US2431677A

US2431677A - Process for the recovery of oil from shales

Info

Publication number: US2431677A
Application number: US598389A
Authority: US
Inventors: Harry D Brown
Original assignee: Individual
Current assignee: Individual
Priority date: 1945-06-08
Filing date: 1945-06-08
Publication date: 1947-12-02
Anticipated expiration: 1964-12-02

Description

Defi. 2 H, D PROCESSES FOR THE RECOVERY OF OIL FROM SHALES Filed June 8, 1945 INVENTOR. HARRY .0. 500w.

ATTORNEY.

Patented Dec. 2, 1947 PROCESS FOR 'rnn macovnmr OF 011.

mom snares Barry D. Brown, Rifle, Colo. Application June a, 1945, Serial Nb. 598,389

2 Claims. (01. 196-14) This invention relates to a method and means for the processing of oil ,shales and other pyrobituminous materials for the recovery of oil therefrom.

The processing of oil shale has presented a dimcult problem. The quantity and character of the evolved oil has been infinitely variable, depending upon the method of retorting and the tem, perature at which the destructive distillation was carried out. The presence of air in a retort is usually detrimental and the carry-over of dust with the vapor interferes with the refining operations which must follow.

The principal object of the invention is to provide a continuous method and means for the complete recovery of oil from oil shale at a low temperature whereby the kerogen is transformed into a soluble group of hydrocarbons inwhich the character and quality of the recovered oil will b uniform.

Another process is to provide a method or process for this purpose in which the bitumen will not be subjected to destructive distillation so that the highest obtainable recovery of oil willbe efiected.

A further object is to provide a process'in which the residue of the shale will have exceptional value as a soil conditioner and fertilizer and in which the same residue may be prepared to form a highly active adsorbent for stabilizing gasoline distillates.

Other objects and advantages reside in'the improved means and the method of use thereof. These will become more apparent from the following description in which reference is had to the accompanying drawing which forms a part' hereof.

The drawing illustrates a diagrammatic flow sheet of the process. 1

Briefly, the method contemplates a removal of the oil from the shale by digestion underthe infiuence of heat in the presence of an oil recycle stock in which the liberated hydrocarbons are soluble aided by a suitable catalyst.

Referring to the drawing, the shale to be treated, having been dried and ground to pass a ten mesh screen (or coarser, if mechanical separation of the pulp can be prevented), is fed from a fine ore bin ID at a uniformrate to a pulp conditioner l2 provided with any suitable agitating mechanism 53. A catalyst, such as aluminum chloride (anhydrous), is added to and agitated with the shale in the conditioner l2 from a catalyst storage hopper ll through a catalyst line Hi. If aluminum chloride is used as the catalyst, it

should not exceed three percent of the dry shale weight.

Suflicient vehicle 011, which will be herein designated the "recycle stock," is fed into the conditioner' I! from a recycle stock piping system iii to form a pulp with the ground shale which is sufliciently fluid to be pumped. The recycle stock is obtained as a product of the improved method as will be later described.

' The fluid pulp, after thorough intermixing, overflows from the conditioner I2 at a point well above the bottom thereof and flows to a pulp pump l6 by means of which it is forced through a pre-heating coil H in a suitable furnace I8 where it is heated to not more than 250 C.

, The hot pulp flows from the furnace to a series of digestion cells l9 provided with any suitable mechanical agitators 20. The pulp is introduced into each cell through a feed sleeve 2| above and about the agitator of that cell and flows from each cell to the next successive cell through a Each digestion cell i9 is provided with a suitable heating jacket 23 capable of maintaining a temperature of 200 C. at the vapor outlet of each cell.

As the digestion progresses in the cells Hi, the

kerogen is. converted to soluble hydrocarbons and fixed gases. The light fractions of the former are volatilized and expelled with the fixed gases through the vapor outlets of the cells to a vapor line.

Exfoliation of the shale particles above grain size along the plane of original laminations occurs under the conditions of the digestion and reduces the shale to a very fine carbonaceous residue. This assuresintimate contact with solvent and complete removal of the oil therefrom.

The density of the pulp overflowing the final cell is adjusted by control of the amount of recycle stock introduced at the conditioner E2 to a consistency of approximately 50% solids. The overflow from the final cell is conducted to a re-, ceiver or surge tank 24 from whence it flows to a continuous, totally enclosed, vacuum filter 25 where substantially all of the remaining oil is removed and/or separated from the residue.

The separated oil is then forced by means of a pump 26 through re-heating coils 21 in the furnace l8, thence through feed lines 33 to a primary fractionating column 28 of conventional design which forms a part of a standard refinery, designated in its entirety by the numeral 29.

The filter cake from the continuous filter 25 is repulped in a suitable mill 38, positioned directly under the filter 25, with a suilicient amount of gasoline or light naphtha, furnished by a solvent pump 41, to dissolverout the remaining oil; The dissolved oil and solvent flow to a settling tank 3|,the clear overflow of which is pumped by means oi a pump 32 into the fractionating column 28 through the lines 33.

The thick sludge from the tank 3! is conveyed by means of the totally enclosed, refuse chain conveyor 34 through a heater 35 in which the temperature of the residue is elevated to not less than 200 C. to volatilize the remaining solvent and any residual aluminum chloride.

The dried residue is cooled and stock piled at 33 ready for market as a soil conditioner. If the residue is to be used as an adsorbent in petroleum distillation, it is discharged from the conveyor 34 directly into a suitable rotary kiln 39 and heated to 500 C. at which temperature the carbon escapes as carbon dioxide (CO2). A light tan colored decarbonized ash is produced, indicated at 43-, which is useful as the adsorbent previously mentioned. The carbon dioxide will pass to the atmosphere or, if desired, may be used in saturating the caustic liquors in the recovery of phenols from the oils of the process.

The vapors and fixed gases originating in the digestion cells I9, and the vapors from the heater 35 together with the aluminum chloride sublimed at these points, are conducted through the vapor line 4| to a dephlegmator or partial condenser 36 where the aluminum chloride is condensed and the solvent vapors and fixed gases are expelled through a vapor line 31 of the fractionating column 28. A portion of the recycle stock is diverted from recycle piping l through a reflux line 42 to the top part of the dephlegmator above trays 43 therein. The reflux cools the vapor to approximately 175 C. so as to remove the aluminum chloride. A small portion oi the light fractions volatilized from the cells l9 will also be condensed and this condensate plus the oil reflux will form a slurry with the aluminum chloride which is returned from the bottom of the dephlegmator, to the recycle stock piping system I5.

An intermixture of the slurry from the dephlegmator 3G and oil from the pump 26 forms the recycle stock which is employed in the conditioner l2. Thus a closed circuit for the catalyst is obtained. Mechanical losses and losses by decomposition of the aluminum chloride due to the presence of water are low and the additional amount of aluminum chloride necessary to maintain a definite reagent concentration of not more than three percent during operation is exceedingly small.

The uncondensed vapors and fixed gases flow from the top of the dephlegmator 36 through the vapor line 31 to the primary fractionating column 28. Aby-Pass line 44 is provided for use with catalysts other than aluminum chloride, thus eliminating the, partial condenser 36 which is intended for aluminum chloride recovery only.

The non-condensable gases from the process are conducted to an absorber 45 in the refinery 29 in whichthe very light hydrocarbons will be recovered. The gases thus stripped are discharged from the top of the absorber through a gas line 46 and pass to a suitable gasometer for use for heating purposes in the plant. It will be noted that the oil recycle stock and the catalyst are acting directly on the ra natural shale and not on any products of destructive distillation. Therefore, the recovery is much more direct and more simplified than prior meth- 4 ods. Specific laboratory tests. substantiate the above process in every detail. I

The oil recycle stock is only a portion of the unvaporized oil from the digestors as separated from the residue on filter 23. The oil not so used passes on to the refinery thru the furnace 18. It will be recalled that the digestors remove only the light hydrocarbons in the form of vapor along with the fixed gases and aluminum chloride.

The endpoint of gasoline is about 200 0., therefore, only crude gasoline has been expelled at the digestion cells. The initial boiling point of the hydrocarbons in solution in the recycle stock, also the recycle stock itself, is 200 C. The unvaporized oil from the digestors will, therefore, contain the fractions starting with kerosene and ending up with lubrication oils and pitch. After primary fractionation these oils are refined to their respective marketable products. Then too, when equilibrium is reached in the process, the amount of recycle stock will be constant and the hydrocarbons derived from the freshshale being intro- 'duced will be over and above that amount used as recycle stock.

While preferred forms of the invention have been described in some detail together with the theories which it is believed to best explain its success, it is to be understood that the invention is not limited to the precise procedure described nor is dependent upon the accuracy of the theories which have been advanced. On the contrary, the invention is not to be regarded as limited except in so far as such limitations are included within "the terms of the accompanying claims in which it is the intention to claim all novelty inherent in the invention as broadly as is permissible in view of the prior art.

Having thus described the invention, what is claimed and desired secured by Letters Patent is:

1'. A process for the recovery of oils from shales comprising: intermixing the shale with sufiicient' vehicle oil to form a fluid mixture;

pumping the mixture through a pre-heater to a overflowing the fluid mixture from the digesting cell; filtering the latter overflow to separate the sludge from the oil in the remaining mixture; pumping a portion of the latter oil through a heater to a fractionating column: fractionating the latter portion to obtain fractions therefrom; intermixing the remainder with additional shale for introduction into the process; repulping the sludge from the filtering step witha gasoline fraction; settling the solids from the pulp; and pumping the fiuid residue to said column, 7

2. A process for the recovery of oils from oil shales comprising: intermixing the shale with a hydrocarbon oil product of the process having an initial boiling point of about 200 C., adding aluminum chloride to said mixture; maintaining the mixture as a pulp by mechanical agitation in a digestion zone at a temperature of 200 C. for a time sufilcient to convert all kerogen of the shale to hydrocarbons and to vaporize aluminum chloride and hydrocarbons boiling below about 200 C.; withdrawing resulting hydrocarbon vapors, fixed gases and aluminum chloride vapors as an overhead product from the digestion zone; condensing the aluminum chloride vapors and at least some of the hydrocarbon vapors to form a slurry of aluminum chloride in liquid hydrocarbons and returning the slum to the initial mixing step; removing. non-volatilized oil and shale residue from the digestion zone; separating the non-volatilized oil from the shale residue; recycling a suitable quantity of the non-volatilized oil to the initial mixing step as the hydrocarbon oil product having an initial boiling point of about 200 C.; discharging the remainder of the non-volatilized oil to a primary fractionating system and recovering a gasoline fraction therefrom, repulping the shale residue with the gasoline fraction for recovery of the oil still retained in the shale; separating the repulped shale residue into a solid shale residue and a liquid oil fraction; and recovering by distillation any gasoline hydrocarbons remaining in the solid shale residue.

- HARRY D. BROWN.

6 1 REFERENCES CITED The following references are of record in the file of this patent: