239A (en) * 1986-11-20 1991-04-09 Tetra Technologies, Inc. apparatus for treatment of oily sludge
US5316664A (en) * 1986-11-24 1994-05-31 Canadian Occidental Petroleum, Ltd. Process for recovery of hydrocarbons and rejection of sand
US5340467A (en) * 1986-11-24 1994-08-23 Canadian Occidental Petroleum Ltd. Process for recovery of hydrocarbons and rejection of sand
GB2213400A (en) * 1987-12-14 1989-08-16 Hydro Int Ltd Separating grit from sewage
GB2213400B (en) * 1987-12-14 1992-04-22 Hydro Int Ltd Separator
US4783268A (en) * 1987-12-28 1988-11-08 Alberta Energy Company, Ltd. Microbubble flotation process for the separation of bitumen from an oil sands slurry
US5264118A (en) * 1989-11-24 1993-11-23 Alberta Energy Company, Ltd. Pipeline conditioning process for mined oil-sand
US5460270A (en) * 1993-08-20 1995-10-24 Alberta Energy Company Ltd. Oil sand extraction process with in-line middlings aeration and recycle
GB2316333A (en) * 1996-08-14 1998-02-25 Ecc Int Ltd Process for treating a waste material
US5846314A (en) * 1996-08-14 1998-12-08 Ecc International Ltd. Process for treating a waste material resulting from an oil recovery from tar sands process
US6254771B1 (en) * 1997-02-05 2001-07-03 Mitsubishi Heavy Industries, Ltd. Method of processing desulfurization absorption liquid and apparatus therefor

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