CA1094484A - Flotation and centrifugation method for recovery of hydrocarbons from dilution centrifuging tailings - Google Patents
Flotation and centrifugation method for recovery of hydrocarbons from dilution centrifuging tailingsInfo
- Publication number
- CA1094484A CA1094484A CA287,612A CA287612A CA1094484A CA 1094484 A CA1094484 A CA 1094484A CA 287612 A CA287612 A CA 287612A CA 1094484 A CA1094484 A CA 1094484A
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- CA
- Canada
- Prior art keywords
- tailings
- froth
- water
- solids
- hydrocarbons
- 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.)
- Expired
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
"FLOTATION AND CENTRIFUGATION METHOD FOR
RECOVERY OF HYDROCARBONS FROM
DILUTION CENTRIFUGING TAILINGS"
ABSTRACT OF THE DISCLOSURE
The invention has to do with treatment of dilution centrifuging tailings which are produced in connection with a hot water extraction operation for recovery of bitumen from oil sands. The tailings are subjected to induced gas flotation for a predetermined period of time to recover con-tained hydrocarbons as froth. The froth is then diluted with naphtha and centrifuged in two stages to recover most of the hydrocarbons in the froth as a processable product while reject-ing solids and water.
RECOVERY OF HYDROCARBONS FROM
DILUTION CENTRIFUGING TAILINGS"
ABSTRACT OF THE DISCLOSURE
The invention has to do with treatment of dilution centrifuging tailings which are produced in connection with a hot water extraction operation for recovery of bitumen from oil sands. The tailings are subjected to induced gas flotation for a predetermined period of time to recover con-tained hydrocarbons as froth. The froth is then diluted with naphtha and centrifuged in two stages to recover most of the hydrocarbons in the froth as a processable product while reject-ing solids and water.
Description
L~ ~184 BACXG~OI~ND OF TEE- I~VENTION
This invention relates to a process for recover-ing hydrocarbons from tailings produced by a dilution centri-fuging circuit within an oil sand operation employing the known hot water extraction process.
The hot water extraction process, used commer-cially to recover bitumen from the Alberta oil sands, involves the following series of steps:
tl) slurrying, heating and conditioning the oil sand in a rotating drum in which it is mixed with steam, hot water and caustic;
This invention relates to a process for recover-ing hydrocarbons from tailings produced by a dilution centri-fuging circuit within an oil sand operation employing the known hot water extraction process.
The hot water extraction process, used commer-cially to recover bitumen from the Alberta oil sands, involves the following series of steps:
tl) slurrying, heating and conditioning the oil sand in a rotating drum in which it is mixed with steam, hot water and caustic;
(2) diluting the slurry with more hot water and introducing it into a primary separation vessel where it is retained to permit buoyant bitumen particles to rise to the surface and form primary froth;
(3) withdrawing a stream of middlings from the midpoint of the separation vessel and sub-jecting it to induced air flotation in a secondary recovery flotation cell to cause contained bitumen to form secondary froth;
and
and
(4) combining the primary and secondary froths to form a combined froth product.
The dilution centrifuging process used to remove water and solids from the froth product of the hot water ex-traction process involves the following steps:
(1) diluting the combined froth product with naphtha to alter the viscosity and specific gravity of the contained bitumen; and (2) introducing the diluted froth into a two-''` ` ' ~ :`
4~8~
stage centrifugal separation circuit where the coarse solids are separated from the stream in a scroll-type centrifuge and the water and fine solids are separated in a disc-type centrifuge.
There is a significant loss of hydrocarbons in the dilution centrifuging (D.C.) tailings produced by the scroll and disc cen~rifuges. More particularly, in the plant presently being constructed by the assignee of this invention, there will be approximately 1.6 million pounds/hour of D.C.
tailings produced containing approximately 3.5% by weight bitu-men, 2.1~ hydrocarbon diluent, 24.0~ solids and 70.4~ water.
The losses of bitumen and diluent per day will be approximately 3,900 barrels and 3,200 barrels, respectively. These figures are only given by way of example, as it is expected that they will vary significantly with plant operating conditions and throughput.
The tailings composition shown above corresponds to the predicted values for a commercial plant. The tailings ~ actually used in developing this invention were derived from pilot plant operations and contained a significantly greater proportion of water, as indicated in Example I. This extra water is a direct result of the mechanical configuration of the pilot plant centrifuges. However, the recovery of hydrocarbon from the pilot plant tailings should be more difficult than it will be from the commercial plant tailings, because the hydro-carbon content of the pilot plant tailings is reduced by the extra water.
A problem which has heretofore existed was how to economically recover the hydrocarbons contained in the D.C.
tailings. If such a process could be developed, it would also -` 10!~ 8~
be desirable that the diluent and bitumen be recovered in a single step.
In this regard, it needs to be kept in mind that the D.C. tailings is a unique and difficult material to deal with. It contains a relatively small amount of bitumen and diluent distributed throughout a large quantity of water and solids. The bitumen in the D.C. tailings is originally recovered as part of the ~roth produçed ~y the hot water ex-traction process. Its rejection to the D.C. tailings together with the proportionate amount of diluent suggests that these hydrocarbons are physically associated with the froth solids and are not recoverable by dilution centrifuging.
SUMM~R~ OF TH~ INVENTION
It has now been found that induced gas flotation can successfully be applied to D.C. tailings to recover the major portion of the bitumen and diluent. The froth which is produced is found to be relatively high in solids and water content, when compared with the froth produced by the primary separation vessel.
It has also been discoyered that the major portion of the hydrocarbons contained in the froth can be recovered by mixing the froth with additional hydrocarbGn diluent and passing the diluted froth through scroll-type and disc-type centrifuge separators in series. 5atisfactory re-covery of the original hydrocarbons and rejection of the contained water and solids is best achieved when the added diluent brings the diluent to bitumen weight ratio in the mixture to a value above 1.0O
Broadly stated, the invention is a method for treating tailings from the dilution centrifuging circuit 10~ 34 of a hot water extraction complex for the recovery of bitumen from oil sands, said tailings containing bitumen, hydrocarbon diluent, solids and water, comprising: introducing the tailings into a flotation cell and retaining it therein for a sufficient period of time, while subjecting it to agitation and flotation using gas introduced into the base of the body of tailings, to recover a significant portion of the conta.~ned bitumen and diluent as froth and reject a portion of the solids and water as underflow;
mixing t~e froth with a further portion of hydrocarbon ~ .
diluent; treating the diluted froth in a scroll-type centrifugal separator to reject solids, water and a minor part of the hydrocarbons in the diluted froth as tailings-, and produce a first product stream comprising hydrocarbons, water and a minor part of the solids in the diluted froth; and treating the first product stream in a disc-type centrifugal separator to reject water, solids and a minor part of ~he hydrocarbons in the first product stream as tailings, and produce a second product stream comprising hydrocarbons and a minor part of the water and solids in the first product stream~
- 4a --- ~o~
.
DESCRIPTION OF THE PR~FE~R~ ~MBODIME~IT
The in~ention is exemplified by the following example:
A mixture of pilot plant D.C. tailings was prepared by mixing 1 part of scroll centrifuge tailings with 12 parts of disc centrifuge tailings. Mixing was carried out by placing 250 pounds of scroll tailings and 350 Imperial gallons of disc tailings in a tank 1 and heating them to 170F
over a period of 1 hour while agitating them. The mixture formed had a composition of 1.70~ by weight hydrocarbons, 6.85~ solids and 91.45% water.
This mixture was fed at a rate of 23.5 lbs./min.
into a ban~ of flotation cells 2 consisting of three 0.8 cubic foot capacity cells. These cells were connected in series such that the under~low from one cell became the feed for the next cell. Each cell was equipped with a Den~er* Sub-A type aeration impellor and air was introduced into the tailings through the impellor mechanism as the mixture was agitated.
The nominal operation con~itions for each cell in the bank were as follows:
retention time ~ 2.26 impeIlor speed - 750 r~p.m.
air rate - 0.175 SC~M/cu. ft~ of cell volume power input - 0.09 HP/cu. ft. of cell volume.
The froth produced from the three cells was combined to yield 2.25 lb~min~ of total froth while the final (Cell 3) tailings were produced at a rate of 21.25 lbs./min.
Total froth and final tailings had the following compositions:
4~4 TAsLE I
% by we~ightTot;al Froth Final Taillngs Hydrocarbons16.2~ 0.19 Solids 31.73 4.66 Water 51.99 95.15 Since the throughput requirements of the experi-mental flotation bank were much less than that of the centrifu-gation equipment, it was necessary to accumulate the froth produced from a number of flotation tests. The froth com-position shown above is representative of one flotation test.Froth was accumulated for centrifu~ation test work in barrels which stood for several days prior to testing. A small portion of clear water was drained from the barrels leaving a total accumulated froth having the following composition:
TABLE II
% by weightA u~ulated Froth Hydrocarbon20.25 Solids 35.32 Water 44-43 600 lbs. of the froth, having a temperature of about 120F, were introduced into a mixer 3 and mixed therein with 119 lbs. of hydrocarbon diluent having a temperature of 60F, said diluent in this case being a naphtha fraction having a boiling point within the range 150F to 450F. The mixture was stirred and heated to a final temperature of 170F.
The diluted ~roth has a composition as follows:
~3~18~
TABI,E III
% by weight Diluted Froth EIydrocarbon 33.48 Solids 29.~5 Water 37.07 Work to date indicates that in the order of 1 to 3 parts of diluent per part of hydrocarbon in the froth is suitable for rendering the bitumen amenable to separation by centrifugal separation.
The diluted froth was fed at 30 I.G.p~m.
into a 12 inch diameter x 30 inch long Bird* scroll-type centrifugal separator 4 operated at the following conditions:
Bowl Speed- 1350 r.p.m.
Pool Depth- 0.43 inches The compositions and rates of the products obtained from the scroll separator are as follows:
TABLE IV
O by weightScroll Ta-ilings Scroll Product Hydrocarbons5.46 56.51 Solids 78.01 5.66 Water 16.53 37.83 Feed Split30.5 69.5 The material balance closures on hydrocarbon, water and solids are 81.8%, 118.3% and 106.1% respectively and in light of the difficulties encountered with such a test, this closure is deemed adequate~ Despite the difficulties with material balance closure, it can be concluded that:
(1) only a minor part of the hydrocarbons originally in the diluted froth reports in the tailings o~ the scroll separator;
and (23 most of the solids are removed by the separator so that the product stream only contains a minor part of the solids originally in th.e dlluted froth.
10~ 34 The product from the scroll centri~uge test was accumulated in a tank and used to run a number of tests in a De Laval*SX 204-T disc type centrifugal separator.
Since the tankage was poorly agitated the composition of disc centrifuge feed tended to vary from test to test. One particu-lar test utilized a feed having the following composition:
TABL~ V
~'by'wè`i'ght'Disc`Feed Hydrocarbons68.12 Solias 3.67 Water 28~22 The product was passed into a De Laval* SX 204-T
disc-type centrifugal separator at a xate of 9 I.G.P.M. This separator was operated at the following conditions:
Bowl Speed5650 r.p.m~
Disc Spacing0.5 mm Capacitance Tank Pres-sure 10 psig Product Back Pressure 10 psig The compositions and rates of the products obtained from the disc separator are as follows:
T~BLE VI
'%'by wei~ht'Disc Tailings Disc Product Hydrocar~ons0.36 84.39 Solids 0.71 4.20 Water 98.93 11.42 It is to be noted that: (1) the disc separator rejects most of the solids and water but only a minor part of the hydrocarbons in the feed from the scroll separator; and (2~ the product stream from the disc separator is essentially hydrocarbons and contains only a minor part of the solids and water in the original feed.
* - indicates registered trade mark
The dilution centrifuging process used to remove water and solids from the froth product of the hot water ex-traction process involves the following steps:
(1) diluting the combined froth product with naphtha to alter the viscosity and specific gravity of the contained bitumen; and (2) introducing the diluted froth into a two-''` ` ' ~ :`
4~8~
stage centrifugal separation circuit where the coarse solids are separated from the stream in a scroll-type centrifuge and the water and fine solids are separated in a disc-type centrifuge.
There is a significant loss of hydrocarbons in the dilution centrifuging (D.C.) tailings produced by the scroll and disc cen~rifuges. More particularly, in the plant presently being constructed by the assignee of this invention, there will be approximately 1.6 million pounds/hour of D.C.
tailings produced containing approximately 3.5% by weight bitu-men, 2.1~ hydrocarbon diluent, 24.0~ solids and 70.4~ water.
The losses of bitumen and diluent per day will be approximately 3,900 barrels and 3,200 barrels, respectively. These figures are only given by way of example, as it is expected that they will vary significantly with plant operating conditions and throughput.
The tailings composition shown above corresponds to the predicted values for a commercial plant. The tailings ~ actually used in developing this invention were derived from pilot plant operations and contained a significantly greater proportion of water, as indicated in Example I. This extra water is a direct result of the mechanical configuration of the pilot plant centrifuges. However, the recovery of hydrocarbon from the pilot plant tailings should be more difficult than it will be from the commercial plant tailings, because the hydro-carbon content of the pilot plant tailings is reduced by the extra water.
A problem which has heretofore existed was how to economically recover the hydrocarbons contained in the D.C.
tailings. If such a process could be developed, it would also -` 10!~ 8~
be desirable that the diluent and bitumen be recovered in a single step.
In this regard, it needs to be kept in mind that the D.C. tailings is a unique and difficult material to deal with. It contains a relatively small amount of bitumen and diluent distributed throughout a large quantity of water and solids. The bitumen in the D.C. tailings is originally recovered as part of the ~roth produçed ~y the hot water ex-traction process. Its rejection to the D.C. tailings together with the proportionate amount of diluent suggests that these hydrocarbons are physically associated with the froth solids and are not recoverable by dilution centrifuging.
SUMM~R~ OF TH~ INVENTION
It has now been found that induced gas flotation can successfully be applied to D.C. tailings to recover the major portion of the bitumen and diluent. The froth which is produced is found to be relatively high in solids and water content, when compared with the froth produced by the primary separation vessel.
It has also been discoyered that the major portion of the hydrocarbons contained in the froth can be recovered by mixing the froth with additional hydrocarbGn diluent and passing the diluted froth through scroll-type and disc-type centrifuge separators in series. 5atisfactory re-covery of the original hydrocarbons and rejection of the contained water and solids is best achieved when the added diluent brings the diluent to bitumen weight ratio in the mixture to a value above 1.0O
Broadly stated, the invention is a method for treating tailings from the dilution centrifuging circuit 10~ 34 of a hot water extraction complex for the recovery of bitumen from oil sands, said tailings containing bitumen, hydrocarbon diluent, solids and water, comprising: introducing the tailings into a flotation cell and retaining it therein for a sufficient period of time, while subjecting it to agitation and flotation using gas introduced into the base of the body of tailings, to recover a significant portion of the conta.~ned bitumen and diluent as froth and reject a portion of the solids and water as underflow;
mixing t~e froth with a further portion of hydrocarbon ~ .
diluent; treating the diluted froth in a scroll-type centrifugal separator to reject solids, water and a minor part of the hydrocarbons in the diluted froth as tailings-, and produce a first product stream comprising hydrocarbons, water and a minor part of the solids in the diluted froth; and treating the first product stream in a disc-type centrifugal separator to reject water, solids and a minor part of ~he hydrocarbons in the first product stream as tailings, and produce a second product stream comprising hydrocarbons and a minor part of the water and solids in the first product stream~
- 4a --- ~o~
.
DESCRIPTION OF THE PR~FE~R~ ~MBODIME~IT
The in~ention is exemplified by the following example:
A mixture of pilot plant D.C. tailings was prepared by mixing 1 part of scroll centrifuge tailings with 12 parts of disc centrifuge tailings. Mixing was carried out by placing 250 pounds of scroll tailings and 350 Imperial gallons of disc tailings in a tank 1 and heating them to 170F
over a period of 1 hour while agitating them. The mixture formed had a composition of 1.70~ by weight hydrocarbons, 6.85~ solids and 91.45% water.
This mixture was fed at a rate of 23.5 lbs./min.
into a ban~ of flotation cells 2 consisting of three 0.8 cubic foot capacity cells. These cells were connected in series such that the under~low from one cell became the feed for the next cell. Each cell was equipped with a Den~er* Sub-A type aeration impellor and air was introduced into the tailings through the impellor mechanism as the mixture was agitated.
The nominal operation con~itions for each cell in the bank were as follows:
retention time ~ 2.26 impeIlor speed - 750 r~p.m.
air rate - 0.175 SC~M/cu. ft~ of cell volume power input - 0.09 HP/cu. ft. of cell volume.
The froth produced from the three cells was combined to yield 2.25 lb~min~ of total froth while the final (Cell 3) tailings were produced at a rate of 21.25 lbs./min.
Total froth and final tailings had the following compositions:
4~4 TAsLE I
% by we~ightTot;al Froth Final Taillngs Hydrocarbons16.2~ 0.19 Solids 31.73 4.66 Water 51.99 95.15 Since the throughput requirements of the experi-mental flotation bank were much less than that of the centrifu-gation equipment, it was necessary to accumulate the froth produced from a number of flotation tests. The froth com-position shown above is representative of one flotation test.Froth was accumulated for centrifu~ation test work in barrels which stood for several days prior to testing. A small portion of clear water was drained from the barrels leaving a total accumulated froth having the following composition:
TABLE II
% by weightA u~ulated Froth Hydrocarbon20.25 Solids 35.32 Water 44-43 600 lbs. of the froth, having a temperature of about 120F, were introduced into a mixer 3 and mixed therein with 119 lbs. of hydrocarbon diluent having a temperature of 60F, said diluent in this case being a naphtha fraction having a boiling point within the range 150F to 450F. The mixture was stirred and heated to a final temperature of 170F.
The diluted ~roth has a composition as follows:
~3~18~
TABI,E III
% by weight Diluted Froth EIydrocarbon 33.48 Solids 29.~5 Water 37.07 Work to date indicates that in the order of 1 to 3 parts of diluent per part of hydrocarbon in the froth is suitable for rendering the bitumen amenable to separation by centrifugal separation.
The diluted froth was fed at 30 I.G.p~m.
into a 12 inch diameter x 30 inch long Bird* scroll-type centrifugal separator 4 operated at the following conditions:
Bowl Speed- 1350 r.p.m.
Pool Depth- 0.43 inches The compositions and rates of the products obtained from the scroll separator are as follows:
TABLE IV
O by weightScroll Ta-ilings Scroll Product Hydrocarbons5.46 56.51 Solids 78.01 5.66 Water 16.53 37.83 Feed Split30.5 69.5 The material balance closures on hydrocarbon, water and solids are 81.8%, 118.3% and 106.1% respectively and in light of the difficulties encountered with such a test, this closure is deemed adequate~ Despite the difficulties with material balance closure, it can be concluded that:
(1) only a minor part of the hydrocarbons originally in the diluted froth reports in the tailings o~ the scroll separator;
and (23 most of the solids are removed by the separator so that the product stream only contains a minor part of the solids originally in th.e dlluted froth.
10~ 34 The product from the scroll centri~uge test was accumulated in a tank and used to run a number of tests in a De Laval*SX 204-T disc type centrifugal separator.
Since the tankage was poorly agitated the composition of disc centrifuge feed tended to vary from test to test. One particu-lar test utilized a feed having the following composition:
TABL~ V
~'by'wè`i'ght'Disc`Feed Hydrocarbons68.12 Solias 3.67 Water 28~22 The product was passed into a De Laval* SX 204-T
disc-type centrifugal separator at a xate of 9 I.G.P.M. This separator was operated at the following conditions:
Bowl Speed5650 r.p.m~
Disc Spacing0.5 mm Capacitance Tank Pres-sure 10 psig Product Back Pressure 10 psig The compositions and rates of the products obtained from the disc separator are as follows:
T~BLE VI
'%'by wei~ht'Disc Tailings Disc Product Hydrocar~ons0.36 84.39 Solids 0.71 4.20 Water 98.93 11.42 It is to be noted that: (1) the disc separator rejects most of the solids and water but only a minor part of the hydrocarbons in the feed from the scroll separator; and (2~ the product stream from the disc separator is essentially hydrocarbons and contains only a minor part of the solids and water in the original feed.
* - indicates registered trade mark
Claims (2)
1. A method for treating tailings from the dilution centrifuging circuit of a hot water extraction complex for the recovery of bitumen from oil sands, said tail-ings containing bitumen, hydrocarbon diluent, solids and water, comprising:
introducing the tailings into a flotation cell and retaining it therein for a sufficient period of time, while subjecting it to agitation and flotation using gas introduced into the base of the body of tailings, to recover a signifi-cant portion of the contained bitumen and diluent as froth and reject a portion of the solids and water as underflow;
mixing the froth with a further portion of hydrocarbon diluent;
treating the diluted froth in a scroll-type centrifugal separator to reject solids, water and a minor part of the hydrocarbons in the diluted froth as tailings, and pro-duce a first product stream comprising hydrocarbons, water and a minor part of the solids in the diluted froth; and treating the first product stream in a disc-type centrifugal separator to reject water, solids and a minor part of the hydrocarbons in the first product stream as tailings, and produce a second product stream comprising hydrocarbons and a minor part of the water and solids in the first product stream.
introducing the tailings into a flotation cell and retaining it therein for a sufficient period of time, while subjecting it to agitation and flotation using gas introduced into the base of the body of tailings, to recover a signifi-cant portion of the contained bitumen and diluent as froth and reject a portion of the solids and water as underflow;
mixing the froth with a further portion of hydrocarbon diluent;
treating the diluted froth in a scroll-type centrifugal separator to reject solids, water and a minor part of the hydrocarbons in the diluted froth as tailings, and pro-duce a first product stream comprising hydrocarbons, water and a minor part of the solids in the diluted froth; and treating the first product stream in a disc-type centrifugal separator to reject water, solids and a minor part of the hydrocarbons in the first product stream as tailings, and produce a second product stream comprising hydrocarbons and a minor part of the water and solids in the first product stream.
2. The process of claim 1 in which the diluted froth has a diluent to bitumen weight ratio greater than 1Ø
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA287,612A CA1094484A (en) | 1977-09-27 | 1977-09-27 | Flotation and centrifugation method for recovery of hydrocarbons from dilution centrifuging tailings |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA287,612A CA1094484A (en) | 1977-09-27 | 1977-09-27 | Flotation and centrifugation method for recovery of hydrocarbons from dilution centrifuging tailings |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1094484A true CA1094484A (en) | 1981-01-27 |
Family
ID=4109641
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA287,612A Expired CA1094484A (en) | 1977-09-27 | 1977-09-27 | Flotation and centrifugation method for recovery of hydrocarbons from dilution centrifuging tailings |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1094484A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4385982A (en) * | 1981-05-14 | 1983-05-31 | Conoco Inc. | Process for recovery of bitumen from tar sands |
| FR2587714A1 (en) * | 1985-09-20 | 1987-03-27 | Petroleo Brasileiro Sa | PROCESS FOR SEPARATING WATER AND SOLIDS FROM FUELS, ESPECIALLY SHALE OIL |
| US8382976B2 (en) | 2009-04-09 | 2013-02-26 | Titanium Corporation Inc. | Recovery of bitumen from froth treatment tailings |
| US8656996B2 (en) | 2010-11-19 | 2014-02-25 | Exxonmobil Upstream Research Company | Systems and methods for enhanced waterfloods |
| US8657000B2 (en) | 2010-11-19 | 2014-02-25 | Exxonmobil Upstream Research Company | Systems and methods for enhanced waterfloods |
| US8739869B2 (en) | 2010-11-19 | 2014-06-03 | Exxonmobil Upstream Research Company | Systems and methods for enhanced waterfloods |
| US8852429B2 (en) | 2010-02-22 | 2014-10-07 | Titanium Corporation Inc. | Method for processing froth treatment tailings |
| US8974661B2 (en) | 2010-12-30 | 2015-03-10 | Exxonmobil Upstream Research Company | Methods for separation of bitumen from oil sands |
| US9314713B2 (en) | 2010-05-12 | 2016-04-19 | Titanium Corporation | Apparatus and method for recovering a hydrocarbon diluent from tailings |
| US9719022B2 (en) | 2009-04-09 | 2017-08-01 | Titanium Corporation Inc. | Methods for separating a feed material derived from a process for recovering bitumen from oil sands |
-
1977
- 1977-09-27 CA CA287,612A patent/CA1094484A/en not_active Expired
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4385982A (en) * | 1981-05-14 | 1983-05-31 | Conoco Inc. | Process for recovery of bitumen from tar sands |
| FR2587714A1 (en) * | 1985-09-20 | 1987-03-27 | Petroleo Brasileiro Sa | PROCESS FOR SEPARATING WATER AND SOLIDS FROM FUELS, ESPECIALLY SHALE OIL |
| US4707275A (en) * | 1985-09-20 | 1987-11-17 | Petroleo Brasileiro Sa-Petrobras | Process for separating water and solids from fuels |
| US8382976B2 (en) | 2009-04-09 | 2013-02-26 | Titanium Corporation Inc. | Recovery of bitumen from froth treatment tailings |
| US9719022B2 (en) | 2009-04-09 | 2017-08-01 | Titanium Corporation Inc. | Methods for separating a feed material derived from a process for recovering bitumen from oil sands |
| US10087372B2 (en) | 2009-04-09 | 2018-10-02 | Titanium Corporation Inc. | Methods for separating a feed material derived from a process for recovering bitumen from oil sands |
| US8852429B2 (en) | 2010-02-22 | 2014-10-07 | Titanium Corporation Inc. | Method for processing froth treatment tailings |
| US9314713B2 (en) | 2010-05-12 | 2016-04-19 | Titanium Corporation | Apparatus and method for recovering a hydrocarbon diluent from tailings |
| US8656996B2 (en) | 2010-11-19 | 2014-02-25 | Exxonmobil Upstream Research Company | Systems and methods for enhanced waterfloods |
| US8657000B2 (en) | 2010-11-19 | 2014-02-25 | Exxonmobil Upstream Research Company | Systems and methods for enhanced waterfloods |
| US8739869B2 (en) | 2010-11-19 | 2014-06-03 | Exxonmobil Upstream Research Company | Systems and methods for enhanced waterfloods |
| US8974661B2 (en) | 2010-12-30 | 2015-03-10 | Exxonmobil Upstream Research Company | Methods for separation of bitumen from oil sands |
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