US2312719A

US2312719A - Cracking process

Info

Publication number: US2312719A
Application number: US238138A
Authority: US
Inventors: Paul E Kuhl
Original assignee: Standard Oil Development Co
Current assignee: Standard Oil Development Co
Priority date: 1938-11-01
Filing date: 1938-11-01
Publication date: 1943-03-02
Anticipated expiration: 1960-03-02

Description

March 2, 1943. A P'. E, KUH!. v A e2312,719

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R lo y A @Yaocwklou GAS A mls] an /Mezr CTAS ('HAMBER 1 0R V4PR- INLET gas I Patented Mar. 2, 1943 UNITED `STATES r CRACKING PROCESS Paul E. Kuhl, Madison, N. J., assignor to Standard Oil Development Company, a corporation of Delaware Application November 1, 1938-, Serial No. 238,138

2 Claims.

The present invention relates to the conversion of relatively high boiling petroleum hydrocarbons int-o relatively low boiling petroleum hydrocarbons. The invention is particularly directed to a method and apparatus of securing in a commercial operation temperatures higher than have previously been secured and is also directed to a method of avoiding deleterious coke formations. The invention is directed to the use of tubular porous linings in the heating tubes and in the reaction chamber of petroleum cracking equipment.

It is well known in the art to convert relatively high boiling petroleum hydrocarbons into more desirable products of relatively lower boiling range. In these processes, the feed material is subjected to Various temperatures and pressure conditions for various time periods which are usually measured in terms of yield per unit throughput, hereinafter termed conversion per pass. These various variable factors are optimumly adjusted to secure the desired yield and depend upon the particular feed material being treated, as well as upon the yields and quality of products desired. In these processes, it has been found that when processing heavy feed stocks such as reduced crude, the ultimate yield of gasoline can be substantially increased by increasing the conversion per pass. A gasoline of higher octane number is also secured. However, it has not been possible to increase the conversion per pass to any substantial extent, due to the fact that as conversion per pass increases an increased amount of coke formation occurs, necessitating closing down the equipment for cleaning. The formation of coke usually occurs upon the surfaces of the reaction chambers and in the tubes in which the petroleum oil is raised to cracking temperatures. Various attempts have been made to rectify these conditions, as for example, by operating in the so-called up-fow manner in which the reaction products ow upwardly through the reaction chamber or soaking drum. These methods have not been entirelyl successful in eliminating coke formations and, as pointed out above, this factor limits the extent to which the conversion per pass may be raised, and also the extent to which the temperature of the oil may be raised by indirect heating. Thus the disadvantages of these limita- Y not in contact with metallic surfaces.

tions may be readily understood when it is confsidered that higher yields and a more economical operation are secured by cracking hydrocarbons at temperatures in excess of those which can now be tolerated when heating indirectly as is the present practice. Thev process of my invention overcomes these difdculties and carries out a cracking operation at temperatures in excess of those now permitted. By the present process it is also possible to substantially increase the con,- Version per pass and thus substantially increase the ultimate yield of gasoline. 4

The process comprises subjecting petroleum hydrocarbons to suitable cracking conditions in a manner that the petroleum hydrocarbons are In accordance with the present processpetroleum hydrocarbons are passed througha porous lining disposed within a metallic shell. Sufficient pressure is maintained in the area between the metallic shell and the porous lining to force an inert gas or an oxygen-containing gas through said lining thereby maintaining between the petroleum hydrocarbons and the porous lining sub; stantially a gaseous wall. By operating in the present manner, it is possible to further increase the temperatures of the hydrocarbons by in, jecting an oxygen-containing gas into the same, thus raising their'temperature by Vdirect heating. It is also possible to prevent undue cokeforma tion, as for example, in the soaking drum, by forcing an inert gas throughr the,` porous lining in order to maintain'a gaseous wall between the petroleum hydrocarbons and the drum; L

The invention may be readily understood by reference to the attached drawings showing modifications of the same. Figure 1 showsua diagrammatical flow plan of a normal cracking operation. Figure 2 isa sketch demonstrating a suitable construction .ora tube to be employed, while Figure 3 shows a satisfactory construction of a soaking drum within the scope of the pres# ent invention.

Referring specifically to the drawings, Figure 1 is a diagrammatical ow plan of a typical crackf AF. In this operation fresh feed is introduced by means of feed line I vintothe bottom of-'prirnary bubble tower 2. The feed together with cycle oil is withdrawn from the bottom of primary bubble tower 2 and introduced into furnace 4 by means of line 3. Furnace 4 is so designed so as to secure optimum heat transfer as the feed stock flows through tubes in the sections and to bring the oil up to cracking temperatures. The total feed is led from furnace 4 through line 5 into soaking drum or reaction chamber 6 which permits additional time under cracking conditions. The oil is withdrawn from reaction drum 6 through line 1 and the pressure reduced by valve 8. The cracked products pass into evaporator 9 from the bottom of which tar or fuel oil of the desired gravity is removed. The vapors pass overhead from evaporator 9 through line I0 into primary bubble tower 2. Cycle stock accumulates in the bottom of primary bubble tower 2 and vapors pass overhead through line II into a secondary bubble tower |21. at the top of tower I2 is controlled so as to pro--v duce an overhead distillate of the desired end point which is removed by line I3 and condensed in cooler I4. The gas is separated from the distillate in distillate drum l5 and removed by means of line I1. The distillate is removed by means of line I 6. Heating -oil may be withdrawn from the bottom of tower I2 through line I8 and may be .recycled if desired through line I9 or withdrawn through line 20.

Figure 2 is a detailed drawing of line or tube 5. It is to be understood that any number of tubes may be employed in any manner desirable, as for example, in order to secure parallel or parallel series ow. The tube consists of a main .tube wall 2| and an inner tube 22. Inner tube 22 is pervious to gases. The exit products from the vfurnace after being heated to the optimum temperature by any of the conventional methods are then passed longitudinally through the inner ,tube 22. Oxygen containing gas is introduced into the area 23 between the tube walls 2| and 22 and between baiiles 24 and 25 by means of gas inlet 26. Sufficient pressure is maintained in the area 23 to cause the gas in this area to flow at the `optimum rate into the inner tube 22. If desirable, inert gas may be introduced into area 2.1 between the tube walls 2| and 22 and baffles 25 and 28 by means of inlet 29.

Figure 3 describes in detail reaction chamber i `or soaking drum 6. This drum consists of an `Suter wall 3u and an inner Wall 3|. The oil is introduced into the reaction drum 6 by means of line 33 and withdrawn by means of line 32. The inner wall 3| is Vpervious to gases. Hydrocarbon gas, inert gas or oxygen-containing gas is introduced into area 34 between

walls

33 and 3| and .baifles 35 Vand 36 by means of line 3l. Oxygen containinggas is introduced into area 4I `between

walls

30 and 3| and

baflies

39 and 42 by means ,of line 43. In a similar manner a suitable inert or .oxygen-containing' gas may be introduced into .area 38 by means of line 4u. Itis understood that ,inertgaa hydrocarbon gas or oxygen-containing -gas may be employed depending upon whether it is desired to simply prevent coking or also vto raise the temperature by direct oxidation of a part of the hydrocarbons.

The process of the present invention pre-heats a feed oil to its maximum, temperature now permitted by indirect heating methods, as for example. in heating coil 4. The oil is then withdrawn at this temperature and introduced into tube 22. Oxygen-containing gas is introduced .into section 23 by vmeans .of line 2S and main- The temperaturev tained at a suiciently high pressure so as to force the gas into tube 22, thus securing internal combustion and raising the temperature considerably above the temperature previously-secured by indirect heating. Inert gas is introduced into area 21 by means of line 2i) and maintained at a sufcient pressure so as to cause the gas to flow through the pervious tube walls 22 and maintain a gas lining along the side walls, thus preventing undesirable and deleterious coke formation. In a similar manner the oil is introduced into soaking drum 6 into which inert gas is maintained between the pervious wall 3| and the outer wall 30. Suiicient pressure is maintained in the

respective areas

34, 38, and 4| to overcome the to iiow through the pervious wall, thereby mainltaining a gas lining between the hydrocarbon products and the wall, thus preventing coke formation. The tubes and reaction chamber of the present invention are preferably used together.

However either the tube or the reaction chamber may be employed in the absence of the other.

The amount of oxygen-containing gas introduced into the pervious tube will at least be suflicient to prevent a temperature drop between the heating coil and the soaking drum. In general, sufficient oxygen-containing gas is introduced to raise the temperature of the oil from about 10 F. to F. Itis preferred to introduce sufficient oxygen-containing gas to raise the temperature of the oil at least 30 above the temperature at which it is withdrawn from the heating coil.

In order to further illustrate the invention, the following examples are given which'should not be construed to restrict the same in any manner whatsoever.

Eample 1 Gas oil boiling in the range from 400 F. to 700 is heated to about 650 F. to 700 F. as it enters the furnace. The feed material passes through the furnace in which it is heated to a temperature of about 915 F. to 925 F. After leaving the heater the total feed enters the reaction chamber or soaking drum which is main- .tained at a pressure of from 650 lbs. to 350 lbs. per square inch. The oil is released from the bottom of this reaction chamber into an evaporator which is maintained at about lbs. pressure and at about 785 F. to 800 F. Part of the feed material which enters the evaporator remains in the liquid state and is withdrawn from the unit as cracking coil tar which has a gravity of about 9 to 10 A. P. I. The vapors leave the top of the evaporator at about 765 F. and ow through suitable heat exchange equipment and then pass into the primary tower where the heavier fractions condense and drop into the accumulator section at'the bottom of the tower to form part of the total feed. The temperature of the vapors leaving the top of the primary tower is maintained at about 525 F. to 550 F. .These vapors pass into the secondary tower where heavier fractions condense to form a light cycle stock. The lighter boiling fractions having an -end point of 400 F. are taken overhead.

The temperature of the total feed leaving the furnace and the temperature maintained in the reaction chamber were limited by the fact that if higher temperatures were employed or if the conversion per pass were increased, undue coke formation would occur. By carrying out` the above process in accordance with the present invention, it is possible to increase the temperature of reaction from about 920 F. to 940 F., and to increase the conversion per pass from about 28% to 32% and thus to increase the yield of gasoline from about 7000 gallons per hour to 8000 gallons per hour.

The improved results secured when cracking gas oil and operating in accordance with the present invention may be summarized as follows:

lal Temperaoperation gltee temp y limited use. by coke pervious formations gs Temperature F- 920 940 Total feed converted to gas per cent.. 28 32 Ultimate yield gasoline .do 63 61. 5 Gasoline gallons per hour.. 7000 8000 O. N. gasoline 7l. 0 72. 5

Reduced crude Temperanormal ture peroperation mitted by temp. use of limited parviens by coke linings formation Temperatura.;` --F...- 890 920 Total feed converted to gasoline.-per cent.. 1l. 5 20 Ultimate yield gasoline -.do 26. 5 29. 5 Gasoline gallons/hour-- 2880 5000 O. N. gasoline 65. 5 0

From the above data it may be seen yields were increased by approximately 75% and the octane number of the product was higher.

Conditions and methods of ow may be widely varied in the process of my invention. Temperatures and pressures may be varied to secure optimum cracking results. For example, the soaker may be either upowing or downlowing and tube 5 may be either a single tube or may be a series of tubes in parallel.

If relatively low temperatures are desired, it may be desirable .to employ merely the lined soaking drum and to dispense with the lined heating tubes. It also may be desirable to employ the lined heating tubes in the absence of the soaking drum of the present invention. The particular construction of the soaking drum and heating tubes may also be varied widely. It is, of course, necessary to employ a complete lining which is preferably similar to the construction of the tube or soaking drum. The area in which the inert gases or oxygen-containing gases are injected may be' any optimum volume with regard to cost of construction and desirable strength of the equipment The process of my invention is not to be limited by any theories or mode of operation, but only by the following claims in which it is intended to claim all novelty insofar as the prior art permits.

I claim:

1. Process of thermal cracking petroleum hydrocarbons, comprising raising said hydrocarbons to cracking conditions by passing the same through non-porous metallic tubes in a furnace, removing the petroleum hydrocarbons from said furnace and passing the same longitudinally through a porous lining situated within a nonporous metallic tube, maintaining an oxygen-containing gas between said non-porous metallic tube and the porous lining under suicient pressure to force said gas through the porous lining into the petroleum hydrocarbons thereby raising the temperature of the same, withdrawing the hydrocarbons and passing the same through a porous lining situated lwithin a non-porous metallic drum in which 'an inert gas is maintained within the area between the non-porous metallic drum and the porous lining of said non-porous metallic drum under suiioient pressure to force said inert gas through the porous lining, thereby maintaining an inert gas wall between said petroleum hydrocarbons and said porous lining.

2. Process in accordance with claim 1 in which suicient oxygen is introduced into the porous lining .to raise the temperature of the oil from 10 F. to 50 F.

PAUL E. KUHL.