Process for retorting oil shale and the like

The production of oil by retorting shale and other hydrocarbonaceous and lignocellulosic solid materials is facilitated by retorting in the presence of steam and acetic acid.

BACKGROUND OF THE INVENTION 
This invention relates to an improved retorting process for the production 
of oil from oil shale and like materials. 
It has been known for many years that a refinable hydrocarbonaceous oil can 
be produced by retorting oil shale and other solid hydrocarbonaceous and 
lignocellulosic materials. The commercialization of such processes is 
intimately dependent upon the yield of oil obtained per ton of starting 
material, the cost of the capital equipment required to conduct the 
process and, to a lesser extent, upon the ecological impact of the process 
upon the surrounding environment. I have now found that an improved yield 
of oil of higher quality is achieved with lower energy consumption by 
conducting the retorting process in the presence of steam and acetic acid. 
U.S. Pat. No. 2,966,450 (Kimberlin et al.) mentions the use of acetic acid 
in conjunction with solvents for extracting oil from shale, but states it 
is unsuitable for this purpose. U.S. Pat. No. 2,560,767 (Huff), U.S. Pat. 
No. 2,710,828 (Scott), U.S. Pat. No. 2,832,725 (Scott) and U.S. Pat. No. 
4,075,083 (Putman) all disclose methods for retorting oil shale where the 
particulate solids are passed down through a treating vessel, through a 
preheating zone, and through zones of progressively higher temperatures. 
Huff discloses a means whereby hot air from the end of the process is 
recycled to the preheat zone. 
SUMMARY OF THE INVENTION 
In one aspect, this invention relates to a process for the production of a 
hydrocarbonaceous oil by heating a hydrocarbonaceous or lignocellulosic 
solid material to form a non-volatile residue and a distillate comprising 
a hydrocarbonaceous oil, which process comprises heating the starting 
solid material in the presence of steam and acetic acid. 
In another aspect, this invention relates to a process for the thermal 
conversion of acetic acid into higher boiling distillable organic material 
comprising the steps of: 
(a) passing a mixture of steam and acetic acid through a bed of 
hydrocarbonaceous or lignocellulosic solid material at a temperature 
effective to convert a portion of the organic material in the solid 
material into a distillable hydrocarbonaceous oil and another portion 
thereof and the acetic acid into a more hydrophilic distillable organic 
material and further effective to volatilize the thusproduced more 
hydrophilic organic material and the hydrocarbonaceous oil; 
(b) separating the volatilized material from the residual non-volatile 
material; 
(c) condensing the volatilized material; 
(d) separating the more hydrophilic organic material from the 
hydrocarbonaceous oil; and 
(e) recovering the thus-produced more hydrophilic organic material and the 
hydrocarbonaceous oil. 
DETAILED DISCUSSION 
This invention is based upon the discovery that the yield of 
hydrocarbonaceous distillable oil produced by the destructive distillation 
of oil-bearing shale and other hydrocarbonaceous and lignocellulosic solid 
materials is increased by the introduction into such materials of both 
steam and acetic acid before the solid material is heated to its maximum 
temperature. Not only is the oil yield increased, e.g., up to 20% or more, 
but a superior quality of oil is produced which is more fluid and which 
contains less nitrogen. In the case of oil shale, oil yields of 110% of 
Fischer assay are common. This apparently is due to the acetic acid being 
a molecular catalyst which enters into a reaction with the kerogen organic 
material. Moreover, the acetic acid employed therein is converted into 
valuable higher boiling hydrophilic materials which can be recovered along 
with the oil. Such hydrophilic materials are of the carboxyl and 
longer-chained group of chemicals and can be separated from the aqueous 
phase by conventional methods, e.g., by the use of solvents, such as 
chloroform, in such volume and value as to make the recovery a worthwhile 
by-product recovery. Both the kind and the volume of by-product chemicals 
obtained vary widely with the oil shale material used. Novel products and 
additional chemicals are also obtained when acetic acid is used on 
lignite. 
The process can be energy self-contained, i.e., the combustible gases 
produced in the process can be burned and the hot combustion gases used to 
heat the solid material to the desired final temperature. The process can 
also be conducted in an ecologically clean manner by using the residual 
non-volatile material as a purifying medium for the water condensed along 
with the thus-produced oil and the more hydrophilic distillable organic 
material, so that it can be re-used in the system. Moreover, whenever 
pieces of wood such as pine tops or that which is left over by crews that 
clean power lines is retorted, such biomass products produce a high 
quality methane base, a lignin which is different than the lignin 
extracted today (because this novel lignin is produced with a different 
specific gravity and with the much desired ability to chemically bond with 
other chemicals and substances). Also, when such biomass is retorted, the 
high quality activated charcoal produced therefrom can be used as the fuel 
to provide the heat in the retort. In this latter use, the low p.p.m. 
"spent" water can be passed through a reverse osmosis membrane to produce 
a pure water, which is inexpensive to process, because the charcoal can be 
thereafter air-dried and used as fuel in the retort. One such biomass 
which can be used to obtain good quality oil, gas and charcoal in the 
central part of the United States is milkweed, which can be harvested 3 
times a year. 
In carrying out the process of this invention, the starting solid material 
is heated from ambient temperature to a final temperature of at least 
450.degree. C., preferably at least 500.degree. C., most preferably about 
500.degree. to 530.degree. C., over a period of about 1 to 2 hours, 
preferably about 1.5 hours. The final temperature is substantially lower 
than that required to conduct the retorting process in the absence of 
steam and acetic acid. 
The preferred starting material is oil bearing shale. Other solid 
hydrocarbonaceous and lignocellulosic materials, e.g., bituminous coal, 
tar sands, peat, and even sawdust, leaves and other waster lignocellulosic 
materials can be employed instead of oil bearing shale as starting 
material in the process of this invention. 
Before reaching the maximum temperature, the solid material is mixed with 
both steam and acetic acid. Glacial or aqueous, e.g., 6%, 28%, 56%, 70% or 
80%, acetic acid can be used. The amount of steam employed is preferably 
about 0.15 lbs. to 0.20 lbs., more preferably about 0.20 lbs., per pound 
of starting solid material. The amount of acetic acid employed is 
preferably about 0.015 lbs. to 0.03 lbs., more preferably about 0.02 lbs. 
(calculated as 100% acetic acid) per pound of starting solid material. In 
the case of oil bearing shale, about 5 gals. of glacial acetic acid per 
ton of shale is an optimal ratio. 
The steam and acetic acid can be mixed with the solid material separately, 
at different points in the process, or preferably concomitantly at 
approximately the same point or points in the process. Preferably, a 
continuous stream of steam and of acetic acid is added to a continuous 
stream of particulate solid material. Preferably also, a portion of the 
steam and acetic acid is added to the solid material while at a lower 
temperature than that at which the remainder of the steam and acetic acid 
is added thereto. Most preferably, a portion of the steam and acetic acid 
is added to the starting solid material in a preheat zone in which the 
solid material is heated to a temperature above 100.degree. C. but below 
the temperature at which the distillate is produced, preferably between 
100.degree. and 120.degree. C. Desirably, the latter portion of steam and 
acetic acid is added at a point where the solid material is at a 
temperature of about 300.degree. to 400.degree. C., preferably at least 
about 400.degree. C. 
The reaction time can be varied widely, e.g., from 60 minutes to 2 hours. 
The optimum reaction time is inversely proportional to the final reaction 
temperature and the rate at which the solid material is heated thereto. 
Generally speaking, a reaction time of about 1 to 2 hours is sufficient to 
yield all of the volatile organic materials which can be produced from the 
starting solid material. 
The reaction can be conducted batch-wise or preferably continuously. 
When conducting the process batch-wise, the starting solid material, acetic 
acid and water can be mixed together prior to initiating heating thereof. 
When the temperature reaches 100.degree. C. (or correspondingly higher, if 
the process is conducted under pressure), the water is converted to steam 
and most thereof is distilled off before any oil is produced, which 
usually does not occur below 200.degree. C. Alternatively, only a portion 
of the acetic acid and only enough water to moisten the solid material can 
be mixed therewith prior to heating and the remainder passed therethrough 
after the mixture is heated above 200.degree. C. and preferably above 
300.degree. C., or the starting raw material can be heated, e.g., above 
100.degree. C., preferably above 200.degree. C., before one or both of the 
steam and acetic acid are mixed therewith. 
Apparatus for conducting the process continuously is disclosed in my 
copending application Ser. No. 173,944, filed July 31, 1980 which issued 
on Apr. 20, 1982 as U.S. Pat. No. 4,325,787 whose disclosure is 
incorporated herein by reference. 
In conducting the process continuously on a commercial scale, oil shale is 
comminuted to a convenient particle range, e.g., ranging from fines to 
particles of about 1/4 inch in diameter. If tar sand is used, it can be 
mixed with other particulate hydrocarbonaceous or lignocellulosic solid 
material to render it less tacky and more flowable. The particulate solid 
material is then mixed with the acetic acid in the selected ratio. The 
beneficial effects of the acetic acid is not due merely to a lowering of 
the pH as strong mineral acids and higher fatty acids do not produce the 
beneficial results achieved with acetic acid. 
As stated above, a portion of the acetic acid, e.g., from 30% to 60%, 
preferably about 50%, is desirably admixed with the starting particulate 
solid material prior to its being heated to about 120.degree. C. This is 
conveniently accomplished before the solid material enters the retorting 
vessel, e.g., prior to or concurrently with the preheating of the starting 
solid material which preferably is conducted. 
Similarly, a portion of the steam employed in the process, e.g., from 30% 
to 60%, preferably about 50%, is desirably admixed with the starting 
particulate solid material prior to its being heated to about 120.degree. 
C. This is conveniently accomplished before the solid material enters the 
retorting vessel, e.g., prior to or concurrently with the step of 
pre-mixing the starting solid material with acetic acid. Such high 
moisture is a good conductor of heat within the solid material. 
After preferably being preheated with a portion of the steam and premixed 
with a portion of the acetic acid employed in the process, the particulate 
starting material is gradually heated to a temperature at which 
destructive distillation of the organic material therein occurs, e.g., to 
at least 450.degree. C., preferably about 500.degree. to 550.degree. C. 
Heating is preferably continued until substantially all of the 
volatilizable organic material has been removed from the particulate solid 
material. During the heating and before the solid material reaches a 
temperature above about 400.degree. C., steam and acetic acid in the 
amounts required to catalyze the volatilization of the organic material 
therein are passed therethrough, preferably as a continuous stream. 
The volatilized products are passed through one or more condensers to 
condense the volatilized liquids therein. When a plurality of successive 
condensers are employed, the liquid products can be fractionated so that 
all or most of the oil phase products are condensed before the aqueous 
phase products condense. Alternatively, all of the condensible products 
can be condensed together and the two phases separated by gravity or 
centrifugation. 
The economics of the process are enhanced by collecting the combustible 
gases remaining after the condensible liquids are separated from the 
gaseous products produced in the process. These gases are of high quality 
and have an energy content of about 700 btu/cu. ft. Most oil bearing shale 
produces enough such gases to provide the requisite heat energy required 
to perform the process if conducted in insulated apparatus and heat losses 
are otherwise minimized. 
The economics of the process are further enhanced by recovering the heat 
present in the spent particulate material. This can be done by passing the 
spent particulate material through a heat exchanger whereby the heat is 
transferred to incoming starting material, or to air used to burn the 
combustible gases and/or to the water used to form the steam employed in 
the process. 
In addition to the low nitrogen content refinable oil produced in the 
process, solid hydrophilic organic products are also produced. When the 
separated aqueous and oil phases are cooled below about 22.degree., these 
products appear as suspended solids in both phases and can be separated by 
filtration or centrifugation. Further organics can be precipitated from 
the aqueous phase by the addition of a solvent, such as chloroform. 
The preferred embodiment of the system disclosed in my prior filed 
application cited above comprises as the principle unit thereof a 
vertically disposed retort silo assembly. The apparatus associated 
therewith includes a receiver hopper for reception of the starting 
particulate raw material from, for example, a dump truck. The crushed oil 
shale or the like as deposited in the hopper is conveyed therefrom by an 
endless belt-type feed conveyor of a conventional nature, such as a bucket 
or plate flight type known in the art. The discharge end of the conveyor 
is in proximity to a vertically disposed endless belt type elevator which 
provides communication generally from the hopper to a discharge end. The 
elevator discharges raw material and dumps it into a bin, the lowermost 
surfaces of which are inclined and the bottom thereof discharges into an 
auger screw type feed conveyor which provides communication between the 
discharge opening of the bin and the interior of the retort. One large bin 
can support a pod of 5 to 10 silos. A baffle plate diverts the raw 
material from the conveyor downwardly into the retort. The retort chamber 
in which the crushed shale is received includes a vertically disposed 
hollow shaft which is mounted in a mercury bearing disposed at the lower 
end thereof. The shaft is driven in any suitable manner, for example by a 
vertically mounted electric motor and any suitable type drive mechanism, 
such as belts or gearing. An upper bearing positions the vertical shaft at 
its upper end. Disposed at periodic intervals along the linear extent of 
the vertical shaft in the retort are a plurality of horn-like arcuately 
shaped stirring fingers which are disposed to continuously agitate the 
shale and enhance migration of the crushed shale from the upper intake 
portion or zone of the retort to a retort spent solids discharge outlet. 
This function is additionally aided by gravity as the material is drawn 
off at the discharge outlet of the system. The particulate material within 
the retort migrates towards this discharge outlet and hence the reactions 
within the retort are of a continuous nature and extraction of the desired 
products of protroleum and other by-products of the chemical reactions 
carried out therein are of a progressive nature as the material moves 
downwardly through the interior of the retort. The lower portion of the 
retort housing is of a generally frustroconical configuration and a 
plurality of scraper blades mounted on positioning shafts, disposed at the 
lower portion of the shaft, effect a scraping movement against the inner 
wall of lower portion of the retort. A plurality of discharge shoevels, 
disposed immediately above the retort spent solids discharge outlet, 
direct the spent solids thereto. The materials falling through the spent 
solids discharge outlet are engaged by a screw type auger discharge 
conveyor, mounted within a housing, for movement horizontally to a 
conveyor discharge outlet for discharge of the material in any suitable 
manner, as by feeding to other conveyors, elevators or into the bed of 
dump trucks or railway hopper cars, as desired. 
The retort has a dual wall structure for providing heat exchange functions 
from hot combustion gases passed between the spaced chamber walls thereof 
to the particulate material contained within the retort. The metal which 
comes in contact with the retort can be constructed of Carpenter 20 Ch-3 
steel clad over T-22 structural steel or any other suitable material for 
both protection and strength. The external surface of the retort is 
covered by a layer of insulation to reduce heat loss. The heated walls 
distribute the heat throughout the outer parts of the retort chamber. Heat 
recovery fins may be made of copper and tied to a ring around the silo for 
better heat recovery. The outer shell metal may be made of steel and 
insulated with a suitable insulating material. The upper end of the heat 
exchange jacket formed by the dual walls of the retort is connected by 
conduits to provide fluid communication from the upper end of the heat 
recovery area of the retort to the outer shell of a steam boiler, disposed 
above the upper bearing assembly for the vertical shaft in the retort. The 
boiler is placed on top of the silo in such a manner as to utilize the 
escaping hot gases for heat recovery and greatest efficiency in the use of 
BTU's. The gaseous products which pass upwardly into the upper chmber area 
of the retort are carried off by an outlet conduit and passed through a 
condenser of a character well known in the art to a plurality of discharge 
conduits. Suitable valve arrangements are provided in the conduits for 
controlling the flow of condensed liquid into a pair of separator tanks. 
The lower end of the separator tanks are of a conical configuration and 
fitted above but proximate thereto are a pair of oil discharge conduits, 
each having discharge valves and being connected to each other by a "Y" 
connection for discharge into a crude oil storage tank. 
Phase separation in the separator tanks can be facilitated by providing 
them with cooling jackets to further cool the liquids condensed in the 
condenser and/or by the use of centrifuges in lieu of or in conjunction 
with the separator tanks, which collect the distilled liquid and separate 
the same by action of the respective specific gravities into crude oil, 
which is discharged at the oil outlets and dirty water which discharges at 
the lowermost water outlets into a water discharge conduit. The crude oil 
storage tank also has a conical configuration at the lower end thereof and 
is fitted with a suitable discharge valve disposed at its outlet for 
controlled discharge of the crude oil contained therein to a suitable 
dispensing conduit. Fitted at the bottom of the separator tanks are a pair 
of valves which control the flow of dirty water from the lowermost point 
of the separator tanks. A "U"-shaped conduit provides fluid communication 
from the discharge valves via a conduit to a dirty water collection tank. 
The lower portion of the dirty water collection tank is provided with an 
inclined bottom which is elevated at the end remote from the discharge end 
for flow from the discharge outlet tube to a limestone briquette water 
neutralizer tank of a construction similar to that of the dirty water 
tank. The neutralizer tank also has an inclined bottom for enhancing flow 
to the discharge outlet tube thereof which in turn is connected to an 
activated charcoal filter tank unit. 
The collected dirty water is run through limestone briquettes in the 
neutralizer tank to remove acidic elements and suspended solids therefrom. 
When the limestone is neutralized, it may be removed in order to extract 
water soluble materials, such as acetone, alcohol and acetic acid, 
therefrom. The inclined bottom thereof discharges into an effluent conduit 
which optionally is connected via pumping means to the water inlet of the 
steam boiler. A centrifuge can be disposed between the separator tanks and 
the dirty water collection tank to remove any solids suspended in the 
dirty water. 
The upper ends of the separator tanks are each connected to a gas venting 
conduit through which the combustible gases vented therefrom are 
transported to a plurality of gas inlet conduits which are connected to a 
plurality of conventional gas burners, two of which are disposed adjacent 
to the tapered bottom portion of the retort, adjacent the scraper 
assemblies, in the interior of the spaced heat exchange chamber between 
the double walls of the retort, thereby to provide heating of the 
particulate material contained in the retort at various levels or zones 
thereof, and others of which are disposed in the housing of a preheat 
chamber surrounding the feed conveyor to preheat the particulate material 
before it enters the retort. 
The interior of the retort heat exchanger portion is provided with a copper 
lining as shown at the frustoconically shaped lower portion thereof for 
more efficient heat exchange. The housing of the discharge conveyor is 
enclosed by a chamber for heat recovery purposes. 
Alternatively, the gas inlet conduits can be connected to suitable gas 
storage tanks and commercially available natural gas can be used in lieu 
of the vented gases or, alternatively, in combination therewith to fuel 
the gas burners. 
The steam boiler is connected to a steam distribution system whereby steam 
is fed into the interior of retort, just above the frusto-conical lower 
portion thereof, by a conduit and to the interior of the housing 
surrounding the feed conveyor which is connected between the bin and the 
interior of the retort at or adjacent the discharge port. The outer 
housing of the heat exchanger also provides a preheat chamber for the gas 
burners therein which are in fluid connection to gas venting conduits with 
the venting conduits at the top of the separator tanks. 
In the preferred embodiment, the housing of the feed conveyor is also 
connected to a first acetic acid storage tank whereby acetic acid is 
carried from the outlet of the tank into the interior of the feed conveyor 
housing for admixture along with the steam with the particulate raw 
material as it moves through the feed auger conveyor to the retort. An 
additional acetic acid dispensing tank and the steam distribution system 
are connected for fluid communication of steam and acetic acid with a 
lower portion of the retort by virtue of an inlet conduit which passes 
through the double walls of the retort. A shield is disposed at the 
entrance to the gas outlet conduit at the top of the retort to prevent any 
particules of raw material from entering the gas outlet. The weight of the 
raw material in the holding bin prevents the rearward escape of any gases 
from the feed conveyor. 
The metal portions of the system which are contacted with the acetic acid 
are formed of a non-corrosive material.

Without further elaboration, it is believed that one skilled in the art 
can, using the preceding description, utilize the present invention to its 
fullest extent. The following preferred specific embodiments are, 
therefore, to be construed as merely illustrative and not limitative of 
the remainder of the disclosure in any way whatsoever. 
EXAMPLE I 
Eastern Shale 
Thoroughly mix 250 kg. of eastern shale (ground to a 1/4 inch size) with a 
mixture of 100 liters of water and 5 liters of glacial acetic acid in an 
acid resistant reactor fitted with a water cooled condenser. Heat the 
mixture from ambient temperature (22.degree. C.) to 102.degree. C. in 
about 35 minutes, at which time water will begin to distill from the 
reactor. Raise the temperature of the shale to 120.degree. C. over a 
period of about two hours, at which time about 100 liters of water will 
have distilled from the reactor. Raise the temperature of the shale to 
530.degree. C. over a period of about 2 hours, at which time about 19.5 
liters of oil phase and about 7.5 liters of aqueous phase distillate is 
obtained. Cooling both phases to below 70.degree. C. and centrifuging 
yields from the oily phase about 19 liters and from the "oily" and aqueous 
phases about one gallon of valuable solid organic products which were 
separated with a solvent (chloroform). The oil is a high quality 
refinable, petroleum-like oil of red color, high quality and free of 
ammonia odor. The yield thereof corresponds to 18.33 gallons per ton of 
shale. The non-condensible portion of the volatiles is a combustible gas 
which can be burned to heat the retort. 
Following the same procedure but omitting the acetic acid yields about 17 
liters of oil phase and about 8 liters of an aqueous phase, neither of 
which phases contain significant additional solid organics. In addition to 
a lower yield of oil than the run conducted with acetic acid, the oil is 
darker and of a lower quality. The yield thereof corresponds to 16.3 
gallons per ton of shale. The acetic acid thus produces 14% more oil of 
higher quality than conducting the retorting process in the presence of 
steam only. Further, the carboxyl group-containing chemicals separated by 
the use of a solvent (chloroform) are very valuable. 
EXAMPLE II 
Pine Sawdust 
Follow the procedure of Example I employing 125 kg. of moist pine sawdust 
(70 kg. dry weight), 100 liters of water and 5 liters of glacial acetic 
acid, heating from ambient temperature to 102.degree. C. over a period of 
2.75 hours; to 200.degree. C. in 1.25 hours and to 465.degree.-478.degree. 
C. in about 3 hours. About 108 liters of water is collected as the 
temperature rises to 200.degree. C. As the temperature rises further to 
about 460.degree. C., about 43 liters of a mixture of water and naval 
stores, and lignin, is obtained. At the highest temperatures, about 2.3 
liters of high quality diesel-like fuel oil is produced. The residue is 
high quality activated charcoal. The lignin produced is novel and 
extraordinary in that it bonds readily with other chemicals. 
Conducting the same reaction in the absence of the acetic acid yields 113 
liters of water; 33 liters of a mixture of water and naval stores; and 1.3 
liters of fuel oil. Use the activated charcoal by-product to clean potable 
or secondary water prior to its use as fuel to provide the necessary heat 
for the retort. 
EXAMPLE III 
Peat 
Following the procedure of Example I using peat and 4% by weight thereof of 
glacial acetic acid yields about 15 gallons of diesel-like fuel oil per 
ton of peat, plus solid distilled organics and copius amounts of 
combustible gas. If the acetic acid is omitted, the yield of oil drops to 
about 10 gallons, the quality thereof is lower and no significant amount 
of solid distilled organics and a lesser amount of combustible gas is 
produced. 
EXAMPLE IV 
Shale 
Employing the retorting apparatus described herein which is the subject of 
my prior-filed application cited hereinabove, feed western shale ground to 
a particle size from 1/4 inch to fines (1%) to a 40 ton capacity retort at 
a rate of 20 tons/hr. so that the shale has an average residence time in 
the retort of about 2 hours. In the preheater, mix the shale with 50 
gallons/hr. of 100% acetic acid and 8,000 lbs/hr. of steam (400.degree. 
C.). Burn combustible gases in the burners in the preheater at a rate such 
that the shale is heated by indirect heat exchange at a temperature of 
about 120.degree. C. Burn combustible gases in the burners positioned 
between the double walls of the retort at a rate such that the shale is 
discharged from the retort at a temperature of about 530.degree. C. About 
half way down the retort, above the frusto-conical bottom portion thereof, 
introduce 50 gals/hr. of 100% acetic acid and 8,000 lbs/hr of steam 
(700.degree. C.) into the shale, where it is at a temperature of about 
500.degree. C. 
In a heat exchanger positioned around the discharge conveyor, cool the 
shale by indirect heat exchange to about 100.degree. C. with air as it 
passes through the conveyor and mix the heated air with the combustible 
gases burned in the preheated and retort. 
Transfer the exhaust gases exiting from the double wall heat exchange area 
of the retort to the shell side of the boiler to supply the steam used in 
the process. Pass the volatiles exiting from the retort through a 
condenser which cools the condensed liquids to about 20.degree. C. 
Transport the residual combustible gases to the burners used to heat the 
preheater and the retort. Separate the aqueous phase of the condensed 
liquids from the oily phase by gravity or centrifugation. Cool the 
separated phases to about 20.degree. C. and separate the solidified solids 
suspended therein, amounting to about 6,700 lbs/hr. in the oily phase and 
about 800 lbs/hr. in the aqueous phase. These solids are valuable organics 
which can be used to defray a substantial portion of the cost of the 
process. Transport the resulting about 840 gals./hr of the oily phase to a 
storage tank for storage prior to shipment to a refinery. 
Pass the about 2,000 gals./hr. of aqueous phase successively through a sand 
bed, a limestone bed and a bed of activated charcoal. Transport the 
resulting clean water along with fresh make-up water to the tube side of 
the steam boiler. 
Transport the residual non-condensed gases (about 22,400 cubic feet/hr.) 
containing about 700 btu/cu.ft. to the burners in the retort system to 
supply at least a portion of the combustible gases burned therein, using 
commercially available gas as needed in start-up operations and storing 
excess combustible gas produced in the process for scrubbing and sale. 
The preceding examples can be repeated with similar success by substituting 
the generically or specifically described reactants and/or operating 
conditions of this invention for those used in the preceding examples. 
From the foregoing description, one skilled in the art can easily ascertain 
the essential characteristics of this invention, and without departing 
from the spirit and scope thereof, can make various changes and 
modifications of the invention to adapt it to various usages and 
conditions.