US2098772A - Continuous pressure distillation process - Google Patents

Description

Nov. 9, 1937. o. c. BREWSTER ET AL CONTINUOUS PRESSURE DISTILLA'IION PROCESS Filed Feb. 13, 1928 2 Sheets-Sheet 1 m fizz/622507.22"

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azzwzw g real E120 Nov. 9, 1937. o. c. BREWSTER ET AL 7" CONTINUOUS PRESSURE DISTILQLATION PROCESS Filed Feb. 13, 1928 2 Sheets-Sheet; 2

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Patented Nov. 9, 1937 PATENT OFFICE 2.098.772 con'rmuoos rasssoan nrs'rmm'nou raooass Oswald C. Brewster, Max "G. Paulus, and Andrew E. Thompson,

Casper,

Wyo., assignors to Standard Oil Company, Whiting, Ind., a cornotation of Indiana Application February is, 1928, Serial No. 253,978

19 Claims.

The present invention relates to improvements in the art of pressure distillation of hydrocarbon oils heavier than gasoline for the production of hydrocarbons of the gasoline range boiling points therefrom. It will be fully understood from the -following description illustrated by the accompanying drawings, in which:

Figure 1 illustrates, partly in section and in part diagrammatically, apparatus suitable for carrying out the invention; and

-Fig. 2 illustrates a modified form of apparatus in which certain variant forms of the invention may be carried out. 7

Referring more particularly to Fig. 1, the numeral 6 indicates a suitable oil container, preferably a horizontal, cylindrical shell or still adapted to withstand high internal pressure and to contain a substantial body of oil undergoing treatment. The shell or still 5 is mounted upon a suitable furnace setting 6, and is protected from the direct heat therefrom. Within the furnace setting there are provided a large number or bank of inclined tubes 1, the lower ends of, which communicate with a lower headerv I and the upper ends of which communicate with an upper header 9. The lower header 8 communicates with a vertical pipe it which extends upwardly out of the furnace setting through the wall of the shell I and for a short distance thereinto. The upper 30 end of this tube or pipe Ill forms a seat for a closure member H mounted on the stem of a rod l2 threaded through a boss I! on the upper part of the shell 5, the rod being operated by a hand wheel I. It is readily apparent that, by operation of the rod I2, the upper end of the tube or pipe Ill may be closed to prevent communication with the contents of the shell 5 or may be opened to permit free communication therewith.

The upper header 9 likewise communicates with an upright pipe or tube J5 which enters the shell 5. The pipe I! is surmounted by a hood or bell '6, the bottom of which is below the outlet of;

From the upper part of the shell 5 the vapor outlet ,Il communicates with a suitable reflux condenser or dephlegmator l8, illustrated diagrammatically. Reflux condensate formed therein is returned by the pipe I9 to the interior of the pipe III in the upper portion thereof. Vapors unoondensed in the reflux condenser l8 are discharged to a suitable final condenser and pressure controlling means, such as are commonly employed in the art and are not shown herein.

From a point above the bottom of the shell 5, a conduit 20, provided with a pressure release valve 2| and control valves 22, leads to a conduit 23, preferably formed with gradually expanding portions and opening into a reduced pressure drum or chamber 24. Within the drum 24, the conduit 23 opens downwardly above a deflector 25 some 5 distance above the bottom of the drum. In the upper portion of the drum there are provided a plurality of baflie plates 28 of any .suitable form, .or other suitable means for preventing entrainment of unvaporized liquids by the vapors leave ing the drum. From the upper portion of the drum, the vapor conduit 21 leads vapors to the lower portion of a column or tower 28, illustrated diagrammatically as a bubble tower. The plates in the tower 28 may be of any desired form.

At asuitable intermediate point in the tower 28, the feed pipe 28 enters and may be employed for thesupply of a hydrocarbon oil cooling medium or for the supply of fresh oil fed to the unit. A second supply pipe 30 enters the upper portion of the tower and may be employed for supplying thereto a cooling'medium of a lower range of boiling points,. such as, for example, a condensate from the vapors evolved from the tower 28. From the upper portion of the tower, a vapor conduit 3| leads to any suitable condensing means (not shown).

Condensate formed in the fractionating column or tower 28 and collected in the base thereof is withdrawn through valved pipe 32 and forced by pump through the valved pipe 34 to an intermediate point in the fraotionating column l8, from. which it passes, together with reflux condensate, through pipe l8 into the large pipe ill extending from the lower header 8 in the furnace into the still 5.

From the base of the drum 24, unvaporized oil is discharged through the valved pipe 38 and forced by pump 21 through the pipe 38. The latter communicates with a pipe 38 provided with control valve 40 leading to a tar cooler or heat exchanger 4 I, from which the cooled unvaporized oil or tar is discharged through the line 42. The pipe 38 also communicates with a line I! provided with control valve 44 through which any desired portion of the unvaporized oil or the tar may be directed to the interior of the shell I.

In carrying out an operation in accordance with the present invention, employing the apparatus of Fig. 1 as herelnbefore described, the still is 50 initially charged with oil to a level substantially 7 above the tops of the pipes l0 and I, said pipes, the headers 8 and 8 and the inclined tubes I being entirely-filled. With a still of ordinary dimensions, say 30 feet in length and feet in brought to cracking temperature, for example,

725 to 750 F.) a suitable superatmospheric pressure being maintained thereon, the valve '2l is opened to permit the flow under reduced pressure of a certain proportion of the contents of the still through the pipe and conduit 23 leading into the drum 24.

, vapors from unvaporized oil takes place, the vapors passing through conduit 21 into the column 28. In order to efl'ect a partial coolingof the vapors in the column 28, oil, such as the stock which it is desired to feed into the unit during operation, is fed in through the pipe 29 and is itself in part preheated by the vapors passing through the column. This feed may be suitably a gas oil of charhcteristics similar to that charged into the still, although, as hereinafter pointed out, the'cold stock fed into the unit in this mam ner may be of widely varying characteristics, crude oil, for example, being suitable. The unvaporizerPportion of the feed, preheatedby the vapors in the column 28 together with the condensate formed from such vapors is withdrawn through the pipe 32 and forced by the pump 33 through the conduit 34 and into dephlegmator l8,

from which it passes with the reflux condensate through pipe l9 into thedepending pipe l0, which is then cut off from communication with the charged through the pipe 38 is forced by thepump 31 through the line 43 back into the shell; During this portion of the operation, it will be noted that the entire unvaporized portion of the liquid removed from the still remaining in the drum 24 is returned directly to the shell or still and the condensate from the vapors given of! e from the drum 24 is returned .together with the fresh feed stock or the unvaporized portion thereof to the interior of the pipe ID, to pass through the heating tubes I and the ascending pipe l5 into the body of the still. At the same time, the reflux condensate formed in the column I 8, being the portim of the vapors evolved fromthe still heavier than the desired distillate product, is

returned through the pipe I! directly ';0 the interior of the depending'pipe III. Under these conditions of operation, the temperature of the oil in the depending pipe "I is substantially lower than that in the pipe l5 and in the shell 5.

Operation in the manner described is continued until the contents of the shell or stfll 5 have reached the. conditions which it is desired to .maintain throughout the operation. For exam- 1 pie, with an initial charge of type of gas oil having a gravity of 33 A. P. I., the stock in the shell may reach an operating temperature of, say

F. After this desired point has been reached,

a certainproportion of the tar or bottoms're-.

In the drum 24 a separation of charged being controlled tomaintain the liquid in the still 5, of the desired character. The amount of fresh feed stock added to the system through .the supply pipe 29 is controlled to maintain a substantially constant volume of oil in the shell 5; that is, it is substantially equal in amount, to the distillate drawn oil from the vapors leaving the still after passing the dephlegmator l8 and the light distillate formed from the vapors leaving the column 28 through the vapor line 3| together with the tars or bottoms through line 39.

In order that the conditions prevailing, in the unit may be clearly understood during its normal operation after a desired running condition has been reached, the following conditions are set forth as they exist in a typical operation in a still of the capacity referred to above, in which the stock initially chargedwas a 33 gravity oil of the character of gas, oil, about 13,000 gallons being held in the shell, pipes l0 and I5, headers 8 and 9 and inclined tubes 1. After normal running conditions were attained, the liquid contents of the still were at a temperature averaging about 735 F., a pressure of 96 lbs. belng maintained thereupon, and rapidly attained a gravity of 25 to 20 A. P. I., subsequently falling slowly in gravity and the tar or unvaporized oil drawn from drum 24 had a Saybolt Furol viscosity of 55 to 60 at 122 F.

The temperature of the descending oil in the pipe I0 is not higher than 650 F. and that in the ascending pipe l5 just.below the bottom of the shell 5 averages about 790 F. 400 to 425'gallons per hour of distillate are taken off from the vapors leaving the shell after reflux condensate has been removed therefrom in a dephlegmator I8, such reflux condensate being returned to the pipe [0. Approximately 1,650 gallons per hour of the contents of the shell are removed throughthe line 20, of which about 350 gallons per hour discharged remain unvaporized in the drum 24 and are withdrawn therefromb Of this, approximately 215 gallons per hour are returned through the line 43 to the shell 5. The remainder, about 135 gallons per hour, is discharged from the system.

The temperature in the drum 24, which is approximately at atmospheric pressure, is about 540 F. The vapors discharged through the line- 21, which are approximately equivalent to 1,300 gallons per hour of oil,"then enter the tower 28, into which about 650 gallons per hour of fresh feed are supplied through the pipe 29. The fresh feed and condensate formed in the tower 28, which together amount to about 1,800 gallons per hour are returned to the pipe l0 through the line 34, dephlegmatorv l8 and pipe l9. It will thus be seen that the amount of oil returned to the still through the lines 34 and 43 is substantially equivalent to the ,sum of the net distillate withdrawn from the still and the tar or unvaporized oil discharged through the line 20.

The above example is by way of illustration, and the invention is not limited to the use of the stocks and pressure conditions set forth therein. Stocks of other characteristics may be charged or fed into the still, and the stocks fed in during normal operation may vary from that initially charged. The pressure may also be widely varied. By operating in the manner described, we have been able" to run continuously for long periods of .time and with great economy of operation. Furthermore, in operating in accordance with the present invention, the desired heating of the oil is effected without the use of excessively-long ,flred coils involving great friction losses and character of the unvaporized liquid or tar formed in and withdrawn from the flash drum 24 may be controlled by varying theextent of vaporiza-' tion taking place therein, any such variation producing a corresponding result in the character of stock in the shell or still.

liquid therein or into the stream of liquid entering the drum. In Fig. l ot the drawings suitable means are provided for using the vapor product present in the still for this purpose. Thus .vapors from the still may pass through line I! 'controlled by valve 16 directly to the line 20 through which the liquid from the still passes to drum 24. A similar result may be secured by increasing the difference in pressure between the still and the drum 24 as by raising the pressure in the former.

It is apparent that if increased proportions of the liquid withdrawn from the still are vaporized in drum 24, larger amounts of condensate are formed in tower 28 and returned to the system, thus permitting the elimination of a greater proportion or all of the tar or residuum formed in drum 24.

Figure 2 illustrates a modified form of constructiomin accordance with the present invention.' In the iorm illustrated in this figure, the numeral 55 indicates a shell or still, 56 the furnace setting, 51 the inclined heating tubes, 58 the lower header and 59 the upper header, these parts being similar in arrangement and construction to the corresponding parts as illustrated in Fig. 1.

The lower header 58 communicates with the vertical pipe 60 which extends upwardly into the shell 55 and is closed ofi from the body of the shell by the closure 6| operated by the rod 82. The upper header 59 is connected by the vertical pipe 53 with an enlarged pipe section 64 within the still, open at the top and surmounted by a bell or hood 65 which directs any material issuing from the pipe section 64 in a downward and later-.

al direction in the shell. The pipemember 64 is connected by a conduit or pipe section 86 with the descending pipe 60. Vapors from the shell or still 55 pass out through the vapor line 61 into the reflux column or dephlegmator 88 in which the portions heaviei' than the desired distillate products are condensed by cooling. The reflux condensate formed is returned through the ,line 51 in countercurrentto the vapors issuing BIS from the still, the reflux condensate dropping into a funnel-shaped opening 69 of a pipe 69", by which it is led to the interior of the enlarged pipe section 64.

The arrangement in connection with the shell 55 for withdrawal of liquid from the shell, reduction of pressure upon and partial vaporizing of this liquid, and return of unvaporized liquid (when desired) are substantially similar to those shown in connection with Figure 1 and the respective parts are indicated by the same numerals with the suilix a. In general the operation conducted in these parts is the same as already described in connection with Fig. 1. In the form shown in Fig. 2, condensate from tower 28 together with fresh feed supplied thereto is forced If desired, steam or other vapor may be introduced in the body of through line 34 directly to a downwardly directed nozzle 35 in conduit 60.

In the operation carried 0 t in the apparatus in'accordance with Fig. 2, will be noted that there is a continuous withdrawal of liquid from the shell or still through line 20', the pressure is reduced upon the material so withdrawn, the vaporized portion is partly condensed and the resulting condensate returned to the interior of the vertical pipe 80 communicating with the bottom header 58 and a part of the unvaporized portion of the liquid withdrawn from the shell 55 may be returned to the shell through the line 43 In these respects the operation is essentia ily similar to that described in connection with Fig. 1. Similarly iresh teed is supplied to the system in essentially the same manner as in the operation previously described. 'It will be noted through the heating pipes 51 and as a consequence, a higher average temperature is maintained in the pipe 60 in the operation conducted in accordance with Fig. 2 than is maintained in the pipe to of the operation of Fig. 1.

We claim: 1'. In apparatus for distilling hydrocarbon oils under pressure for theproduction of lighter hydrocarbon oils of the character of gasoline, a container, a bank or inclined tubes below said container, means for heating said'tubes, upper and lower headers communicating with the upper and lower ends of said tubes, conduits extending irom said upper and lower headers into the .said container, said conduits extending above the lowermost portion of said container, means for cutting off communication between the interior of the container and the'conduit extending to the lower header, means for withdrawing liquid from the interior of said container, means for vaporizing a portion oi the liquid so removed,

and means for supplying unvaporized portions of removed liquid directly to the container.

, 2. In apparatus for distilling hydrocarbon oils under pressure for the production of lighter hydrocarbon oils of the character of gasoline, a container, a bank 01 inclined tubes below said container, means for heating said tubes, upper and lower headers communicating with the upper the interior of said container, means for vaporizing a portion of the liquid so removed, and means for supplying a portion of the unvaporized material directly to the container, means tor condensing at least a portion or the vaporized part 01' said liquid, means for supplying condensate thus formed within the conduit communicating with the lower header.

3. In apparatus for distilling hydrocarbon oils under pressure for the production of lighter hydrocarbon oils of the character of gasoline, a container adapted to contain a body of liquid hydrocarbon oil undergoing cracking, a bank of inclined tubes below said container, means for heating said tubes, upper and lower headers communicating with the upper and lower ends of said tubes, conduits extending from said upper and lower headers into-the said container, said conduits extending above the lowermost portion of said container to a point below the level of liquid oil therein, means for cutting of! communication between the interior of the container and the inlet opening of,,the conduit'extending ,to the lower header, means for introducing 011 into said conduit from the exterior of the chamber below said closure means, means for withdrawing oil from said container, from a level below the tops of said conduits, means for distilling the duit at an intermediate portion thereof, separately removing and discharging a portion of vaporfrom said body of oil into said conduit'in a portion thereof under reduced pressure, and removing and separately cooling the vapors evolved from said enlarged chamber.

5. In apparatus for distilling hydrocarbon oils under pressure for the production oi lighter hydrocarbon oils of the character of gasoline, a

container; a plurality of inclined pipes below said container, headers at each end of said pipes, conduits connecting said headers with the interior of said container, said conduits extending above the lowermost portion of the container and having their tops below the intended liquid level therein a closure means for the conduit communicating with the lowermost header,- and a bell surmounting the conduit communicating with the uppermost header.

6. The method "of effecting the distillation of hydrocarbon oils under pressure for the production of low boiling hydrocarbon products such as gasoline which comprises maintaining a body of oil under pressure at conversion temperature, separately withdrawing evolved vapors from said body while maintaining them under pressure, passing said vapors directly to a fractionating operation, separately discharging liquid from said body of oil through a conduit of restricted crosssection into an enlarged chamber, reducing the pressure within said conduit at an intermediate portion thereof, withdrawing another portion of the evolved vapors from said oil body and passinglthem directly from said oil body into said conduit in the portion thereof under reduced pressure. 7. In apparatus-for distilling hydrocarbon oil under pressure for the production oi lighter hydrocarbon oils of the character of gasoline, a container, an elongated heated passageway, con- .duits extending from each end of/ said heated passageway into said container abovethe lowermost portion thereof, said conduits having their tops below the intended liquid level in said container, one of said conduits serving to conduct oil from said container to said heated passageway and the other oi said conduits serving to return 011 from the said heated pasageway to said container, a closure means for the said conduit for conducting oil to said heated passageway. and a body and passing them directly to a fractionatvaporized liquid oil from said low pressure distion of low boiling hydrocarbon products such as 5 gasoline which comprises maintaining a body of oil under pressure at conversion temperature, separately withdrawing, evolved vapors from said ing operation, separately withdrawing liquid from said oil body and discharging the same into a separate zone maintained under substantially lower pressure, and withdrawing another portion of the vapors evolved from said oil body and flowing them directly from said oil body into said low pressure zone in admixture with the said liquid flowing thereto from said oil body.

9. Themethod of efiecting the distillation of hydrocarbon oils under pressure for the production of lower boiling products which comprises maintaining in an enlarged chamber a body of oil under pressure at conversion temperature, separately removing evolved vapors from said enlarged chamber and subjecting them to fractionation to condense constituents thereof heavier than the desired low boiling products, withdrawing the fractionated vapors and condensing them, withdrawing the condensate. from said fractionating operation and passing it through a heated passageway to heat it to cracking temperature, discharging heated products from said passageway into said enlarged chamber, separately withdrawing liquid oil from said enlarged chamber and discharging it into a distilling zone maintained under a materially reduced pressure, withdrawing evolved vapors from said enlarged chamber and intimately contacting them with the liquid oil entering said low-pressure distilling zone, separately withdrawing un- 40 tilling zone and returning it directly to said enlarged-chamber, separately withdrawing evolved vapors from said low pressure distilling zone and passing them to a fractionating operation separate from the aforesaid first named fractionating operation, withdrawing condensate from the said second named independent fractionating operation and passing it through said heated passageway in admixture with the first named condensate.

'10. The method of effecting the distillation of hydrocarbon oils under pressure for the productionlof lower boiling products which comprises maintaining in an enlarged chamber a body of oil under pressure at conversion temperature, 55

separately removingevolved vapors from said enlarged chamber and subjecting them to fraction-f ation to condense constituents thereof heavier than the desired low boiling products, withdrawing the fractionated vapors and condensing 60 them, withdrawing the condensate from said fractionating operation and passirig it through a heated passageway to heat it to cracking temperature, discharging heated products from said passageway into said enlarged chamber, separately withdrawing liquid oil from said enlarged chamber and discharging it into a distilling zone maintained under a materiallyireduced pressure,

withdrawing evolved vapors from said enlarged chamber and intimately commingling them with the liquid oil entering said low pressure distilling zone, separately withdrawing unva'porized liquid oil from said low pressure distilling zone and returning it directly to said enlarged chamber, separately withdrawing evolved vapors from said liquid oil entering said low press re distilling low pressure distilling zone and passing them to a fractionating operation separate from the aforesaid first named fractionating operation, withdrawing condensatefrom the said second named independent fractionating operation and passing it through a heated passageway wherein it is heated to cracking temperature and thereafter discharging cracked products from the latter passagewayinto said enlarged chamber.

11. The method of effecting the distillation of hydrocarbon oils under pressure for the production of lower boiling products which comprises maintaining in an enlarged chamber a body of chamber and intimately contacting them with the v oil under pressure at conversion temperature, separately removing evolved vapors from said enlarged chamber and subjecting them to fractionation to condense constituents thereof heavier than the desired low boiling products, withdrawing the fractionated vapors and condensing thenr, withdrawing the condensate from said fractionating operation and passing it through a heated passageway to heat it to cracking temperature, discharging heated products from said passageway into said enlarged chamber, separately withdrawing liquid oil iromsaid enlarged chamber and discharging it into a distilling zone maintained under a materially reduced pressure,

withdrawing evolved vapors from said enlarged liquid oil entering said low-pressure distilling zone, separately withdrawing unvaporized liquid oil from said low pressure distilling zone and returning it directly to said enlarged chamber? separately withdrawing evolved vapors from said low pressure distilling zone and passing them to a fractionating operation separate from the aforesaid first named iractionating operation, introducing relatively cool fresh-oil into the latter fractionating operation and contacting the said fresh oil with the vapors therein to eflect frac- .ionation of the said vapors; withdrawing the resulting condensate-fresh oil mixture from the latter fractionating operation and contacting it twith the vapors undergoing fractionation in said first named fractionating operation. 12. The method of effecting the withdrawing the condensate from said fractionating operation and passing it through a heated passageway to heat it to cracking temperature, discharging heated products from said passageway into said enlarged chamber, separately withdrawing liquid oil from said enlarged chamber and discharging it into a distilling zone maintained under a materially reduced pressure, withdrawing evolved vapors from said enlarged chamber and intimately commingling th m with the zone, separately withdrawing unvaporized liquid oil from said low pressure distilling zone and returning it directly to said reaction zone, separately withdrawing evolved vapors from said low pressure distilling zone and passing them to a fractionating operation separate from the aforesaid first-named fractionating operation, withdrawing condensate from the said second named independent fractionating operation and distillation of hydrocarbon oils under pressure for the produccomprises passing the oil through a heating zone and heating the same therein to cracking tem perature under pressure, discharging the heated oil into a vapor separating zone and separating the same therein into vapors and residual oil, dividing the vapors into a first vapor stream and a second vapor stream, dephlegmating the first vapor stream and returning the resultant reflux condensate to the heating zone, finally condensing the dephlegmated vapors as a product of the process, removing the residual oil from the separating zone and flash distilling the sameby lowcring th pressure thereon, and passing said second v r stream directly from the separating zone into intimate contact with the residual oil undergoing flash distillation to assist the vaporization thereof. Y

14. In apparatus for distilling hydrocarbon oils under pressure for the production of lighter hyextending to the lower header, means for withdrawing liquid from the interior of said container,

means for distilling the withdrawn liquid, means for returning liquid unvaporized during such distillation directly to said container, and means for supplying oil to be treated within the conduit leading to the lower header and-at a point beyond said closure means.

15. In apparatus for distilling hydrocarbon oils under pressure for the production of lighter hydrocarbon oils of the character of gasoline, a container, a heating zone. a conduit for conveying oil from the container through the heating zone and back to the container, said conduit extending into the interior of said container, closure means for cutting of! communication between the container and the inlet end of said conduit, means for withdrawing liquid from said container, means for distilling such liquid, means for returning liquid unvaporized during such distillation directly to said container, means for withdrawing vapors from. the container and condensing portions thereof heavier thanthe desired gasoline product, and means for introducing the resulting condensate into the.conduit below said closure means and ahead of said heating zone.

16. In apparatus for distilling hydrocarbon oils under pressure for theproduction of lighter hydrocarbon oils of the character of gasoline, a container, a heating zone, a conduit for conveying oil from the container to the heating zone and back to the container, said conduit extending into the interior of said container, closure means for cutting oi! communication between the container and the inlet end of said conduit, means for with-J drawing liquid oil from said container, means for distilling such oil, means for returning liquid unvaporized during such distillation directly to said container, means for withdrawing vapors from the container, means for effecting heat exchange between the removed vapors and fresh oil, thereby condensing the portions of said vapors heavier than the desired gasoline products and heating said oil, and means for introducing the said heated oil and the condensate into the conduit below said closure means and ahead of said heating zone.

17. In apparatus for distilling hydrocarbon oils under pressure for the production of lighter hydrocarbon oils oi the character 01' gasoline, a container, a heating zone, a conduit for conveying oil from the container to the heating zone and back to the container, said conduit extending into the interior of said container, closure means for cutting of! communication between the container and the inlet end of the conduit, means for withdrawing liquid oil from said container, means for distilling such 011, means for returning liquid unvaporized during such distillation directly to said container, means for withdrawing vapors from the container, means for contacting'the vapors thus withdrawn with fresh oil, thereby condensing the portions of said vapors heavier thanthe desired gasoline products and heating the said oil,

I and means for introducing the said oil and condensate into the conduit below said'closure means and ahead of said heating "zone.

18. A method of effecting the distillation of hydrocarbon oils under pressure for the production of low boiling hydrocarbon products such as gasoline which comprises maintaining a body oi oil under pressure and at conversion temperature,

continuously flowing oil to be subjected to conversion conditions through a heating zone where- Patent No; 2,09 ,772,

It is hereby certified that error app CERTIFICATE OF CORRECTION.

OSWALD 'c. "BREWSTER, ET AL.

in it is brought to conversion temperature and into said body or oil, continuously and separately removing evolved vapors from said 011 body and.

perature under pressure, discharging the heated oil into a vapor separating zone and separating the same therein into vapors and residual oil, dividing the vapors into a first vapor stream and a second vapor stream, dephlegmating the first vaporstream to separate refluircondensate therefrom, finally condensing the dephlegmated vapors as a product of the process, removing residual oil irom the separating zone and vaporizing the same, and-passing said second vapor stream .di--

rectly from the separating zone into intimate contact with the residual oil undergoing vaporization to'assist in the vaporization thereof.

OBWALD C. BREWSTER. .MAX G. PAULUS.

ANDREW E; 'I'I-IOMPSON.

Notem er' 9 7 ears in the printed specification of the above numbered patent requiring correction as fol lows Page 5 first column, line 69', "claim 12, for the words "reaction zone" her; and that the said Letters Patent should be read wit read enlarged cha nn this correction therein that the same may conform toethe record of them ase" in the Patent 1 Office. J

Signed and, sealed this 25th, day of January, 1 958 (seal):

Henry Arsdale Acting Commissioner of Patents.

than the desired gasoline products and heating said oil, and means for introducing the said heated oil and the condensate into the conduit below said closure means and ahead of said heating zone.

17. In apparatus for distilling hydrocarbon oils under pressure for the production of lighter hydrocarbon oils oi the character 01' gasoline, a container, a heating zone, a conduit for conveying oil from the container to the heating zone and back to the container, said conduit extending into the interior of said container, closure means for cutting of! communication between the container and the inlet end of the conduit, means for withdrawing liquid oil from said container, means for distilling such 011, means for returning liquid unvaporized during such distillation directly to said container, means for withdrawing vapors from the container, means for contacting'the vapors thus withdrawn with fresh oil, thereby condensing the portions of said vapors heavier thanthe desired gasoline products and heating the said oil,

I and means for introducing the said oil and condensate into the conduit below said'closure means and ahead of said heating "zone.

18. A method of effecting the distillation of hydrocarbon oils under pressure for the production of low boiling hydrocarbon products such as gasoline which comprises maintaining a body oi oil under pressure and at conversion temperature,

continuously flowing oil to be subjected to conversion conditions through a heating zone where- Patent No; 2,09 ,772,

It is hereby certified that error app CERTIFICATE OF CORRECTION.

OSWALD 'c. "BREWSTER, ET AL.

in it is brought to conversion temperature and into said body or oil, continuously and separately removing evolved vapors from said 011 body and.

perature under pressure, discharging the heated oil into a vapor separating zone and separating the same therein into vapors and residual oil, dividing the vapors into a first vapor stream and a second vapor stream, dephlegmating the first vaporstream to separate refluircondensate therefrom, finally condensing the dephlegmated vapors as a product of the process, removing residual oil irom the separating zone and vaporizing the same, and-passing said second vapor stream .di--

rectly from the separating zone into intimate contact with the residual oil undergoing vaporization to'assist in the vaporization thereof.

OBWALD C. BREWSTER. .MAX G. PAULUS.

ANDREW E; 'I'I-IOMPSON.

Notem er' 9 7 ears in the printed specification of the above numbered patent requiring correction as fol lows Page 5 first column, line 69', "claim 12, for the words "reaction zone" her; and that the said Letters Patent should be read wit read enlarged cha nn this correction therein that the same may conform toethe record of them ase" in the Patent 1 Office. J

Signed and, sealed this 25th, day of January, 1 958 (seal):

Henry Arsdale Acting Commissioner of Patents.

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