US1830963A

US1830963A - Distilling petroleum residuum

Info

Publication number: US1830963A
Application number: US625742A
Authority: US
Inventors: Francis M Rogers; Claude P Mcneil
Original assignee: Standard Oil Co
Current assignee: Standard Oil Co
Priority date: 1923-03-17
Filing date: 1923-03-17
Publication date: 1931-11-10
Anticipated expiration: 1948-11-10

Description

Nov. 1.0, 1931. F. M. ROGERS ET AL 1,830,963

DISTILLING PETROLEUM RESIDUUM Filed Marqh 17, 1923 Patented Non. l0, lg3d UNITED. STATES PATENT OFFICE FRANCIS M. ROGERS AND CLAUDE P. MQNEIL, OF WRITING, INDIANA, ASSIGNORS TO STANDARD OIL COMPANY, OF vWHITIN' G, INDIANA, A CORPORATION OF INDIANA DISTILLING- PETROLEUM RESIDUUM Application led March 17, 1923. Serial No. 625,742.

This invention relates to the production of` useful hydrocarbon oil products from heavy residual pitches derived, for example, by the steam distillation of crude petroleum 011s.

The present invention is particularly useful in the handling of the heavy pitch residues resulting from a continuous steam distillation of crude or reduced crude oils to bottoms corresponding, for example, to about 15% or less than 15 per cent on oils of the character of mid-continent crude oil. Such residues are normally exceedingly viscous or solid at ordinary temperatures, have a iash point above 500 F., and their further decomposition by destructive distillation is attended With many ractical difficulties. In the specific embodlment of this invention hereinafter fully disclosed, the coking or dry distillation of such residues is effectively and economically accomplished by a continuous process. The invention will be more fullyv understood by reference to the accompanying drawingin which is shown somewhat diagrammatically and partly in section, apparatus suitable for carrying the invention into effect. n

Referring more particularly to the drawing, the numeral 5 indicates an oil preheater and the numeral 6, a steam superheater. The' residue to be treated is forced from a supply tank (not shown) through pipe 7 to the preheater, and from the preheater through pipe 8 to the inner tube of an atomizing nozzle 9, the body of which extends through a combustion chamber l0. Superheated steam passes from the superheater 6 through the plpe 11 to the outer concentric tube of the atomizer 9. The combustion chamber 10is heated by a suitable means, for example, a gas burner 12a, shown in end elevation, and supplied with fuel gas and air through

pipes

12 and 13 respectively.

The combustion chamber 10 opens into an enlarged chamberYV '15 which serves both as a reaction chamber and as a settling chamber for separating out coke or other solid matter. The atomizing nozzle 9 is s'o disposed as to direct the atomized mixture of heavy residuum and steam directly into this chamber. Products not deposited in the chamber 15,

heated steam through pass out through the vapor pipe 16, a baile 17, forcing a circuitous flow of the products through the chamber 15, before entering the outlet. ACondensate or entrained liquids deposited in the vapor outlet 16, may be removed through the draw-olf pipe 18, for example, for examination or testing. Products passing off through the vapor outlet 16, are drawn off through pipe 19 and pass through a suitable condenser 20, which may be Water cooled if desired. From the condenser 20, the products pass into a riser or gas separator 21, condensates passing out through pipe 22, and exhaust gases being withdrawn from the top.

In carrying out the process, it has been found convenient to control the heating of the combustion chamber 10 by the temperature conditions desired in the chamber 15, in which the distillation process appears to take place.` It has been found that satisfactory yields of distillation products may be obtained when the temperature Within the main portion of the reaction chamber 15 is perature reading being taken near the inlet lto the chamber from the combustion chamber 10 and indicating approximately the temperature of the atomized mixture after entering the chamber 15. The oil may suitably be preheated in the preheater 5 to temperatures of 500 to 700 F. i

In beginning the operation of the apparatus, steam is forced through both the inner and outer tubes ofthe atomizer 9 while the combustion chamber is being heated, an excessively high temperature of the parts being thereby avoided. When the desired temperature hasbeen reached, as'indicated by tempera-ture readings in the reaction chamber `-15 as indicated, the heavy residuum, previheater 5, is introduced into the inner tube of the atomizing nozzle, the passage of superthe outer tube being continued. The heavy residuum is very finely dispersed or atomized and the mixed residuum and steam enter the chamber 15. In passing through the combustion chamber the oil is protected by the surrounding jacket of steam, and does not attain cracking temperature until it enters the reaction chamber and is admixed with the highly heated steam. rlhe temperature readings taken therein are a reasonably accurate measure of the temperature imparted to the finely divided residual oil. By reason of the Hnely divided condition of the residuum, its distillation is very rapid and is materially aided by the superheated steam present which acts as an inert gas. The greater part or substantially all of the coke formed as a result of its distillation, and which is in very finely divided form, separates out in the chamber and may be drawn off through the outlet 24. The chamber 15 is shown in a very simple form, it being clear that its construction may be suitably modified, in accordance with the usual dust separator practice, to facilitate the deposition of the fine particles of coke. The vaporized portions pass out through the vapor line 16 and the entire body of vapor products, including any condensate formed in the vapor line, may, if desired, be passed through the condenser 20.

Where separation of entra-ined liquid or of liquid condensed in the line 16 is desired, it may be effected through the line 18. Liquid products issuing from the condenser 2O pass into the receiver 23, suitable means being provided for the escape of gas as already described.

The following example illustrates the carrying out of the present invention. The residuum handle was at 14 B. Mid-continent crude residuum having a Hash point of about 525 F. The oil was preheated to a temperature of about 600 F. and then passed through the atomizing nozzle and atomized with super-heated steam into the chamber 15. The combustion chamber was heated to produce a temperature of 1,000 to 1,100 degrees F. in the chamber 15, the temperature being measured in the manner already indicated, so thatl it represented approXimatelv the temperature to which the atomized oil vv'as heated. The yield of liquid distillate products Was about 60 to 65 per cent, having a viscositv of about 128 Saybolt at 210o F. and a Baum gravity of 18 to 20. The distillate product began to boil at 5,80 to 400, and showed approximately 80% ofi' at 750 F. (The ranges of percentages and temperatures given, indicate average results obtained from a number of runs).

Although the present invention has been described in connection with the specific details of a processv carrying it into effect, it is not intended that these details, shall be regarded as limitations upon the scope of lthe process, except in so far, as included in the accompanying claims.

What We claim as new and desire to secure by Letters Patent, is:

1. The method of distilling to coke a heavy crude oil residuum having a Hash point above 500 F. which consists in continuously Howing such residuum in a stream through a heated zone, surrounding the strength of residuum in the heated zone with a confined body of inert gas, Hnely subdividing the residuum in a reaction zone immediately after passing through the heated zone, andsupplying heat to the residuum after subdividing to bring the temperature of the subdivided residuum in the reactiony zone to 800 to 1200 F., thereby substantially distilling the latter to coke.

2. The method of distilling to coke a heavy crude oil residuum having a Hash point above 500O F. which consists in continuously HOW- in g such residuum in a stream through a heated zone, surrounding the stream of residuum in the heated zone with a confined body of inert gas, finely subdividing the residuum in a reaction zone immediately after passing through the heated zone, and supplying heat to the residuum after subdividing to bring Athe temperature of the subdivided residuum in the reaction zone to 800o to 1200 F., thereby substantially distilling the latter to coke, and separating the resulting coke and distillate products.

3. The method of distilling to coke a heavy crude oil residuum having a Hash point above 500 F. which consists in continuously Howing such residuum in a stream through a zone of hot combustion gases, surrounding the stream of residuum in the zone of hot combustion gases with a confined layer of inert gas, atomizing the residuum immediately ater passing through the heated zone, and projecting the atomized residuum and inert gas into a reaction zone While surrounding the atomized residuum and inert gas With combustion gases introduced into the reaction zone from the combustion gas zone whereby the subdivided residue is brought to 800 to 1200 F. thereby substantially distilling the latter to coke.

4. The method of distilling to coke a heavy crude oil residuum having a Hash point above 500 F. which consists in continuously Howing such residuum in a stream through a zone of hot combustion gases, surrounding the stream of residuum in the heated zone of hot combustion gases With a confined body of eX- traneous inert gas, atomizing the residuum immediately after passing through the heated zone, intermingling the atomized residuum and inert gas with combustion gases from the heated zone whereby the subdivided oil is heated to 800 to 1200 F. and distilled to coke. and separating the resulting coke and distillate products.

5. The method of distilling to coke a heavy crude oil residuum having a Hash point above 500 F. which consists in continuously Howing such residuum in a stream through a zone of hot combustion gases, surrounding the stream of residuum Howing through the zone of combustion gases with a confined body of extraneous inert gas, discharging the residuum in finely subdivided form into a reaction zone together with the extraneous inert gas While introducing combustion gases from the combustion zone into the reaction chamber.

6. The method of distilling to coke a heavy crude oil residuum having a flash point above 500 F. which consists in continuously flowing such residuum in a stream through a zone of hot combustion gases, surrounding the stream of residuum flowing through the zone of combustion gases With a confined body of extraneous inert gas. discharging the residuum in finely subdivided form into a reaction Zone together With the extraneous inert gas While introducingr combustion gases from the combustion zone into the reaction lchamber at a point adjacent the point at which the residuum and inert duced.

7 In apparatus for the distillation to coke of heavy crude oil residuum, a combustion chamber, a separating chamber, a conduit passing through vthe combustion chamber and opening into the separating chamber for supplying residuum into the latter, and a second conduit passing through the combustion chamber and opening into the separating chamber for supplying an inert gas into the latter, said second conduit surrounding a portion of the first named residuum conduit.

8. In apparatus for the distillation to coke of heavy crude oil residuum, a combustion chamber, a separating chamber, a conduit passing through the combustion chamber and opening into the separating chamber for supplying residuum into the latter, a second conduit passing through the combustion chamber and opening into the separating chamber for supplying an inert gas into the latter, said second conduit surrounding a portion of the first named residuum conduit, and means for introducing combustion gases from the combustion chamber into the separating chamber at a point adjacent the outlets of the residuum and inert gas conduits.

FRANCIS M. ROGERS. CLAUDE P. MCNEIL.

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