U.S. patent number 3,901,791 [Application Number 05/496,774] was granted by the patent office on 1975-08-26 for method for upgrading bitumen froth.
This patent grant is currently assigned to Great Canadian Oil Sands Limited. Invention is credited to Robert A. Baillie.
United States Patent |
3,901,791 |
Baillie |
August 26, 1975 |
Method for upgrading bitumen froth
Abstract
The present invention provides a procedure for removing mineral
matter and water from a primary bitumen froth recovered from tar
sands which comprises diluting the raw bitumen froth with a
hydrocarbon diluent boiling in the range of
350.degree.-750.degree.F. and thereafter settling the diluted
bitumen froth in an autoclave settling zone to provide a froth
product and a tailings product. The tailings product is thereafter
subject to centrifugal force to provide a centrifugal tailings
product and a centrifugal froth product. The centrifugal froth
product is recycled to the settler zone.
Inventors: |
Baillie; Robert A. (West
Chester, PA) |
Assignee: |
Great Canadian Oil Sands
Limited (Toronto, CA)
|
Family
ID: |
23974076 |
Appl.
No.: |
05/496,774 |
Filed: |
August 12, 1974 |
Current U.S.
Class: |
208/188; 208/390;
208/425 |
Current CPC
Class: |
C10L
1/20 (20130101); C10G 1/045 (20130101); C10G
33/06 (20130101) |
Current International
Class: |
C10G
1/00 (20060101); C10G 33/00 (20060101); C10G
1/04 (20060101); C10G 33/06 (20060101); C10L
1/10 (20060101); C10L 1/20 (20060101); C10g
033/04 () |
Field of
Search: |
;208/188,187,11 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Gantz; Delbert E.
Assistant Examiner: Crasanakis; G. J.
Attorney, Agent or Firm: Church; George L. Hess; J. Edward
Maloney; Richard P.
Claims
The invention claimed is:
1. A method for removing mineral matter and water from bituminous
froth containing bitumen, mineral matter, and water which
comprises:
a. combining a raw bituminous froth containing substantial
quantities of mineral matter and water with a hydrocarbon diluent
boiling in the range of 350.degree.-750.degree.F.;
b. heating said diluted froth from step (a) to a temperature in the
range of 300.degree.-1000.degree.F.;
c. combining said heated diluted froth with centrifugal froth
hereinafter recovered via step (f);
d. settling said combined diluted froth from step (c) in an
autoclave settling zone at a temperature in the range of
300.degree.-1000.degree.F. at a pressure in the range of 0- 1000
psig to provide an upper bitumen froth layer, a middle water layer
containing minor quantities of bitumen and mineral matter, and a
lower tailings layer comprised substantially of mineral matter with
a minor quantity of bitumen;
e. combining said lower tailings layer with a liquid hydrocarbon
diluent boiling in the range of 350.degree.-750.degree.F. and
transferring the diluted tailings to a centrifuging step;
f. centrifuging said tailings to provide a centrifugal froth which
is thereafter recycled and combined with said heated diluted froth
in step (c); and
g. recovering from the settling zone of step (d) said bitumen froth
as product having substantially reduced mineral matter and
water.
2. A method according to claim 1 wherein the ratio of said diluent
to bitumen in step (a) is in the range of 0.3:1 to 1:1.
3. A method according to claim 1 wherein the diluent to tailings
ratio of step (e) is in the range of 1 to 20 volumes of said
diluent per volume of bitumen in the tailings.
Description
BACKGROUND OF THE INVENTION
The present invention relates to an improved process for upgrading
bitumen froth such as that recovered by a hot water procedure for
recovering bitumen from tar sands. The present invention, more
particularly, relates to a method wherein the raw bituminous froth
product containing mineral matter and water is diluted with a
liquid hydrocarbon boiling in the range of
350.degree.-750.degree.F. and thereafter settled in an autoclave
settling zone whereby mineral matter and water are removed from the
bitumen froth.
Numerous deposits of bituminous tar sands exist throughout the
world. The most extensive deposits are found in Northern Alberta,
Canada. The sands are composed of a siliceous material, generally
having a size greater than that passing a 325 mesh screen,
saturated with a relatively heavy, viscous bitumen in quantities of
from 5 to 21 weight percent of the total composition. More
typically, the bitumen content of the sands is between 8 to 15
percent. This bitumen is quite viscous and contains typically 4.5
percent sulfur and 38 percent aromatics. Its specific gravity at
60.degree.F. ranges typically from about 1.00 to about 1.06. The
tar sands also contain clay and silt. Silt is defined as material
which will pass a 325 mesh screen but which is larger than 2
microns. Clay is material smaller than 2 microns including some
siliceous material of that size.
There are several well-known procedures for effecting separation of
bitumen from tar sands. One particularly effective method is that
disclosed in Canadian Pat. No. 841,581 issued May 12, 1970 to Paul
H. Floyd et al. The method of this disclosure provides that the
bituminous sands are jetted with steam and mulled with a minor
amount of hot water at a temperature in the range of
140.degree.-210.degree.F. in a conditioning drum.
An alkaline reagent can also be added to the conditioning drum
usually in amounts of from 0.1 to 3.0 lbs. per ton of tar sands.
The amount of such alkaline reagent preferably is regulated to
maintain the pH of the middlings layer in a subsequent separator
zone within the range of 7.5 to 9.0. Best results seem to be
obtained at a pH value of 8.0 to 8.5. The amount of the alkaline
reagent that needs to be added to maintain a pH value in the range
of 7.5 to 9.0 may vary from time to time as the composition of the
tar sands as obtained from the mine site varies. The best alkaline
reagents to use for this purpose are caustic soda, sodium
carbonate, or sodium silicate, although any of the other monovalent
alkaline reagents can be used if desired.
Mulling of the tar sands produces a pulp which then passes from the
conditioning drum to a screen. The purpose of the screen is to
remove from the tar sand pulp any debris, rocks, or oversized
lumps. The pulp then passes from the screen to a sump where it is
diluted with additional water including middlings recycle stream
from the separation cell. Recycling of the middlings is not
essential in all cases, particularly when the clay content of the
tar sands is high. In this event a relatively high rate of fresh
feed water is employed to compensate for the high clay content
while a correspondingly high rate of transfer of middlings layer to
a secondary scavenger zone can be maintained.
The process as above described can also include sending a minor
portion of the middlings recycle stream to the conditioning drum to
supply all or a part of the water needed therein other than that
supplied through condensation of the steam which is consumed. Also,
a stream of the middlings recycle is sometimes introduced into the
screen to flush the pulp therethrough and into the sump. As a
general rule, the total amount of water added to the natural
bituminous sands as liquid water and as steam prior to the
separation step is in the range of 0.2 to 3.0 tons per ton of the
bituminous sands. The amount of water needed within this range
increases as the silt and clay content of the bituminous sand
increases. The resulting pulp is thereafter carried into a
separation cell maintained at a temperature of about
150.degree.-200.degree.F.
In the separation cell, sand settles to the bottom as tailings and
bitumen rises to the top in the form of an oil froth which is the
primary bitumen froth product. An aqueous middlings layer
containing some mineral and bitumen is formed between these layers.
A scavenging step is normally conducted on this middlings layer in
a secondary flotation zone normally referred to as a scavenger
zone. In the scavenger zone, the feed material is aerated so as to
produce a scavenger froth product and a scavenger tailings product.
The scavenger cell froth product normally contains a substantial
amount of water and mineral matter and is thereafter treated in
accordance with the procedure disclosed in Canadian Pat. No.
857,306 issued Dec. 1, 1970 to Ernest W. Dobson. This method
comprises passing the scavenger froth to a settling zone wherein a
froth product rises to the surface and the mineral matter within
the froth product settles to the bottom of the settler zone. The
froth product from this settling zone is thereafter combined with
the froth product from the heretofore disclosed primary separation
zone and subsequently combined with a diluent to provide a
bituminous froth product suitable for further treatment prior to
upgrading to synthetic petroleum crude.
The raw bitumen froth normally suitable for use in the process of
this invention can be described as a raw bitumen froth which
normally comprises 20 to 45 percent and more typically 30 percent
water, 2.0 to 6.0 and more typically 3.0 to 5.0 percent mineral and
the remainder being principally hydrocarbons. The raw bituminous
froth containing these high concentrations of mineral matter and
water is not suitable for typical refinery processing and,
therefore, must be further upgraded to reduce mineral matter and
water to substantially low concentrations. In the process of the
present invention, this end is accomplished in an economic and
efficient manner.
Heretofore this froth product recovered as a combination of the
primary separation zone froth and the settled scavenger zone froth
has been diluted with a hydrocarbon diluent and then upgraded by
centrifuging to reduce the amount of mineral in the centrifuged
bitumen product to about 1 to 2 weight percent. Generally, the
weight ratio of diluent to bitumen (D/B) in the combined froths
lies within the range of between 0.3 to 1.0. When the bitumen is
later coked to produce synthetic crude, the minerals are
concentrated to about 6 to 8 weight percent in the coke. This
quantity of mineral matter is generally undesirable and renders the
coke product somewhat difficult to recover. In commercial
operation, this coke is burned to provide power. When the coke is
burned in boilers, the contained minerals or ash must be removed to
keep the boiler tubes from fouling. Excessive quantities of
minerals reduce operational ability and require expensive
maintenance and air pollution control equipment. The combined froth
products also contain from 20 to 45 percent water which must be
removed prior to the coking procedure.
One procedure for upgrading froth is disclosed in U.S. Pat. No.
3,607,721 issued Sept. 21, 1971. By this procedure, raw bituminous
froth is diluted with a light hydrocarbon diluent such as coker
naphtha and settled in a settling vessel. The sludge recovered as
tailings from the settler is thereafter treated in a centrifuge to
recover additional bitumen. Unfortunately, use of a light
hydrocarbon diluent often leads to unreasonable losses of diluent
to waste water streams which makes the process economically less
attractive.
Heretofore, efficient and economical procedures which provide high
volume production of substantially mineral and water-free bitumen
froth from crude or raw bitumen froth have been overlooked. By way
of the present invention, a new procedure for recovering a
substantially water and mineral-free bitumen froth product from a
raw bitumen froth product produced by a hot water separation
procedure for recovering bitumen from tar sands is provided.
DESCRIPTION OF THE INVENTION
By the method of the present invention, raw bituminous froth is
first diluted with a liquid hydrocarbon boiling in the range of
350.degree.-750.degree.F. and thereafter transferred to an
autoclave settling zone wherein the diluted froth, in combination
with a recycle centrifugal froth hereinafter described, is settled
to provide an upper froth layer, a water layer, and a lower mineral
tailings layer. The tailings layer is thereafter withdrawn from the
autoclave settling zone, diluted with diluent similar to that added
to the raw bitumen froth, and thereafter transferred to a
centrifuge which is preferably a scroll centrifuge wherein a
centrifugal froth product is recovered and recycled to the
autoclave settling zone. By this process, a froth product
substantially reduced in mineral matter and water and thereby
suitable for further refining with well-known petroleum refining
techniques is provided.
A distinct advantage of the present method lies in the dilution of
the settler tailings with added hydrocarbon diluent. By this
procedure, diluent can be added to the tailings prior to the
centrifuge step in ratios of 1 to 1 to as high as 20 to 1 diluent
to bitumen by weight. This high ratio of diluent to bitumen
provides more efficient recovery of bitumen from this stream. The
addition of diluent to the settler tailings stream provides a
method whereby the diluent is most effective in recovery of bitumen
from minerals. By this method, the amount of diluent added to the
froth prior to the settling step can be reduced. The diluent not
added to the froth fed to the settler can be added to the tailings
from the settler where it is more effective in freeing bitumen from
minerals. Thus, the overall quantity of bitumen losses in the
tailings is appreciably reduced.
In order to more completely define the method of the present
invention, the following description is presented. Referring to the
drawing, raw bituminous froth of the type normally recovered from
hot water extraction techniques, hereinabove disclosed and
described, is transferred via line 11 and combined in line 13 with
hydrocarbon diluent boiling in the range of
350.degree.-750.degree.F. received from line 12. The diluent added
to the froth at this step can be in the range of 0.3 to 1.0 volume
of diluent per volume of froth. In this example, 0.5 volume of
diluent per volume of bitumen is used. The diluted bitumen froth is
thereafter heated to a temperature in the range of
300.degree.-1000.degree.F. by way of heat exchanger 14 and
thereafter transferred to line 15 where it is combined with a
centrifugal froth product hereinafter described. From line 15, the
combined froth is transferred to autoclave settling zone 16 which
can be defined as an autoclave-type pressure vessel having heat
exchange means such as a steam jacket or other means. The froth
product is settled in this zone at a temperature in the range of
300.degree.-1000.degree.F. and a pressure in the range of 0 to 1000
psig to provide an upper froth layer comprised substantially of
bituminous froth, a middle layer comprised substantially of water
containing minor amounts of mineral matter and bitumen, and a lower
tailings layer comprised substantially of mineral matter and
containing minor quantities of bitumen. The refined froth product
is recovered via line 17 from autoclave 16 which product is a froth
substantially reduced in mineral matter and water and suitable for
further petroleum refining. Water is removed from autoclave
settling zone 16 via line 18. This water can thereafter be recycled
to other areas where fresh water is required or can be discarded.
The tailings from autoclave settling zone 16 are withdrawn via line
19 and combined in line 21 with five volumes of liquid hydrocarbon
diluent boiling within the range of 350.degree.-750.degree.F. per
volume of bitumen in the tailings from line line 20. The diluted
tailings are thereafter transferred to scroll centrifuge 22 wherein
a centrifugal froth product is recovered via line 24 and recycled
to line 15 where it is combined with the raw diluted bitumen froth.
A tailings stream is withdrawn from scroll centrifuge 22 via line
23 and discarded.
Typically, the bituminous froth product recovered from autoclave
settling zone 16 can be characterized as containing at least 96
percent hydrocarbon and no more than 0.5 percent mineral matter and
3.5 percent water. The advantages of this froth refining technique
are particularly realized by greater volume throughput of froth as
well as improved quality of the bitumen froth product as compared
to other known techniques. Equally important is the fact that
substantial benefits and economics are realized by low maintenance
and low capital investment resulting from use of the bitumen froth
process of the herein disclosed invention. A particularly suitable
advantage of the present invention is the use of the higher boiling
liquid hydrocarbon diluent which provides greater viscosity
reduction to the froth and further provides efficient settling of
the froth at elevated temperatures, an advantage heretofore not
disclosed in the art. This greater viscosity reduction comes about
because at constant pressure, a higher temperature can be employed
with a higher boiling diluent than with a lower boiling diluent.
The higher the temperature to which the diluent-bitumen mixture is
heated, the lower its viscosity.
Thus, one embodiment of the present invention comprises a method
wherein a bituminous froth product is substantially improved by
removal of mineral matter and water comprising the steps of:
a. combining a raw bitumen froth product containing substantial
quantities of mineral matter and water with a hydrocarbon diluent
boiling in the range of 350.degree.-750.degree.F.;
b. thereafter heating said diluted froth to a temperature in the
range of 300.degree.-1000.degree.F.;
c. combining said heated diluted froth product with centrifugal
froth herinafter recovered via step f;
d. settling said combined diluted froths in an autoclave settling
zone at a temperature in the range of 300.degree.-1000.degree.F. at
a pressure in the range of 0- 1000 psig to provide an upper bitumen
froth layer, a middle water layer containing minor quantities of
bitumen and mineral matter, and a lower tailings layer comprised
substantially of mineral matter with minor quantities of
bitumen;
e. transferring the tailings layer to centrifuging step;
f. centrifuging said tailings in a centrifuge to provide a
centrifugal froth product which is thereafter recycled and combined
with said diluted froth feed; and
g. recovering from the settling zone a froth product having
substantially reduced mineral matter and water.
The liquid hydrocarbon diluent suitable for use in the method of
the present invention can generally be defined as a petroleum
naphtha containing aromatics, saturates, and olefins boiling in the
range of 350.degree.-750.degree.F.
* * * * *