U.S. patent number 3,875,046 [Application Number 05/459,268] was granted by the patent office on 1975-04-01 for recovery of oil from tar sand by an improved extraction process.
Invention is credited to William J. Rosenbloom.
United States Patent |
3,875,046 |
Rosenbloom |
April 1, 1975 |
RECOVERY OF OIL FROM TAR SAND BY AN IMPROVED EXTRACTION PROCESS
Abstract
An improved process for extracting oil from tar sand containing
fines using extraction and phase separation techniques. A
closed-cycle, single-stage process uses only one extraction vessel
in which tar sand is contacted by an extractant, such as water
containing a wetting agent and/or a solvent, and recycle water in a
fluidized bed condition which avoids disturbing fines attached to
the tar sand particles. Fines exiting the extraction vessel in a
water phase are agglomerated and reintroduced to the bottom of the
extraction vessel where they are filtered out by the extracted sand
passing downward in the vessel. The solvent may be vaporized to
enhance contact and assure complete recovery. Steam is
advantageously introduced to the extraction vessel to scour the
sand particles free of solvent. The usual process control additives
may be included in the recycle water. The sand and fines tailings
are essentially free of pollutants.
Inventors: |
Rosenbloom; William J.
(Westport, CT) |
Family
ID: |
23824086 |
Appl.
No.: |
05/459,268 |
Filed: |
April 9, 1974 |
Current U.S.
Class: |
208/391; 208/432;
208/426 |
Current CPC
Class: |
C10G
1/047 (20130101) |
Current International
Class: |
C10G
1/00 (20060101); C10G 1/04 (20060101); C10g
001/04 () |
Field of
Search: |
;208/11 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Davis; C.
Attorney, Agent or Firm: Noe; Alphonse R.
Claims
I claim:
1. In a process for recovering oil from tar sand by extraction and
phase separation, the improvement of a closed-cycle process
comprising:
introducing the tar sand to a single-stage extraction vessel,
flowing a liquid extraction stream including water countercurrent
to the tar sand to maintain it in a fluidized bed condition,
separating an oil phase above the tar sand fluidized bed,
separating a water phase above the tar sand but below the oil
phase,
withdrawing a water stream from the water phase in the extraction
vessel,
recycling the water stream to the extraction vessel at a point
below the top of the tar sand fluidized bed,
withdrawing the spent sand from the extraction vessel, and
withdrawing an oil stream from the oil phase in the extraction
vessel.
2. The improved process as claimed in claim 1, further
including:
introducing steam to the extraction vessel at a point below the
fluidized bed, and
steam scouring the sand particles to remove therefrom essentially
all extraction stream constituents except inert solids.
3. The improved process as claimed in claim 1, wherein the tar sand
is introduced into the reaction vessel at a point below the oil
phase.
4. The improved process as claimed in claim 1, wherein the tar sand
contains fines and the process further includes:
maintaining the fluidized bed condition of the tar sand such that
effective tar sand-liquid extraction stream contact is provided and
the sand is sufficiently suspended to act as a filter media for
agglomerated fines, but insufficiently active to dislodge any fines
which may be attached to the sand particles,
collecting the unattached fines in the separated water phase,
withdrawing the fines in the water phase along with the water
stream,
recycling the water-fines stream to the vessel through introduction
thereto at a point below the top of the fluidized bed,
removing the fines in the water-fines recycle stream by passing the
stream through the sand in the fluidized bed condition to filter
them,
withdrawing the sand and filtered fines from the vessel, and
withdrawing an oil stream, from the oil phase, with reduced content
of contaminants such as fines.
5. The improved process as claimed in claim 1, wherein the liquid
extraction stream includes dissolved oil extraction control agents
selected from the group consisting of wetting agents and dispersing
agents.
6. The improved process as claimed in claim 1, wherein the liquid
extraction stream includes solvent which is fed to the extraction
vessel at a point near the bottom of the fluidized bed and an
oil-solvent phase is separated above the fluidized bed.
7. The improved process as claimed in claim 4 further
including:
passing the withdrawn water-fines stream to a storage and treatment
vessel, and
agglomerating the fines in the water-fines stream within the
storage and treatment vessel prior to recycling the stream of the
extraction vessel.
8. The improved process as claimed in claim 1 further
including:
feeding a solvent to the extraction vessel at a point near the
bottom of the fluidized bed,
vaporizing the solvent within the extraction vessel, and
separating an oil-solvent phase above the fluidized bed.
9. The improved process as claimed in claim 7, further including
back washing the sand and fines withdrawn from the extraction
vessel prior to dumping the same as tailings in order to assure
that they are pollutant-free.
10. The improved process as claimed in claim 4, further including
mixing the tar sand with hot water prior to introduction into the
extraction vessel, the mixing to be sufficiently gentle to assure
that any fines attached to the sand particles are not dislodged
therefrom.
11. A closed cycle process for recovering oil from tar sand by
extraction and phase separation comprising:
introducing the tar sand to a single stage extraction vessel;
flowing a liquid extraction stream countercurrent to the tar sand
to maintain it in a fluidized bed condition;
separating an oil phase above the tar sand fluidized bed;
withdrawing an oil stream from the oil phase in the extraction
vessel; and
withdrawing spent sand from the extraction vessel.
Description
BACKGROUND OF THE INVENTION
1. Field of the Invention
This invention relates to the extraction of oil from
bituminous-containing sands. More particularly, this invention
relates to a method of removing oil from tar sands by an improved
extraction process carried out in a closed cycle system to yield an
oil phase containing a reduced amount of contaminants without the
need for excessive process water requirements, high extractant
losses and discharge of polluted waste streams.
Tar sands, also known as bituminous sands and oil sands, are
primarily aggregates of sand, clay, oil and water capable of being
surface mined. There are large known reserves of heavy petroleum
locked up in tar sand deposits in various parts of the world, the
best known of which is the Athabasca Tar Sands in Alberta, Canada,
which has estimated recoverable reserves in excess of 250 billion
barrels of oil. The significance of this quantity is apparent from
the fact that the proven world-wide oil reserves as of early 1973
were 667 billion barrels. Currently, increasing world dependence
upon petroleum for energy and for the manufacture of
petroleum-based products coupled with a diminishing supply of
petroleum suggests that the tremendous tar sand deposits of oil be
exploited provided that suitable processing methods are
available.
The tar or bitumen content of tar sand varies from natural deposit
to natural deposit and contains 5 to 20 percent heavy oil, by
weight. On the average this constitutes about one barrel of oil per
2 tons of sand. In addition to the sand component of the mineral,
there are usually fine particles of clay and silt the quantity of
which also varies and can range from 1 to 50 percent, by weight.
Tar sand may also contain 1 to 10 percent, by weight, water in the
form of a film around the sand grains. Prior to being useful in
ordinary oil refining processes, the petroleum must be separated
from the tar sand and various procedures for accomplishing this
have been suggested.
2. Description of the Prior Art
Among the best known prior art methods for separating the oil from
the sand are those utilizing water extraction processes and known
as the "hot water method" and the "cold water method." In the hot
water method, the tar sand is treated with steam and thoroughly
mulled and aerated in large rotating drums with a minimal amount of
hot water at a controlled temperature. The pulp is then dropped
into a turbulent stream of circulating hot water and carried to a
separation cell. In the separation cell, sand settles to the
bottom, oil rises to the top in the form of a frothy mixture of
minerals and oil and an aqueous middlings layer comprising clay and
silt is formed between the sand and the frothy layer.
Cold water processes have involved adding a hydrocarbon diluent,
such as kerosene, soda ash and a wetting agent to the tar sand
followed by charging the mixture to a ball mill for mixing and
grinding. The mixture is then mixed with large amounts of water in
a settling zone. Most of the sand settles out and a frothy
bituminous emulsion is floated to the top in a manner similar to
the hot water method. Other cold water processes involve the use of
agitation followed by classification and thickening to encourage
settling of the sand. Still other processes involve shearing in
water in a through-type kneader.
The water extraction processes possess several serious
disadvantages. In particular, tar sand having a high clay and silt
content results in poor oil separation and larger amounts of the
oil remain with the middlings layer. Consequently, a scavenger step
is required for further treatment of the middlings layer to recover
this unseparated oil. See, for example, U.S. Pat. No. 3,401,110.
Such a process also requires considerable slurry pumping and
handling with the result that the abrasiveness of the sand takes a
heavy toll on material handling equipment. The greater the clay and
silt fines content, the greater also the process water required.
The amount of water thus required is related to the fines content
and may run as high as 150 to 250 gallons per ton of tar sand
processed when 30 percent of the mineral is below 44 microns in
size, a size below which fines are the greatest contaminant
problem. Not only does such an amount of water represent large
process water requirements, but, in addition, loss of heated water
results in large heat losses as well as disposal problems.
In the attempt to overcome some of aforementioned drawbacks there
have been proposed ion exchange systems to reduce fresh water
requirements, U.S. Pat. No. 3,496,093, as well as techniques for
desirably determining accurate water process requirements based on
sand aluminum content, U.S. Pat. No. 3,558,469. The use of a
flocculation zone following a sand separation zone subsequent to
the scavenger zone in the hot water process in order to remove
fines from the water stream has also been suggested. See U.S. Pat.
No. 3,487,003. However, the aforementioned processes do not reduce
the simplicity of the process or equipment required but rather
either add another process step or require the use of chemical
additives with a concomitant increase in complexity of handling
requirements and cost.
Cold water methods may be essentially solvent extraction processes
in which the tar sands are mixed with a hydrocarbon solvent slurry
followed by removal of the fat solvent by filtration, centrifuging
or other similar means. The main objections of this approach
include the hazards involved in the slurrying of the tar sand with
hydrocarbon solvent as well as the loss of solvent with the sand
tailings, thus making the process uneconomical. As an aid to
separation of the water from the bituminous emulsion in the water
extraction processes, the use of chelating agents, U.S. Pat. No.
3,522,168, as well as the adjustment of the pH of the aqueous
phase, U.S. Pat. No. 3,542,666, have been suggested. Control of
viscosity conditions has also been suggested as an aid to
separation. See U.S. Pat. No. 3,399,765. Controlled velocity to
separate bitumen from bituminous sand in a dense slurry has also
been proposed. See U.S. Pat. No. 3,556,981.
Other prior art extraction processes utilize primarily a
hydrocarbon solvent to extract the oil from bituminous sands. See,
for example, U.S. Pat. No. 3,553,099. In such processes tar
recovery is good; however, solvent losses constitute a serious
drawback because of the high cost of solvent. Since a high quantity
of sand must be processed in order to recover relatively small
quantities of oil, even a small percentage of solvent in the sand
tailings cannot be tolerated as a loss since the overall amount
will be great relative to the oil recovered. As a consequence,
multi-stage recovery equipment and processes utilizing filtration
or centrifugal separation have been proposed, as for example in
U.S. Pat. No. 3,553,099. While solvent recovery may be enhanced in
such systems, the capital cost of equipment as well as operating
costs tend to be high. Alternatively, special treatment involving
control of viscosity and differential velocity and utilizing high
volumes of water to minimize solvent loss have been proposed. See
U.S. Pat. No. 3,553,098.
Thus, it can be seen that many and diverse methods for separating
the oil from bituminous sands by fluid extraction followed by
separation have been proposed. Thus, there have resulted various
proposed methods including hot water flotation, gravity separation,
cold water flotation, centrifugal separation, solvent extraction
and various combinations thereof. However, a serious drawback has
remained in that the hydrocarbon product recovered by these
processes, that is, the oil or bitumen and sometimes solvent,
commonly contains, after the initial separation from the bullk of
the sand, significant amounts of water, mineral matter, and
sometimes air or gas in an emulsion or froth. In addition, process
requirements of important resources such as water are high and
losses of expensive solvents cannot be economically tolerated. A
further disadvantage of the prior art processes is the fact that
waste streams from these processes frequently contain pollutants
that give rise to serious environmental concerns. Yet, the
economical elimination of such contaminants must be achieved if a
process is to be commercially exploited.
SUMMARY OF THE INVENTION
The present invention overcomes many of the disadvantages
associated with the prior art processes and provides an efficient
and relatively economical process yielding oil containing reduced
amounts of contaminants from tar sand. Thus, prior art drawbacks
involving material handling problems due to pumping of erosive sand
slurries, high mineral contamination of separated oil, hazards in
solvent handling, loss of solvents, high requirements of process
water, high heat requirements and disposal problems due to polluted
effluents, are overcome by the process of my invention which
provides a closed-cycle single-stage system that offers the
advantages of the hot water and solvent extraction processes while
at the same time remaining physically and economically
attractive.
My invention is an improvement on both the water and the solvent
extraction type processes and overcomes the disadvantages of the
prior art by providing a closed-cycle, single-stage extraction
process requiring no reprocessing and repumping of the tar sand for
high extraction recovery. In addition, the heat requirements of the
process of my invention are minimal because the sand and fines
tailings are discharged at essentially the same temperature as the
incoming tar sand and the liquid media remains within the system
and is recycled rather than discharged. Thus, the hazards of
solvent handling are minimized, solvent losses are negligible and
pollution reduced.
The process according to my invention involves the following steps.
Tar sand is pretreated with hot water from a process recycle
stream, described below, to make it sufficiently free flowing for
removal of oversized material. The mixing of the tar sand with hot
water should be sufficiently gentle to avoid disruption of the
clays attached to the sand particles. The tar sand is then fed into
the top of an extraction vessel designed so as to allow adequate
contact time between the rising extraction liquid medium and the
slowly down-flowing solid sand bed. The extraction may be hot
water, containing a wetting or dispersing agent facilitating the
extraction of oil from the sand, if desired, or solvent may be
introduced into the lower section of the down-flowing sand bed.
With the up-flowing extraction liquid, the system functions as a
countercurrent extraction system minimizing extractant, water or
solvent, use to that required for viscosity control of the oil. The
point of tar sand feed to the top of extraction is to a level at
least below the collected solvent-oil layer.
The rate of flow of the liquid medium in the extraction vessel
should be adjusted to maintain the sand particles in a fluidized
form but also sufficiently gentle to prevent the disruption of the
clays attached to the sand particles. This rate of liquid flow also
allows flocculated fines to be filtered out by the sand bed prior
to discharge, as described below. Steam is also introduced into the
bottom of the extraction vessel, either directly or indirectly, in
order to heat any remaining solvent occluding on the sand to
vaporize it. Solvent vapors condense on the cooler down-falling
oil-rich sand above it. This vaporization of the solvent provides
quicker and more complete dissolution of the tar on the sand and
assures complete removal of solvent from the discharging sand. A
recycle stream of water is also introduced at the bottom of the
extractor.
The oil-solvent layer collects at the top of the extraction vessel
and is there withdrawn. Below this layer is a layer of water and
fines which is recycled first to a water storage and treatment
vessel and then to the bottom of the extraction process. In the
recirculating water system there may be incorporated, in addition
to the storage and treatment tank, means for adding treatment
chemicals for pH control, wetting agents, dispersing agents, and
flocculants for agglomerating the fine particles. The system also
permits the addition of salts, such as sodium chloride, for
increasing the gravity if it is advantageous to increase the
buoyancy of the oil.
The spent sands and the flocculated fines are removed from the
extractor by a suitable drag conveyor such as a screw conveyor. In
addition, the hot water contained in the sand may be replaced by
cold make-up water introduced countercurrent to the sand flow to
assure removal of soluble chemicals and the inert solids can be
dumped. Alternatively, if it is advantageous to dispose of the sand
as a slurry, means may be provided for pumping instead of drag
removal of the sand.
Accordingly, it is a feature of my invention to provide a process
for the solvent extraction of oil from tar sand in a single-stage,
closed-cycle process which essentially eliminates extractant loss
and minimizes sand slurry pumping requirements.
It is a further feature of my invention to provide an improved
process for extracting oil from tar sand by utilizing an
extractant, such as a solvent, which is essentially recovered in
the process.
A still further feature of my invention is the provision of a tar
sand extraction process which results in removal of chemicals in
sand tailings and in the absence of polluted effluent waste
streams.
Another feature of this invention is the provision of a tar sand
extraction and recovery process which results in the production of
a hydrocarbon product free of significant amounts of contaminants
such as sand silt and other mineral matter.
The foregoing features and other features of this invention will
become apparent from the following description of a preferred
embodiment thereof.
BRIEF DESCRIPTION OF THE DRAWING
The drawing shows a schematic representation of a suitable process
flow arrangement for carrying out a preferred embodiment of the
process of my invention. The illustration represents conventional
process equipment that is known to the art and readily commercially
available. For simplicity, details, such as pumps and valves, have
not been shown although it is understood that those skilled in the
art will be able to supply the necessary equipment to carry out the
process functions taught herein. The legends on the drawing aid in
understanding thereof and characterize the process steps.
DESCRIPTION OF THE PREFERRED EMBODIMENT
The process of my invention is best understood by reference to the
drawings. Tar sand is fed into the processing system, shown at 10,
into a mixer 14 which may be of the simple low energy type such as
a rotary cement mixer. Hot water from the water recycle system is
also fed into the mixer through a line 12. Sufficient hot water,
plus steam if needed, is added to form a fluid slurry. The
temperature within the mixer is preferably maintained at the lowest
possible temperature for suitable fluidity. Within the mixer 14
gentle mixing to prevent disruption of the clays and other fines
attached to the sand particles takes place. That the mixing be
sufficiently gentle to avoid displacement of the fines is important
in my process and is in distinction from previously known processes
which deliberately mull, aerate or grind the tar sand. The tar
sand-water slurry flows from the mixer 14 to a screen 18 via the
line 16. On the screen 18 over-size material may be removed and
discarded via a conveyor 20. It is also important that this
screening not disrupt the clays and other fines attached to the
sand particles. The screened slurry is then fed through a line 22
to the top of the extractor vessel 24. Within the extraction vessel
an internal downcomer 26 assures that the tar sand-water slurry is
fed to a level below the oil-solvent collection layer (hydrocarbon
phase) and preferably to a point below the water-contaminants
layer.
The extraction liquid, or extractant, may be hot water, or it may
be water to which has been added wetting agent, dispersing agent
and the like in order to facilitate extraction of the oil. Also,
solvent of the type customarily used in such extraction processes
may desirably be introduced to the extraction vessel 24 via a line
28 at a point near the lower portion of the extraction vessel.
Steam is also introduced, indirectly or directly, into the
extraction vessel 24 at a point near the bottom of the vessel via a
line 30 which is located below the point of introduction of the
solvent. After start up, once the process has reached steady-state
operation, there exists a recycle stream containing water and
contaminants such as clay and other fines from the extraction
process. This recycle stream may also contain slight amounts of
additives, such as wetting agents, dispersing agents, flocculants,
and caustic for pH control, used for process control. This recycle
stream is introduced to the extraction vessel 24 at a point below
the points of introduction of the solvent and steam through a line
32.
The extraction process within the extraction vessel operates as
follows: The up-flowing extractant liquid, including the recycled
water, adjusted for the most suitable pH and containing wetting or
dispersing agents, and dissolved salts, if necessary, for increased
density, and solvent acts to release the tar or heavy oil from the
sand and cause it to rise to an upper oil-solvent liquid layer in
the extraction vessel. This hydrocarbon phase is shown
schematically and referenced by the numeral 100. Since the
extraction is countercurrent, the tar sand becomes more depleted in
oil as it continues in its downward path in the extraction vessel
while becoming exposed to leaner solvent and solvent vapor until
practically all oil is removed and the sand is wetted with the
solvent only.
As the sand continues its downward path in the extraction vessel 24
below the point of solvent introduction via the line 28, it is
heated by steam introduced via the line 30. The heating by steam
may be accomplished directly or indirectly; however, the
introduction of live steam is preferred because it allows for the
use of induction nozzles which provide an intimate mix with the
sand particles. The steam scours the remaining solvent and other
chemcials off of the sand particles and the amount of steam
necessary to accomplish this is used. Should this scouring be
insufficient to remove all solvent, additional steam is added until
the sand temperature is above the boiling point temperature of the
solvent, which has a boiling point temperature lower than the
boiling point temperature of the circulated liquid, in order to
vaporize the solvent.
The solvent vapor rises with the flowing liquid and condenses on
the cooler down-coming sand. The oil-solvent phase constitutes the
uppermost layer in the extraction vessel and is removed as a
relatively clean hydrocarbon phase containing a reduced amount of
contaminants via the line 34. This hydrocarbon phase may then be
further refined, if desired, and separated into a solvent fraction
and a product tar fraction for a refinery feed. The solvent
fraction from such further refining may then be reintroduced to the
system as make-up solvent entering via the line 28. The water phase
containing fines such as silt and clay and other contaminants in
addition to additives is an intermediate layer, shown at 200,
between the oil-solvent phase and the sand extraction zone. This
phase, which may also contain some dispersed hydrocarbon, is
removed via a line 36 to a storage and treatment tank 38.
In the storage and treatment tank 38 this recycle material is
sampled and its pH, wetting agent and salt content, and
flocculating agent composition adjusted, if needed. This adjustment
is accomplished through the introduction of additives from suitable
supply tanks illustrated generally by the representative tank 40
feeding into the water storage and treatment tank 38 via a line 42.
The water storage and treatment tank 38 is selected so as to
provide sufficient retention time for agglomeration of the fines in
a quescent zone incorporated in the tank. The agglomerated fines
concentrated in the recycle waste are represented at 600. The
length of time of agglomeration will, of course, be dependent upon
the particular clays and other fines found in the tar sand and may
vary. Agglomeration is aided through the addition of flocculating
agents. The incidence of collision of the particles to improve
adherence in agglomeration may be enhanced by the incorporation of
a vibrator, such as a sonic vibrator, as is known in the art. The
treated liquid containing concentrated agglomerated fines exits the
storage and treatment tank 38 via a line 32 for reintroduction into
the extraction system. Under some circumstances the tank may not be
required and agglomeration in the layer will be sufficient. As
previously mentioned, hot water may be removed from an upper phase
in the water storage and treatment tank 38 via a line 12 for
addition to the tar sand in the mixer 14. Also, any minor amount of
oil dispersed in the water phase may be permitted to separate here
and withdraw from the top, if desired.
The tar sand is contacted with the up-flowing stream including all
of the solvent, recycle water and steam introduced to the
extraction vessel as is shown generally at 300. Here the relative
velocities of the down-flowing sand and up-flowing steam should be
such that the tar sand is fluidized sufficiently to permit good
effective tar sand-extractant contact but insufficiently active to
dislodge fines which are attached to the sand particles. This is an
important aspect of my process since it reduces the amount of fines
which must be removed in the water phase and helps assure that the
hydrocarbon phase has a minimum of fines. Thus, many fines can
remain with the sand as fines attached to the sand particles.
The sand, which is free of solvent and soluble chemicals following
the steam scouring, continues its down-flow against the incoming
recycle water containing concentrated agglomerated clay and silt
fines. As shown at 400, the sand particles are merely sufficiently
suspended and fluidized to act as a filter medium for removing
agglomerated fines from the recycle steam. The fluid velocity in
the extraction vessel will vary with the other process conditions
which are dependent upon the composition of the tar sand and the
nature of the extractant fed to the system. In any event, the
velocity should be great enough only to permit uniform distribution
of the extractant and desirably kept as low as possible for good
extraction contact.
The sand containing the filtered silt, clay and other agglomerated
fines settles to the bottom of the extraction vessel 24 where it is
represented at 500. Here it may be removed either by a drag type
conveyor 44, such as a screw conveyor, or pumped away as a slurry.
The drag type conveyor is preferred in that it allows the removal
of sand tailings containing a minimum amount of water and avoids
the need for pumping abrasive slurries. Furthermore, any water
remaining with the sand is likely to be hot and contain the
additives of the system. These can be recovered by adding a cold
water back wash to the conveyor via a line 46 at the point of
discharge of sand and agglomerated fines via a line 48. As a
consequence, not only are heat and conditioning chemicals retained
in the system, but the sand and agglomerated fines tailings
disposed of are free of possible pollutants.
It will be appreciated by those skilled in the art that process
variables such as the degrees of bed fluidization, process liquids
flow rates, as well as composition of additives in the system will
be governed by the mined tar sand to be processed. These operating
parameters can be determined according to known procedures by those
skilled in the art. In particular, considerable flexibility is
possible in the use of alkali for pH control, quantity of oil
extraction affecting agents such as wetting agents, dispersing
agents, gravity affecting salts and amounts of solvents because of
the closed-cycle feature in which all additives are recycled. For
example, if large quantities of solvent are required, the vapors,
which would collect in a vapor phase in the top of the extraction
vessel 24 may be compressed or condensed and recycled. The
requirements for pH, type and quantity of wetting agent, dispersing
agent, density of liquid media and amount of solvent will vary
according to the quality of the tar sand fed to the system. Thus,
it is likely that some or all additives, which are known in this
art, may not be required to obtain the degree of extraction
desired.
Thus there has been provided a process for extracting tar from tar
sand which is an improvement on the solvent-extraction procedure.
In particular, the system is highly advantageous in that it
requires only one extraction vessel and provides waste effluents
which are pollution free. Water process requirements are reduced
and, by virtue of using a closed system, solvent losses are
minimized and essentially negligible, thus contributing to
economies of operation. In addition, capital equipment costs are
decreased since this process does not require repumping and further
separation vessels such as elutriation vessels, phase separators,
particle separators, centrifuges, filter beds and the like.
* * * * *