CA1267860A - Inclined plate settling of diluted bitumen froth - Google Patents
Inclined plate settling of diluted bitumen frothInfo
- Publication number
- CA1267860A CA1267860A CA000538412A CA538412A CA1267860A CA 1267860 A CA1267860 A CA 1267860A CA 000538412 A CA000538412 A CA 000538412A CA 538412 A CA538412 A CA 538412A CA 1267860 A CA1267860 A CA 1267860A
- Authority
- CA
- Canada
- Prior art keywords
- froth
- settler
- diluted
- hydrocarbon
- overflow
- 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
Links
Classifications
-
- 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
Abstract
"INCLINED PLATE SETTLING OF DILUTED BITUMEN FROTH"
ABSTRACT OF THE DISCLOSURE
'Diluted bituminous froth' is a product from the hot water extraction process for recovering bitumen from tar sand. This diluted froth is a mixture comprising bitumen, water, light hydrocarbon diluent, and particulate solids. In accordance with the invention, the diluted froth is treated in an inclined plate settler, before it enters the centrifuge circuit conventionally used to separate the components of the froth. The settler is controlled by varying its underflow withdrawal rate in response to the hydrocarbon content of the overflow from the settler, to maintain said overflow hydrocarbon content at a level which is sufficiently pure so as to be acceptable, after diluent removal, as feed to the downstream upgrading process. The underflow from the settler is passed to the centrifuge circuit to recover hydrocarbon therefrom. The composition of the underflow has been found to be less variable than the composition of the diluted froth feed, thereby making it easier to operate the centrifuge circuit.
ABSTRACT OF THE DISCLOSURE
'Diluted bituminous froth' is a product from the hot water extraction process for recovering bitumen from tar sand. This diluted froth is a mixture comprising bitumen, water, light hydrocarbon diluent, and particulate solids. In accordance with the invention, the diluted froth is treated in an inclined plate settler, before it enters the centrifuge circuit conventionally used to separate the components of the froth. The settler is controlled by varying its underflow withdrawal rate in response to the hydrocarbon content of the overflow from the settler, to maintain said overflow hydrocarbon content at a level which is sufficiently pure so as to be acceptable, after diluent removal, as feed to the downstream upgrading process. The underflow from the settler is passed to the centrifuge circuit to recover hydrocarbon therefrom. The composition of the underflow has been found to be less variable than the composition of the diluted froth feed, thereby making it easier to operate the centrifuge circuit.
Description
1~;786~3 1 FIELD OF T~IE INVENTION
2 The invention pertains to a process involving treating diluted
3 bituminous froth, from the known hot water extraction process, by passing4 said diluted froth through an inclined plate settler to recover part of the contained bitumen in a form pure enough to be fed directly to the 6 conventional downstream upgrading circuit.
8 There are large surface deposits of tar sand in the Athabasca9 region of Alberta. These deposits are presently being produced by two large commercial plants, one of which is owned by the assignee of this 11 application.
12 More particularly, these tar sand deposits are being mined 13 and the valuable contained component, bitumen, is extracted and recovered 14 by a process known as 'the hot water process'. The recovered bitumen is then upgraded in a refinery-type facility to produce hydrocarbon products 16 hav;ng various commercial uses.
17 In this hot water process~ the as-mined tar sand is introduced 18 into a horizontal rotating drum, together with hot water and caustic.
19 The m;xture is retained in the drum for a short period while the ingredients mix, the tar sand ;s heated, and the components of the tar sand are dispersed 21 in the water. The step is referred to as 'conditioning'. The slurry that22 emerges from the drum is diluted with additional hot water and screened 23 to remove rocks and oversize lumps of tar sand. The screened slurry is 2~ passed into a thickener-like vessel (referred to as the 'PSV', for 'primary ~3 separation vessel'). ~lere the slurry is retained for a period of time ~ under quiescent conditions. Bitumen globules, which have become aerated 27 in the conditioning step, rise to the surface of the PSV contents and fcrm 2~ a froth. This froth, called 'primary froth', is recovered. The primary 29 froth has a bitumen content of about 65% by weight, the balance being - 2 - -~
~;~678Ç~() 1 contaminants,in the form of water and solids. Most of the sand present in 2 the slurry drops downwardly into the conical lower end of the PSV and is 3 concentrated therein. The sand is removed through the bottom outlet.
8 There are large surface deposits of tar sand in the Athabasca9 region of Alberta. These deposits are presently being produced by two large commercial plants, one of which is owned by the assignee of this 11 application.
12 More particularly, these tar sand deposits are being mined 13 and the valuable contained component, bitumen, is extracted and recovered 14 by a process known as 'the hot water process'. The recovered bitumen is then upgraded in a refinery-type facility to produce hydrocarbon products 16 hav;ng various commercial uses.
17 In this hot water process~ the as-mined tar sand is introduced 18 into a horizontal rotating drum, together with hot water and caustic.
19 The m;xture is retained in the drum for a short period while the ingredients mix, the tar sand ;s heated, and the components of the tar sand are dispersed 21 in the water. The step is referred to as 'conditioning'. The slurry that22 emerges from the drum is diluted with additional hot water and screened 23 to remove rocks and oversize lumps of tar sand. The screened slurry is 2~ passed into a thickener-like vessel (referred to as the 'PSV', for 'primary ~3 separation vessel'). ~lere the slurry is retained for a period of time ~ under quiescent conditions. Bitumen globules, which have become aerated 27 in the conditioning step, rise to the surface of the PSV contents and fcrm 2~ a froth. This froth, called 'primary froth', is recovered. The primary 29 froth has a bitumen content of about 65% by weight, the balance being - 2 - -~
~;~678Ç~() 1 contaminants,in the form of water and solids. Most of the sand present in 2 the slurry drops downwardly into the conical lower end of the PSV and is 3 concentrated therein. The sand is removed through the bottom outlet.
4 This stream, referred to as 'primary tailings', is discarded. Some bitumen, which has failed to ascend to the ~roth layer, and some solids remain in 6 the watery layer between the froth and the concentrated sand. This mixture 7 is referred to as 'middlings'. A stream of the middlings is continuously 8 withdrawn from the PSV and advanced to sub-aerated flotation cells. Here 9 the middlings are subjected to vigorous agitation and aeration. A froth layer is produced by the cells as a result of this treatment - the froth 11 is referred to as Isecondary froth'. This secondary froth is 'dirtier' 12 than the primary froth - it has a relatively high content of water and 13 solids. The bitumen content is commonly only about 25%. The secondary froth 14 is passed into a tank and retained for a period of time, to allow some of the solids and water to settle. The 'cleaned' secondary fro-th is de-16 canted off and recombined with the primary froth to produce the 'combined 17 froth product'.
18 This combined froth produce is not acceptable yet For processing 19 in the upgrading circuit. The water and solids associated with the froth, partially in an emulsified form, must be removed to produce a hydrocarbon 21 product which, after diluent removalJ is suitable for upgrading. Such a 22 product preferably is one containing at least 95% by weight hydrocarbon.
23 The cleaning of the combined froth product is conventionally 24 accomplished by a process referred to as 'dilution centrifuging'.
Dilution centrifuging involves first adding naphtha to the 26 combined froth product. This is done to give a less viscous hydrocarbon 27 phase and to increase the density difference between the hydrocarbon phase 28 and the water and solids phases. The resulting 'diluted froth' is now 29 amenable to treatment in centrifuges to e-ffect separation of ~he bitumen from the water and solids.
6() 1 The commercially practised centrifuging process is carried 2 out in a two step operation. More particularly, the diluted froth is 3 first fed to a scroll-type centrifuge, which is adapted to remove the coarse 4 solids from the feedstock. The hydrocarban~rich product from the scroll centrifuge is then passed to a disc-type centrifuge, to separate the 6 hydrocarbon from the remaining water and fine solids.
7 While the two stage centrifuging circuit has been used for 8 years in the two plants in operation, there are a good many problems 9 associated with it.
For example, one problem has to do with the fact that the 1l composition of the diluted froth can vary quite widely, as a result of 12 variations in the composition of the tar sand itself. The following 3 compositions are typical of froth compositions for 'high' and 'low' 4 quality froths that are produced in applicant's plant:
High quality Low quality 16 Hydrocarbon 80 55 17 Solids S 8 18 Water 15 37 19 Taking the case of the disc centrifuge, it has internal components7 (such as discs and nozzles) which have operating parameters 21 (such as disc spacing and size of nozzles). Once these parameters are 22 set, they cannot be changed while the machine is in operation. So once 23 the parameter design is established for the machine, it has only a narrow 24 range of froth compositions that it can handleg at normal operating speed.
To provide disc centrifuge capacity adequate to cope with the 26 variable feed, it is therefore necessary to provide an excess of machines, 27 some of which are therefore standing idle much of the time.
28 Another significant problem characterizing the centrifuge 29 circuit is its very high maintenance cost. The wear on ~he machines, gi~len the erosive nature of the mixture being processed~ is almost 31 prohibitive.
3L~ 7~36~3 1 The reason that the centrifuge circuit is in fact used is that 2 it leads to a final hydrocarbon product of the desired quality. Typically, 3 the disc centrifuge product comprises:
4 Hydrocarbon 95% by wt.
Solids 4.5%
6 Water 0.5%-7 In summary then~ there has long been a need for a separating 8 means which could be inserted to supplement or partly substitute for the 9 centrifuges. The added separating means should be characterized by:
- the capacity to produce a hydrocarbon product suitable after 1l diluent removal for upgrading; and 12 - the capacity to improve the stream going on to the 13 centrifuge circuit to reduce its variations in 14 composition.
SUMMARY OF THE INVENTION
16 In accordance with the invention, diluted bituminous froth is 17 passed through an inclined plate settler, before it is treated in the 18 centrifuge circuit. The settler recovers a portion of the bitumen, 19 contained in the froth, in the form of a hydrocarbon stream which is sufficiently pure to be acceptable, after diluent removal, as a produc-t 21 for feeding directly to the upgrading circuit.
22 The settler is controlled, to cope with variations in diluted 23 bituminous froth composition and feed rate, by varying the withdrawal 24 rate of underflow in response to the hydrocarbon content of the settler overflow. More particularly, the underflow withdrawal rate is varied 26 to keep the overflow hydrocarbon content high enough that the overflow 27 is accpetable for feeding directly to the upgrading circuit. Stated 28 otherwise, the settler is operated at a cut intensity within the range of 29 product withdrawal rates that give product of the desired quality.
~ 7 ~3~
1 The invention is characterized by a number of advantages:
2 (1) A machine fr~ee of moving parts and which works on the 3 principle of gravity separation has surprisinyly been 4 discovered to:yield a product comparable in q~ality to that produced by machines operating with the mechanism ~ of powerful centrifugal separation;
7 (2) The settler yields a bitumen-containing underflow 8 product which surprisingly has only limited variations 9 in composition and which thus provides a much improved feed for the centrifuge circuit;
11 (3) And part of the cleaning/separating circuit for the 12 diluted bituminous froth now takes the ~orm of a settler 3 which is substantially free of wear and maintenance 14 problems.
Broadly stated, the ;nvention is a process for treating diluted 16 bituminous froth from the hot water process, which comprises passing the 17 froth through an inclined plate settler to produce overflow and underflow 18 streams and varying the underflow withdrawal rate from the settler in 19 response to the hydrocarbon content of the overflow:from the settler to maintain said overflow hydrocarbon content sufficiently high whereby it 21 may be fed directly to an upgrading circuit.
Figure 1 is a schematic flowsheet showing in operating 24 sequence a source of diluted bitumen froth, an inclined plate settler, and a centrifuge circuiti 26 Figure 2 is a triangular plot showing the variation in 27 composition of diluted bitumen froth~ as experienced in applicant's 28 commercial plant; and ~ 8~
1 Figure 3 is a plot showing ~ oil recovery versus product quality 2 for an inclined plate settler incorporated into a circuit in accordance 3 with the present invention.
4 DESCRIPTION OF THE P~EFERRED EMBODIMENT
A circuit in accordance with the invention is shown in 6 Figure 1. This circuit was used in developing the present invention.
7 The circuit comprised a conventional source 1 of diluted 8 bituminous froth. More particularly, the source 1 included a froth storage 9 tank 2 which received bituminous froth from a hot water process plant (not shown). A source 3 of light hydrocarbon diluent, preferably naphtha, 11 was also provided. The froth from the storage tank 2 was fed via line 12 4 and pump 5 to a diluent froth mixer 6. Naphtha was also fed, via line 13 7, into the mixer 6. A stream of diluted bitumlnous froth issued from 14 mixer 6 and was fed via line 8 into an inclined plate settler 9. Over-flow and underflow streams from the settler 9 issued through lines 10, 11 16 respectively. A pump 12 controlled the withdrawal rate through underflow 17 line 1l.
18 Typically, the diluted bituminous froth produced by the source 1 19 has a naphtha/bitumen ratio of about 0.6 to 0.8. The froth composition commonly falls within the enclosed area shown in Figure 2.
21 The inclined plate settler 9 used by applicant in the course 22 of developing the present invention was a Model LGS 2500/45 unit available 23 from Axel Johnson Inc. of Montreal. The settler parameters were as 24 folloWS:
Dimensions: height 4.6 m 26 length 6.0 m 27 width 3.7 m 28 Type of plates: flat 29 Effective plate surface area: 350 m2 31 Plate angle: 45G.
67~
1 The plates ~ere adjustable to a limited extent - their spacing 2 could be varied between 3.2 and 5.0 cms.
3 Applicant inserted the test settler 9 in its plant circuit 4 immediately before its conventional centrifuge circuit (not shown), fed diluted froth to the settler, and passed the settler underflow on to the 6 plant~s centrifuge circuit.
7 In the course of testing the inclined plate settler 9 in this8 operation, applicants found that, i~ the settler was controlled by monitoring 9 the settler overhead stream hydrocarbon content and varying the settler underflow withdrawal rate in response thereto, one could maintain the 1l purity of the overflow stream at a value in the order of about 95%. More 12 particularly, the underflow withdrawal rate was controlled by varying the3 speed of underflow pump 12~ in response to periodic composition analyses 4 of the overflow stream. Table I sets forth a comparison of the composition of a typical settler overflow product with a typical disc centrifuge pro-16 duct previously obtained with no settler in the line:
18 Component (wt%) Disc Centrifuge IPS
19 Hydrocarbon 94.7 95.3 Solids 0.8 0.8 21 Water 4.5 3.9 22 When the settler 9 was operated to produce an overhead product 23 with a purity in accordance with Table I, it w~s found that about 75%
24 to 85% of the hydrocarbon contained in the diluted froth could be recovered as overhead product.
26 In summary then, about 85% of the contained hydrocarbon in the 27 diluted froth can be recovered as settler product having a purity in the 28 order of about 95% hydrocarbon. This is supported by the data displayed 29 in Figure 3.
7~
I
1 It was also shown, when the settler 9 was tested, that the 2 underflow product had a relatively constant composition. This provided 3 a feed for the centrifuge circuit which was much easier to cope with than 4 diluted froth. This is supported by the following typical data obtained during testing of the settler in the circuit:
6 _un A
7 feed 74% hydrocarbon 8 20% water 9 6% solids hydrocarbon re-11 covered from 12 settler 85%
13 ratio of hydro-14 carbon/solids +
water in the under-16 flow 0.50 17 Run B
18 feed 66% hydrocarbon 19 28% water 6% solids 21 hydrocarbon re 22 covered from 23 settler 85%
24 ratio of hydro-carbon/solids +
26 water in the under-27 flow ~
g ~l2~:i7~360 SUPPL_N NTARY DISCLOSURE
It can be advantageous to operate the separation process with the feed froth at an elevated temperature. By operating at a higher temperature, the viscosity o-f the hydrocarbon is reduced. This allows the solid particles to settle more rapidly. In addition, at higher temperature, the water droplets coalesce more readily, which facilitates their separation from the hydrocarbon. A higher purity produ~ct can be produced ~ith lower residence time.
At higher temperatures, fractions of the diluent can approach or exceed their atmospheric boiling point. To prevent flashing of the diluent and to contain the pressures generated, it is then necessary to operate the circuit at elevated pressure, using a controlled back pressure valve in the vent line from the settler.
In accordance with this aspect of the invention then, the cixcuit is made pressure~retaining using conventional means and the process is operated at elevated temperature and pressure.
- 9a -
18 This combined froth produce is not acceptable yet For processing 19 in the upgrading circuit. The water and solids associated with the froth, partially in an emulsified form, must be removed to produce a hydrocarbon 21 product which, after diluent removalJ is suitable for upgrading. Such a 22 product preferably is one containing at least 95% by weight hydrocarbon.
23 The cleaning of the combined froth product is conventionally 24 accomplished by a process referred to as 'dilution centrifuging'.
Dilution centrifuging involves first adding naphtha to the 26 combined froth product. This is done to give a less viscous hydrocarbon 27 phase and to increase the density difference between the hydrocarbon phase 28 and the water and solids phases. The resulting 'diluted froth' is now 29 amenable to treatment in centrifuges to e-ffect separation of ~he bitumen from the water and solids.
6() 1 The commercially practised centrifuging process is carried 2 out in a two step operation. More particularly, the diluted froth is 3 first fed to a scroll-type centrifuge, which is adapted to remove the coarse 4 solids from the feedstock. The hydrocarban~rich product from the scroll centrifuge is then passed to a disc-type centrifuge, to separate the 6 hydrocarbon from the remaining water and fine solids.
7 While the two stage centrifuging circuit has been used for 8 years in the two plants in operation, there are a good many problems 9 associated with it.
For example, one problem has to do with the fact that the 1l composition of the diluted froth can vary quite widely, as a result of 12 variations in the composition of the tar sand itself. The following 3 compositions are typical of froth compositions for 'high' and 'low' 4 quality froths that are produced in applicant's plant:
High quality Low quality 16 Hydrocarbon 80 55 17 Solids S 8 18 Water 15 37 19 Taking the case of the disc centrifuge, it has internal components7 (such as discs and nozzles) which have operating parameters 21 (such as disc spacing and size of nozzles). Once these parameters are 22 set, they cannot be changed while the machine is in operation. So once 23 the parameter design is established for the machine, it has only a narrow 24 range of froth compositions that it can handleg at normal operating speed.
To provide disc centrifuge capacity adequate to cope with the 26 variable feed, it is therefore necessary to provide an excess of machines, 27 some of which are therefore standing idle much of the time.
28 Another significant problem characterizing the centrifuge 29 circuit is its very high maintenance cost. The wear on ~he machines, gi~len the erosive nature of the mixture being processed~ is almost 31 prohibitive.
3L~ 7~36~3 1 The reason that the centrifuge circuit is in fact used is that 2 it leads to a final hydrocarbon product of the desired quality. Typically, 3 the disc centrifuge product comprises:
4 Hydrocarbon 95% by wt.
Solids 4.5%
6 Water 0.5%-7 In summary then~ there has long been a need for a separating 8 means which could be inserted to supplement or partly substitute for the 9 centrifuges. The added separating means should be characterized by:
- the capacity to produce a hydrocarbon product suitable after 1l diluent removal for upgrading; and 12 - the capacity to improve the stream going on to the 13 centrifuge circuit to reduce its variations in 14 composition.
SUMMARY OF THE INVENTION
16 In accordance with the invention, diluted bituminous froth is 17 passed through an inclined plate settler, before it is treated in the 18 centrifuge circuit. The settler recovers a portion of the bitumen, 19 contained in the froth, in the form of a hydrocarbon stream which is sufficiently pure to be acceptable, after diluent removal, as a produc-t 21 for feeding directly to the upgrading circuit.
22 The settler is controlled, to cope with variations in diluted 23 bituminous froth composition and feed rate, by varying the withdrawal 24 rate of underflow in response to the hydrocarbon content of the settler overflow. More particularly, the underflow withdrawal rate is varied 26 to keep the overflow hydrocarbon content high enough that the overflow 27 is accpetable for feeding directly to the upgrading circuit. Stated 28 otherwise, the settler is operated at a cut intensity within the range of 29 product withdrawal rates that give product of the desired quality.
~ 7 ~3~
1 The invention is characterized by a number of advantages:
2 (1) A machine fr~ee of moving parts and which works on the 3 principle of gravity separation has surprisinyly been 4 discovered to:yield a product comparable in q~ality to that produced by machines operating with the mechanism ~ of powerful centrifugal separation;
7 (2) The settler yields a bitumen-containing underflow 8 product which surprisingly has only limited variations 9 in composition and which thus provides a much improved feed for the centrifuge circuit;
11 (3) And part of the cleaning/separating circuit for the 12 diluted bituminous froth now takes the ~orm of a settler 3 which is substantially free of wear and maintenance 14 problems.
Broadly stated, the ;nvention is a process for treating diluted 16 bituminous froth from the hot water process, which comprises passing the 17 froth through an inclined plate settler to produce overflow and underflow 18 streams and varying the underflow withdrawal rate from the settler in 19 response to the hydrocarbon content of the overflow:from the settler to maintain said overflow hydrocarbon content sufficiently high whereby it 21 may be fed directly to an upgrading circuit.
Figure 1 is a schematic flowsheet showing in operating 24 sequence a source of diluted bitumen froth, an inclined plate settler, and a centrifuge circuiti 26 Figure 2 is a triangular plot showing the variation in 27 composition of diluted bitumen froth~ as experienced in applicant's 28 commercial plant; and ~ 8~
1 Figure 3 is a plot showing ~ oil recovery versus product quality 2 for an inclined plate settler incorporated into a circuit in accordance 3 with the present invention.
4 DESCRIPTION OF THE P~EFERRED EMBODIMENT
A circuit in accordance with the invention is shown in 6 Figure 1. This circuit was used in developing the present invention.
7 The circuit comprised a conventional source 1 of diluted 8 bituminous froth. More particularly, the source 1 included a froth storage 9 tank 2 which received bituminous froth from a hot water process plant (not shown). A source 3 of light hydrocarbon diluent, preferably naphtha, 11 was also provided. The froth from the storage tank 2 was fed via line 12 4 and pump 5 to a diluent froth mixer 6. Naphtha was also fed, via line 13 7, into the mixer 6. A stream of diluted bitumlnous froth issued from 14 mixer 6 and was fed via line 8 into an inclined plate settler 9. Over-flow and underflow streams from the settler 9 issued through lines 10, 11 16 respectively. A pump 12 controlled the withdrawal rate through underflow 17 line 1l.
18 Typically, the diluted bituminous froth produced by the source 1 19 has a naphtha/bitumen ratio of about 0.6 to 0.8. The froth composition commonly falls within the enclosed area shown in Figure 2.
21 The inclined plate settler 9 used by applicant in the course 22 of developing the present invention was a Model LGS 2500/45 unit available 23 from Axel Johnson Inc. of Montreal. The settler parameters were as 24 folloWS:
Dimensions: height 4.6 m 26 length 6.0 m 27 width 3.7 m 28 Type of plates: flat 29 Effective plate surface area: 350 m2 31 Plate angle: 45G.
67~
1 The plates ~ere adjustable to a limited extent - their spacing 2 could be varied between 3.2 and 5.0 cms.
3 Applicant inserted the test settler 9 in its plant circuit 4 immediately before its conventional centrifuge circuit (not shown), fed diluted froth to the settler, and passed the settler underflow on to the 6 plant~s centrifuge circuit.
7 In the course of testing the inclined plate settler 9 in this8 operation, applicants found that, i~ the settler was controlled by monitoring 9 the settler overhead stream hydrocarbon content and varying the settler underflow withdrawal rate in response thereto, one could maintain the 1l purity of the overflow stream at a value in the order of about 95%. More 12 particularly, the underflow withdrawal rate was controlled by varying the3 speed of underflow pump 12~ in response to periodic composition analyses 4 of the overflow stream. Table I sets forth a comparison of the composition of a typical settler overflow product with a typical disc centrifuge pro-16 duct previously obtained with no settler in the line:
18 Component (wt%) Disc Centrifuge IPS
19 Hydrocarbon 94.7 95.3 Solids 0.8 0.8 21 Water 4.5 3.9 22 When the settler 9 was operated to produce an overhead product 23 with a purity in accordance with Table I, it w~s found that about 75%
24 to 85% of the hydrocarbon contained in the diluted froth could be recovered as overhead product.
26 In summary then, about 85% of the contained hydrocarbon in the 27 diluted froth can be recovered as settler product having a purity in the 28 order of about 95% hydrocarbon. This is supported by the data displayed 29 in Figure 3.
7~
I
1 It was also shown, when the settler 9 was tested, that the 2 underflow product had a relatively constant composition. This provided 3 a feed for the centrifuge circuit which was much easier to cope with than 4 diluted froth. This is supported by the following typical data obtained during testing of the settler in the circuit:
6 _un A
7 feed 74% hydrocarbon 8 20% water 9 6% solids hydrocarbon re-11 covered from 12 settler 85%
13 ratio of hydro-14 carbon/solids +
water in the under-16 flow 0.50 17 Run B
18 feed 66% hydrocarbon 19 28% water 6% solids 21 hydrocarbon re 22 covered from 23 settler 85%
24 ratio of hydro-carbon/solids +
26 water in the under-27 flow ~
g ~l2~:i7~360 SUPPL_N NTARY DISCLOSURE
It can be advantageous to operate the separation process with the feed froth at an elevated temperature. By operating at a higher temperature, the viscosity o-f the hydrocarbon is reduced. This allows the solid particles to settle more rapidly. In addition, at higher temperature, the water droplets coalesce more readily, which facilitates their separation from the hydrocarbon. A higher purity produ~ct can be produced ~ith lower residence time.
At higher temperatures, fractions of the diluent can approach or exceed their atmospheric boiling point. To prevent flashing of the diluent and to contain the pressures generated, it is then necessary to operate the circuit at elevated pressure, using a controlled back pressure valve in the vent line from the settler.
In accordance with this aspect of the invention then, the cixcuit is made pressure~retaining using conventional means and the process is operated at elevated temperature and pressure.
- 9a -
Claims (3)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for treating diluted bituminous froth from the hot water process, which comprises:
passing the froth through an inclined plate settler to produce overflow and underflow streams and varying the underflow withdrawal rate from the settler in response to the hydrocarbon content of the overflow from the settler to maintain said overflow hydrocarbon content sufficiently high whereby it may be fed directly to an upgrading circuit.
passing the froth through an inclined plate settler to produce overflow and underflow streams and varying the underflow withdrawal rate from the settler in response to the hydrocarbon content of the overflow from the settler to maintain said overflow hydrocarbon content sufficiently high whereby it may be fed directly to an upgrading circuit.
2. The process as set forth in claim 1 wherein:
the overflow hydrocarbon content is maintained at about 95%
by weight.
CLAIMS SUPPORTED BY THE SUPPLEMENTARY DISCLOSURE
the overflow hydrocarbon content is maintained at about 95%
by weight.
CLAIMS SUPPORTED BY THE SUPPLEMENTARY DISCLOSURE
3. The process as set forth in claims 1 or 2 wehrein:
the froth feed is at elevated temperature and the settler is maintained at elevated pressure.
- 10a -
the froth feed is at elevated temperature and the settler is maintained at elevated pressure.
- 10a -
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000538412A CA1267860A (en) | 1987-05-29 | 1987-05-29 | Inclined plate settling of diluted bitumen froth |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000538412A CA1267860A (en) | 1987-05-29 | 1987-05-29 | Inclined plate settling of diluted bitumen froth |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1267860A true CA1267860A (en) | 1990-04-17 |
Family
ID=4135778
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000538412A Expired CA1267860A (en) | 1987-05-29 | 1987-05-29 | Inclined plate settling of diluted bitumen froth |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1267860A (en) |
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| US5223148A (en) * | 1991-11-08 | 1993-06-29 | Oslo Alberta Limited | Process for increasing the bitumen content of oil sands froth |
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| US7141162B2 (en) | 2002-09-19 | 2006-11-28 | Suncor Energy, Inc. | Bituminous froth inclined plate separator and hydrocarbon cyclone treatment process |
| US7527726B2 (en) | 2006-01-25 | 2009-05-05 | Q'max Solutions Inc. | Fluid treatment apparatus |
| US7569137B2 (en) | 2004-01-08 | 2009-08-04 | Fort Hills Energy L.P. | Process and apparatus for treating tailings |
| US7651042B2 (en) | 2005-11-09 | 2010-01-26 | Suncor Energy Inc. | Method and apparatus for creating a slurry |
| US7736501B2 (en) | 2002-09-19 | 2010-06-15 | Suncor Energy Inc. | System and process for concentrating hydrocarbons in a bitumen feed |
| US7763166B2 (en) | 2006-06-16 | 2010-07-27 | Canadian Oil Sands Limited | Relocatable countercurrent decantation system |
| US7914670B2 (en) | 2004-01-09 | 2011-03-29 | Suncor Energy Inc. | Bituminous froth inline steam injection processing |
| US8016216B2 (en) | 2005-11-09 | 2011-09-13 | Suncor Energy Inc. | Mobile oil sands mining system |
| US8168071B2 (en) | 2005-11-09 | 2012-05-01 | Suncor Energy Inc. | Process and apparatus for treating a heavy hydrocarbon feedstock |
| US8393561B2 (en) | 2005-11-09 | 2013-03-12 | Suncor Energy Inc. | Method and apparatus for creating a slurry |
| US20130140249A1 (en) * | 2010-08-17 | 2013-06-06 | Ken N. Sury | Feed delivery system for a solid-liquid separation vessel |
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| US9676684B2 (en) | 2011-03-01 | 2017-06-13 | Fort Hills Energy L.P. | Process and unit for solvent recovery from solvent diluted tailings derived from bitumen froth treatment |
| US9791170B2 (en) | 2011-03-22 | 2017-10-17 | Fort Hills Energy L.P. | Process for direct steam injection heating of oil sands slurry streams such as bitumen froth |
| US9789422B2 (en) | 2010-11-02 | 2017-10-17 | Fort Hills Energy L.P. | Apparatus and method for separating a feed material containing immiscible phases of different densities |
| US10041005B2 (en) | 2011-03-04 | 2018-08-07 | Fort Hills Energy L.P. | Process and system for solvent addition to bitumen froth |
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| US10781375B2 (en) | 2017-09-11 | 2020-09-22 | Syncrude Canada Ltd. In Trust For The Owners Of The Syncrude Project As Such Owners Exist Now And In The Future | Froth washing prior to naphtha dilution |
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-
1987
- 1987-05-29 CA CA000538412A patent/CA1267860A/en not_active Expired
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| US5223148A (en) * | 1991-11-08 | 1993-06-29 | Oslo Alberta Limited | Process for increasing the bitumen content of oil sands froth |
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| US7527726B2 (en) | 2006-01-25 | 2009-05-05 | Q'max Solutions Inc. | Fluid treatment apparatus |
| US7964101B2 (en) | 2006-01-25 | 2011-06-21 | Q'max Solutions Inc. | Fluid treatment process |
| US7763166B2 (en) | 2006-06-16 | 2010-07-27 | Canadian Oil Sands Limited | Relocatable countercurrent decantation system |
| US8968580B2 (en) | 2009-12-23 | 2015-03-03 | Suncor Energy Inc. | Apparatus and method for regulating flow through a pumpbox |
| US20130140249A1 (en) * | 2010-08-17 | 2013-06-06 | Ken N. Sury | Feed delivery system for a solid-liquid separation vessel |
| US9789422B2 (en) | 2010-11-02 | 2017-10-17 | Fort Hills Energy L.P. | Apparatus and method for separating a feed material containing immiscible phases of different densities |
| US10125325B2 (en) | 2011-02-25 | 2018-11-13 | Fort Hills Energy L.P. | Process for treating high paraffin diluted bitumen |
| US9676684B2 (en) | 2011-03-01 | 2017-06-13 | Fort Hills Energy L.P. | Process and unit for solvent recovery from solvent diluted tailings derived from bitumen froth treatment |
| US10041005B2 (en) | 2011-03-04 | 2018-08-07 | Fort Hills Energy L.P. | Process and system for solvent addition to bitumen froth |
| US10988695B2 (en) | 2011-03-04 | 2021-04-27 | Fort Hills Energy L.P. | Process and system for solvent addition to bitumen froth |
| US9791170B2 (en) | 2011-03-22 | 2017-10-17 | Fort Hills Energy L.P. | Process for direct steam injection heating of oil sands slurry streams such as bitumen froth |
| US10226717B2 (en) | 2011-04-28 | 2019-03-12 | Fort Hills Energy L.P. | Method of recovering solvent from tailings by flashing under choked flow conditions |
| US11261383B2 (en) | 2011-05-18 | 2022-03-01 | Fort Hills Energy L.P. | Enhanced temperature control of bitumen froth treatment process |
| US10781375B2 (en) | 2017-09-11 | 2020-09-22 | Syncrude Canada Ltd. In Trust For The Owners Of The Syncrude Project As Such Owners Exist Now And In The Future | Froth washing prior to naphtha dilution |
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