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Publication numberUS2905731 A
Publication typeGrant
Publication dateSep 22, 1959
Filing dateJul 25, 1955
Priority dateJul 25, 1955
Publication numberUS 2905731 A, US 2905731A, US-A-2905731, US2905731 A, US2905731A
InventorsKenneth W Seed
Original AssigneePhillips Petroleum Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Hydrocarbon conversion method
US 2905731 A
Abstract  available in
Images(1)
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Claims  available in
Description  (OCR text may contain errors)

2,905,731 I I HYDROCARBON CONVERSION METHOD.

Kenneth W. Seed, Bartlesville, Okla assigniir to Phillips This invention relates to the conversion of hydrocar- States Patent bons. It also relates to a combination apparatus for effeoting conversion of hydrocarbons. In one of its aspects,

the invention relates to a method in which hotgases or products of combustion are forced into a venturi in which the gases are admixed with distillate aspirated by said venturi from a distillation zone.

a venturi and a distillation zone so arranged and adapted that combustion gases produced in said combustion zone can be fed to the venturi rendering the same operative to aspirate distillate from the distillation zone into the said venturi for a controlled reaction time at a controlled temperature following which there can be effected a controlled quench. In another of its aspects, the invention relates to apparatus adapted to carry out the various modus operandi set forth and described herein, the said apparatus being so combinedand proportioned as (0 Permit flexible, yet simultaneous, conversion of, say, a hydrocarbon gas and a hydrocarbon oil to useful products, the said apparatus in one embodiment consisting essentially of a pressure combustion chamber communicating with a venturi, a vacuum drum communicating with the throat of the venturi and a quench vessel communicating with the discharge of the said venturi.

In the refining of petroleum, a reduced crude or heavy In another aspect the I zone, preferably'operated at a reduced pressure, the vapors being cracked by a controlled time-temperature reaction broughtabout by use of hot combustion gases obtained from a combustion zone, akin to a rocket or jet engine, operated under pressure, by feeding said gases into and through a venturi to which are aspirated by its action the said vapors from the said distillation zone.

Thus, according to the present invention, there is pro,- vided a modus operandi for the conversion of a hydrocarbon vapor, produced by distillation of a hydrocarbon oil, preferably under a reduced pressure, which comprises feeding hot gases at a temperature and in quantity sufficient to crack a hydrocarbon oil vapor into a venturi, feeding a hydrocarbon vapor also into said venturi for admixture therein with said hot combustion gases, and, in said venturi transferring heat from said hot gases tosaid hydrocarbon vapor to convert the same to an extent desired-by a controlled time-temperature reaction. lnthe now preferred form of the invention, the reacted-gas mixture is immediately quenched to a temperature at .1 which no substantial undesirable degradation or other invention relates to a combination of a combustion zone,

residual oil, that is, a crude oil from which propane, butane, gasoline, kerosene, and light and heavy gas oils have been removed, is vacuum flashed to remove vacuum distillate. This fraction makes a suitable stock for cracking,

and if subjected to high temperatures, can be used as a chamber such as a rocket or jet engine firing into the throat of the venturi, the discharge tube of which is equipped with a quench and the throat of which is connected to a vacuum drum, substantially as set forth and described in connection with the drawing. Figure 1 shows diagrammatically an embodiment of the invention ask is applied tothe cracking of a heavy residual oil vacuum distillate employing hotcombustion gases. Figure 2 shows details of the venturi apparatus shown in Figure 1. j

Referring now to Figure l, a chargeoil is fed by way of conduit 1, by means of pump 2, into vacuum drum. 3,.

Vaporsgenerated in the vacuum drum are aspiratedby i is quenched in quench vessel 8 bymeans of waterintroduced through manifold 9 and spray heads 10. In quench vessel 8, the temperature is lowered rapidly, almost imme-. diately, to a level at which no undesirable reaction can take place. The quenched products are thenpassed by I way of conduit 11 into a second quench vessel 12 to which ene and ethylene. It is another object of this invention to employ hot combustion gases for the controlled time.- temperature reaction of a hydrocarbon distillate oil to produce useful products including at least one of acetyl ene and ethylene.

A further object of this invention is the provision of apparatus so constructed and arranged .asto: provide for the production of hot gases, preferably under elevated pressure, which can be employed to cause the conversion of a hydrocarbon oil distillate produced with the assistance of the said hot combustion gases.

Other aspects, objects, as well as. advantages of the invention are apparent from a study of this disclosure, the drawing, and the appended claim.

The invention is particularly applicable to the cracking is pumped a portion of the charge from conduit 1 by way of conduit 13, pump 14, conduit -15, and spray heads 16. In quench vessel 12-, liquid products which are obtained by condensation, admixed with the quench medium, are passed by way of conduit .17 into knockout drum 18 in which a phase separation takes place. .The upper hydroe carbon-phase is passed by way of conduit 19, pump. 20, and conduit 21 into the vacuum drum 3. Vaporous material which is disengaged from the liquid collectingin knockout drum 1-8 is passed by way of pipe'22into con duit 23 in which said vaporous material is admixed with the'mai'n stream of vapors coming from quench zone-16'. The combined vaporous materials are pumped by pump or blower 24 into discharge conduit 25 and from there to gas purification means, not shown. The aqueous phase collected in knockout drum 18 is discarded through con} duit 26. The portion of charge 1 unvaporized in vacuum drum, 3. is discarded through conduit 27. Y

Figure 2 is a diagrammatic cross-sectional view showing details ofa suitable venturi apparatus 6 for carrying out of hydrocarbon oil vapors obtained from a distillation this invention. Combustiongases from combustion zone hr "a '7 through conduit 28 to a nozzle, comprising converging section '29, throat 30 and diverging section 31, which communicates with chamber 32 in which vapors from conduit 4 are mixed and entrained with the combustion gases. Downstream of chamber 32 is a difiusen'comprisingconverging section 33, throat 5' and divergingsection '34. The gasespass through conduit 35 to quench zone "8, Depending upon the hot gases supplied to venturi throat Sand the character of the oil and the distillation of it which is carried out in vacuum drum 3as well as upon the conditions which are maintainedin discharge 6 of theventuri and in quench zone 8, the products whichresuit and which are'discharged by way of conduit-25 will befofvarying character as'willbe understood by-one skilled in the art having'studied'this disclosure; Thus, any fuel'can be usedto supply the hot combustion gases in engine 7. For example, therecan be employed gases resultingfrom-fuel's suchas hydrogen,'-natural gas, other hydrocarbons such as butane or even liquid hydrocarbons such as -kerosenes,'etc. .Also, oxidizing agents such as air, 'e nriched'air, 'or' even oxygen can be used. Further, liquid oxidizing agents as nitric acid or hydrogen peroxide can also be used in the combustion zone or chamber.

Also, as a specific variation within the scope of the claims to this invention, the high pressure combustion zone can'rbe one in which a desirable oil fraction such as an aromatic oil is burned under carbon black producing conditions to produce carbon black contained in comventuri. a r Thus, the invention is applicable to any combination operation wherein a high temperature, high velocity combustiongas steam is used as a source of heat for a thermal operation such as cracking, the said stream, according to the invention, being also a means for creating a vacuum whereby the stock for conversion or cracking is introduced into the hot gases. 1 The high pressure combustion zone can be operated at anypressure which is sufficient to provide for'aspiration into the venturi throat of the vapors from the distillation zone. Preferably, the pressure in the combustion zone will be above atmospheric. The greater the ratio of the pressure in the chamber to that prevailing in the vacuum drum, the greater will be the coolingin the expansion in the venturi discharge. Further, the greater the pressure ratio, the smaller will be the amount'of gas which must be expanded to compress the vapors coming from the vacuum drum to a pressure sutficient to discharge the bastion gases under pressure'sufiicient to operate; the

. 4- 5 drum under a vacuum. However, a vacuum is preferred and usually a pressure of from 1 to about 5 pounds per square inch absolute in thevacuum drum is considered satisfactory. Though not shown in the drawing, the feed to the vacuum drum, especially when it is a well-reduced crude, will be heated. Suitable heating means (not shown) are provided in the vacuum drum to bring about the desired distillation therein.

The..timei-taken.,forthecracking of the .oil vapors in the venturi discharge .is. of the order of a fraction of a second. cracking is eifiected with contact times of frori'1 about"0.005 to about 0.1 second. The temperature as 'rioted isratherihighanda water quench, as shown in the drawing, located immediately downstream of the venturi dischargejfdiices the temperature of the mixture and arrests the reaction. The following is an example according to the invention in which a specific high methane content natural gas is burned to produce gases with which a reduced crude is cracked.

. I Example I Ahigh methane content natural gas with the following analysis is burned with the theoretical amount of air.

- 96.0 co, 3.2 N, 0.8

A-fiow rate of 100 standard cubic feet of natural gas per minute-feeds the combustion chamber at 100 psi. Nine hundred twenty standard cubic feet of air per minute is used. Upon combustion, the mixture attains a temperature of 3650 F.

The hot combustion gases expand through a converging-diverging nozzle to a pressure of 4 p.s.i.a., the pressuremaintained in the vacuum drum. The nozzle is constructed with a 50 angle of convergence to a throat of same through the venturi. It WiILbe-understood by one skilled in the art in possession of this disclosure that the high temperature combustion gases are expanded through a converging-diverging nozzle to supersonic speeds. These gases entrain the vapors from the vacuum drum and compress them from drum pressure to discharge pressure-in a second, and larger, converging-diverging nozzle.

. In one embodiment of the invention, the combustion chamber is a reaction zone in which a high temperature cracking can be elfected. For example, methane is partially oxidized with oxygen to acetylene at a high temperature, say, in the range 3000 to 5000 degrees F The pressure ratio in the expansion through the convergingdiverging nozzle is adjusted to lower the temperature, upon expansion, to one in the range of 1500 to 2000 degrees F. which is then suitable for cracking vapors frompurpose.

about'Z inches in diameter with a 15 angle of divergence downstream. A ratio of nozzle discharge area to nozzle throat area of about 4 to 1 exists. The nozzle discharge velocity is about 5700 feet per second. The combustion chamber exhaust gas composition is approximately as follows:

M01 percent CO 18.9 H O 9.6 N: t 71.5

,R'cduced crude with an API gravity of 25.0and an ASTM Initial Boiling Point of 320 F. is fed to the vacuum drum after being used as secondary quench for the process off-gases. The vacuum drum is maintained at a pressure of 4 p.s.i.a. and a temperature of about 525 F. Coil heaters are used to maintain the drum temperature. External heaters can also be used for this Vapors from the vacuum drum are entrained by the high velocity combustion gases and cracked. The vacuum drum vapors have the following characterisn'cs (liquid);

Gravity, API. Sulfur, weight percent 0.266 Refractive index 1.4633 ASTM distillation:

IBP 280 20% 526 40% 562 60% 606 662 Cracking is carried out at about 1800 F. and the mixture of gases passes to theconvergingdiverging diffuser where it is compressed from drum pressure (4 p.s.i.a.) to discharge pressure, 16 p.s.i.a. A reaction time of 0.069 second (i.e., of the order of less than $5 second) is maintained by proper sizing of the diffuser and the soaking chamber downstream. A Water quench cools the gases to a temperature below that at which any reaction can take place and final cooling is brought about by using the reduced crude feed to the vacuum drum.

Using the quantity of natural gas specified at the beginning of the example (100 SCFM), 1500 pounds per hour of vapors are withdrawn from the vacuum drum.

In the difiuser, the ratio of inlet area to throat area is about 1.4 to 1. A difiuser throat diameter of about 4 inches is required for the flow rates specified in this example.

After the secondary quench, the condensate separates into two layers, a water layer and an organic layer. The water layer amounting to about 750 pounds per hour is discarded and the organic layer is fed to the vacuum drum. In the secondary quench, 250 pounds per hour of heavy oil and tars are removed from the gases for discard with the residual oil from the vacuum drum. The gases from the secondary quench have the following composition.

These gases are compressed for processing in suit-able recovery zones downstream.

In the foregoing example, the cracking to ethylene was carried out in a comparatively long time, that is, approximately 0.07 second. This requires some soaking volume downstream of the diffuser. When higher temperature cracking to acetylene is carried out, a very short reaction time, as low as 0.005 second, is required and the difiuser downstream section is altered accordingly. Or, as an alternative, the volume of materials passing through the diffuser section is sufiiciently great to reduce the contact time.

It will be noted from the foregoing example that there is present a large percentage of nitrogen in the off-gases. Use of oxygen or an oxygen-enriched air in the combustion chamber will, of course, reduce the nitrogen in the oft-gases as Well as produce a higher temperature in the combustion chamber.

Reasonable variation and modification are possible Within the scope of the foregoing disclosure, drawing, and the appended claim to the invention, the essence of which is that a venturi actuated by hot gases, as described, is used to aspirate vapors from a distillation or other zone for conversion of the said vapors using the heat of the said gases upon admixture with said vapors in the venturi to carry out a time-temperature controlled reaction to produce useful products. When desirable, the products are quenched also as described.

I claim:

A method for converting a hydrocarbon oil to produce ethylene, acetylene, aromatics, and the like which comprises introducing said oil into a distillation Zone maintained under high vacuum of the order of 4 p.s.i.a. and at a temperature of the order of 525 F., operating a venturi, the low pressure zone of which communicates directly with said distillation zone by burning a fuel in a jet engine under elevated pressure, forcing combustion gases at said elevated pressure from said jet engine into said venturi at a velocity such that said venturi will by itself maintain said high vacuum of the order of 4 p.s.i.a. in said distillation zone, and sucking vapors immediately as formed, and without any further step, from said distillation zone directly into said venturi, therein cracking said Vapors and then quenching and recovering products of reaction from said venturi.

References Cited in the file of this patent UNITED STATES PATENTS 2,179,379 Metzer -Nov. 7, 1939 2,520,149 Keeling Aug. 29, 1950 2,767,233 Mullen et al. Oct. 16, 1956 OTHER REFERENCES Perry et al.: Chemical Engineers Handbook, pages 1453-56 (1950 published by McGraw-Hill Book C0,, Inc.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2179379 *Jul 18, 1936Nov 7, 1939Air ReductionManufacture of acetylene
US2520149 *Jun 14, 1944Aug 29, 1950Koppers Co IncProcess for producing olefins
US2767233 *Jan 7, 1952Oct 16, 1956Chemical Construction CorpThermal transformation of hydrocarbons
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3000989 *Jun 24, 1959Sep 19, 1961Montedison SpaProcess and apparatus for the thermal cracking of liquid or gaseous hydrocarbons
US3049574 *Jan 15, 1959Aug 14, 1962Phillips Petroleum CoProcess and apparatus for the oxidative dehydrogenation of organic compounds
US3207676 *Oct 7, 1963Sep 21, 1965Edmund A J MrozHeat treating of liquors containing dissolved solids whose solubility decreases at increasing temperature
US3219419 *Oct 25, 1960Nov 23, 1965Braconier Frederic Fran AlbertAdjustable quench pyrolysis furnace
US3248437 *Jan 3, 1961Apr 26, 1966Monsanto CoHydrocarbon conversion process
US3256065 *Oct 30, 1962Jun 14, 1966Continental Carbon CoApparatus for making carbon black
US3341429 *Apr 2, 1962Sep 12, 1967Carrier CorpFluid recovery system with improved entrainment loss prevention means
US3413375 *Apr 2, 1965Nov 26, 1968Knapsack AgProcess of the manufacture of butine-2
US3505176 *Feb 26, 1968Apr 7, 1970Lummus CoVacuum jet ejector distillation for recovery of toluene diisocyanate
US3531266 *Jan 31, 1968Sep 29, 1970Chemical Construction CorpProduction of synthetic methanol
US4278446 *May 31, 1979Jul 14, 1981Avco Everett Research Laboratory, Inc.Very-high-velocity entrained-bed gasification of coal
US4288408 *Jul 7, 1978Sep 8, 1981L. A. Daly CompanyApparatus for the diacritic cracking of hydrocarbon feeds for the selective production of ethylene and synthesis gas
US5026946 *Jul 26, 1988Jun 25, 1991The British Petroleum Company P.L.C.Production of C2 or higher hydrocarbons including ethylene
US5531866 *Dec 6, 1994Jul 2, 1996Gas Research InstituteWater and organic constituent separator system and method
US5545296 *Apr 27, 1995Aug 13, 1996Gas Research InstituteWater and organic constituent separator system and method
US6019820 *May 7, 1997Feb 1, 2000E. I. Du Pont De Nemours And CompanyLiquid jet compressor
US8887525Dec 6, 2010Nov 18, 2014Pax Scientific, Inc.Heat exchange and cooling systems
WO2011123904A1 *Apr 10, 2011Oct 13, 2011Abaridy Pty LtdVapour absorption system
WO2014058417A1 *Oct 9, 2012Apr 17, 2014Abaridy Pty. Ltd.Vapor absorption system
Classifications
U.S. Classification208/92, 48/213, 585/955, 423/450, 585/539, 261/DIG.540, 585/650, 208/366, 203/91, 208/132, 585/911
International ClassificationC10G7/06
Cooperative ClassificationC10G9/38, C10G9/36, Y10S261/54, C10G7/06, Y10S585/911, Y10S585/955
European ClassificationC10G9/36, C10G9/38, C10G7/06