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Publication numberUS3661543 A
Publication typeGrant
Publication dateMay 9, 1972
Filing dateNov 26, 1969
Priority dateNov 26, 1969
Also published asCA935106A1, DE2054125A1, DE2054125B2, DE2054125C3
Publication numberUS 3661543 A, US 3661543A, US-A-3661543, US3661543 A, US3661543A
InventorsArthur L Saxton
Original AssigneeExxon Research Engineering Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Fluid coking process incorporating gasification of product ore
US 3661543 A
Abstract
A heavy carbonaceous material such as petroleum residuum (1,050 DEG F.+) is converted completely to distillate and gaseous products by an integrated process consisting of a conventional fluid coking reactor, a circulating coke heater, and a gasifier in which the coke formed in the reactor is converted to an H2 and CO rich gas by reaction with steam and an oxygen-containing gas. The process can also be operated by yield a net product of good quality coke.
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Description  (OCR text may contain errors)

United States Patent 3,66 1 ,543

Saxton 1 May 9, 1972 154] FLUID COKING PROCESS 3.542.532 11/1970 Johnson et a1 .208/127 8 et X 2,600,430 6/1952 Rlbletl ..48/206 x PRODUCT ORE 2,605,215 7/1952 Coghlan ..201/1 6 x Inventor: Arthur L. Saxton, Warren Township, NJ.

Assignee: Esso Research and Engineering Company Filed: Nov. 26, 1969 Appl. No.: 880,219

US. CL; ..48/206, 48/63, 23/204 M, 23/212 R, 201/31, 201/44, 208/127 Int. Cl ..Cl0j 3/00,C10b 49/10 FieldoiSearch... ..20l/15,16,14,13,17,31, 201/44; 48/206, 63; 208/127; 23/204 M, 212 R References Cited UNITED STATES PATENTS 2/1955 Keith ..208/127 GAS FRA T GAS 011.

STEAM Primary Examiner-Norman Yudkoff Assistant Examiner-David Edwards Attorney-Pearlman and Stahl and C. D. Stores [5 7] ABSTRACT A heavy carbonaceous material such as petroleum residuum 1,050" F.+) is converted completely to distillate and gaseous products by an integrated process consisting of a conventional fluid coking reactor, a circulating coke heater, and a gasifier in which the coke formed in the reactor is converted to an H and CO rich gas by reaction with steam and an oxygen-containing gas. The process can also be operated by yield a net product of good quality coke.

10 Claims, 1 Drawing Figure 1101' COKE ASH P'ATENTEDHM 9 1972 moSmEGE 5200 w $5 INVENTOR.

ATTORNEY mdbxz kudxmu mun -mum FLUID COKING PROCESS INCORPORATING GASIFICATION OF PRODUCT ORE BACKGROUND OF THE INVENTION In conventional fluid coking, the carbonaceous feed is injected into a bed of fluid coke where it is cracked to vapors and coke. The vapors pass through a cyclone to a scrubber/fractionator where they are fractionated to gas, naphtha and oil products, and a heavy stream which is recycled to the coking reactor. A circulating stream of coke is stripped in the bottom zone of the reactor and transferred to a coke burner where sufficient air is injected for burning part of the coke and heating the remainder sufficiently to satisfy the heat requirements of the coking reactor when the unburned hot coke is recycled thereto. Net coke above that consumed in the burner is withdrawn as product coke.

Unfortunately, the market for this coke has been limited with the result that attempts have been made to increase its value by subsequent treatment such as high temperature calcining and briquetting. Alternatively, the coke can be converted to an H and CO rich gas in a subsequent processing step by reaction with steam and an oxygen-containing gas. None of these subsequent coke processing steps has been found to be economically attractive for general use.

Furthermore, when processing typical petroleum residuum in a conventional fluid coker, the combustion products from the burner have an undesirably high SO content which is an atmospheric pollutant.

The two above problems low market value of the product coke, and atmospheric pollution from the burner have limited the use of fluid coking which is otherwise a superior residuum conversion process.

SUMMARY OF THE INVENTION ficulties can be overcome and the attractiveness of the basic fluid coking process greatly enhanced by replacing the coke burner used in the normal fluid coking process with an integrated coke heater and gasifier system comprising two fluidized beds of coke separated by a grid or other means, wherein coke is gasified in the lower'zone in'the presence of steam and air or commercially pure oxygen forming hotgases which pass into the upper bed, releasing heat which is transferred to the reactor via a circulating coke stream.'-Altematively, the gases from the gasification zone could'be combined with the circulating coke'from the reactor and conducted through a transfer line into a separator vessel'from which the hot coke circulates back to the reactor to supply its heat requirements. In either case, entrained coke will also pass to the heater'to provide additional heat for the coker-reactor. Air, or other oxygen-containing gas may be added to the heating zone to burn a portion of the CO and hydrogenand thus provide any additional heat which is required to satisfy the coking reactor heat requirement.

The gas product from the heater is rich in H, and CO and is an attractive feed gas for manufacturing a concentrated H stream via the well-known'water-gas-shift reaction, or' for BRIEF REFERENCE TO THE DRAWING The invention will be better understood by reference to the accompanying drawing which shows in diagrammatic form suitable apparatus for carrying out a preferred embodiment of the invention.

PREFERRED EMBODIMENT OF THE INVENTION Referring now to the drawing, a carbonaceous material having a Conradson carbon of about 15 percent, such as heavy residuum boiling l,050 F.+, or a coal charslurry, is passed into coking zone 1 by line 2, manifold 3 and multiple feed nozzles represented by lines 4, 5, 6, 7 and 8 onto a fluidized bed of solids, e.g., coke of 40 to 1,000 microns in size, having an upper level L. A fluidizing gas,e.g., steam, is admitted to the base of the vessel through line 9 in amounts sufficient to obtain superficial fluidizing gas velocities in the range of 0.5 to 4 ft./sec. Coke at a temperature to 300 F. above the coking temperature is admitted to the coker-by line 10 in amounts sufiicient to maintain a coking temperature in the range of 900 to l,200 F. The lower portion of the coker serves as a stripping zone to remove occluded hydrocarbons from the coke. Coke is withdrawn from this stripping zone by line 11 and is circulated to heater l2. Conversion productsare passed through cyclone l3 to remove entrained solids which are returned to the coker through dipleg 14. The vapors leave the cyclone through line 15 and pass into scrubber-fractionator 16 where they are fractionated to gas leaving by line 17 naphtha by line 18 and gas oil by line 19. A heavy stream is removed through line 20, a portion of which is circulated through conventional heat removal exchangers and returned to scrubber as pumparound by line 21; another portion is recycled to the coker by line 22. The small amount of fine solid particles which pass through the reactor cyclone is returned to the coker reactor with this recycle stream.

In heater 12, stripped coke from the reactor (commonly called cold coke) is introduced by line 1 1 to a fluid bed of hot coke having .a level L. The bed is heated by fuel gas passing upward through disc and donut distributor 23 and egg crate baffle 24. Hot coke is removed from the fluidized bed in heater 12 by line 25 and a portion is passed by line 26 to a bed of fluidized coke having a level L in gasifier 27. Another portion is recycled to the coker by line 10 to supply heat thereto. The coke introduced to'the fluidized bed in the gasifier 27 is contacted with steam introduced by line28and air or oxygen by line 29 where the following reactions take place:

When coke is oxidized,the initial product is a mixture of CO and CO as shown inequation "1. At temperatures of 1,600" F.+ in the presence of oxygen, C0 is rapidly oxidized to CO according to equation 2. After oxygen has been exhausted, CO reacts with carbon to form CO. At high temperatures, equilibrium favors drawingequation' 3-to the rightto form CO. Low pressure also favors this'reaction. Reaction 3 is slower'thanreaction 2. Thus,equilibrium would favor very reaction is slightly endothermic and when steam issubstituted for some of the oxygen, the, gasification zone temperature drops at a constant quantity of coke gasified. Finally, water reacts with C0 to produce CO and hydrogen inthe water gas shift represented by equation 5. Most of the sulfur in the coke will be converted to H S with a very small amount of COS being formed.

The gases formed by the above reactions pass upwardly through the gasifier and into, the heater by way of the narrow neck portion 30. Additional air or oxygen may, be admitted to the heater by lines 31 to burn a small portionof these gases .and supply additional heat to the coke in the heater. The gases Mol.% Including Mol.% Excluding ,0 i-i 11,0 as H, 6.5 as 11.0 2.9 co 19.9 20.6 co, 1.9 8.2 N, 61.9 64.4 ms 0.9 i

Net heating value on a dry basis is 84.6 BTU/SCF. When oxygen is used for gasification, a typical composition of the gas Net heating value on dry basis is 224 BTU/SCF. Small quantities of cracked hydrocarbon materials will also be present in the product gases and will increase the heating value of the product gases. The quantity and composition will vary somewhat depending on the coker reactor feed and on reaction and stripping conditions.

Some net product coke may be withdrawn if desired through line 33. Agglomerates of foreign solids, which mayform in some cases, can also be purged via this line through an elutriator from which any included coke can be blown back into the gasifier.

While the process has been described with respect to the circulation of coke as the fluidized medium used in the process, it is to be understood that a captive bed of fluidized inert particles, such as alundum or mullite, may be used in the gasifier 27. This can. be advantageous for systems in which substantial quantities of very fine about p.) particles of foreign solids are released inthe gasifier such that very low velocities would be required in order to maintain a stable fluidized bed. Such a captive bed can be fluidized readily without significant entrainment of the captive bed particles at superficial velocities substantially higher than the entrainment velocity of line particles released from the coke. Such a captive bed provides a well mixed reaction zone in the gasifier in which the carbon can be burned and the foreign solids released without causing severe fluidization problems. Some equilibrium concentration of the fine particles are retained in the gasifier bed, thus providing-sulficientresidence time for complete gasification of the carbon before the bulk of the particles are entrained by the exit gases. The hot gasifier products, including entrained solid particles, pass through a heat exchangebed similar to the bed described in connection with heater 12. In this heat exchange bed the coke from the reactor would be heated as required to satisfy the reactor heat balance. This type of process would be preferable when processing feeds containing much higher solids than are normally present in petroleum residuum, e.g., bitumen from coal, tar sands or shale which may contain -20 percent inert solids. The solids, such as fine sand, metal oxides, or the like, contained in the bitumen are released in the captive bed in the gasifier and being smaller than the coke are more easily entrained out and carried upwardly through the heat exchange bed. These fine particles will also pass through the conventional cyclones in the heater vessel but can be recovered by a downstream electrical precipitator.

EXAMPLE A Kuwait vacuum residuum containing 5.5 wt. percent suifur, boiling l,050 F.+ and having a Conradson carbon of 21.8 is introduced into the fluidized bed of coker 1, operating at 975 F. The coke produced is passed to heater 12 at 950-975 F. and heated with gases from gasifier 27 at 1,800 F. This gas is formed from coke gasified in gasifier 27 by air or oxygen and steam introduced thereinto. The gas leaves the heater at 1,150 F. After transferring heat to the circulating coke. Virtually all solid material is removed from the gas by cyclone 32.

Steam/air rates are controlled to maintain the gasifier bed at a temperature of about 1,800" F. The heater operates at a pressure of 20 psig and the gasifier at 25 psig.

The following data are obtained:

TABLE 1 Operating Conditions and Feed and Product Compositions Coker Feed and Operating Conditions Coker feed Rate 12,000 B/SD Source Kuwait 1050F.+Residuum Con. carbon, wt.% 21.8 Sulfur, wt.% 5.5 Gravity, APl 5.7 Va, ppm 1 13- Ni, ppm 25 Totalash, ppm 252 Operating conditions Reactor temperature, F. 975 Reactor product final cut point, F. 950 Coke circulation rate, tons/min. 15.5 Heater zone temperature, F. l 150 pressure, psig 20 Gasifier zone temperature, F. 1800 pressure, psig 25 Coke composition Gross Oil Net to gasification Hydrogen, wt.% 6.0 14.7 Carbon, wt.% 86.6 77.9 90.1 Sulfur, wt.% 7.4 7.4 7.4 Va, ppm 410. Ni, ppm Total ash, ppm 906 Air/Steam Oxygen/Steam Product gas composition Gasification Gasification Composition, mol.%

CO 20.4 42.0 CO, 6.6 18.0 H, 4.4 18.7 11 0 1.4 6.7 (C1-1) 5.0 1 1.0 1-1,S 1.2 2.6 N, 61.0 1.0

100.0 100.0 Fuel gas heating valve (Hi-1V) BTU/SCF (ex. H,S) 150 350 The material balance on the heater gasifier is as follows:

TABLE IL-HEATER-GASIFIER HEAT AND MATERIAL BALANCE Material Balance! (Number for oxygen/steam gasificatlon shown in parenthesis where different from air/steam gaslfication.)

Cold coke Hot coke Air or from Entrained to Steam (oxygen) Steam reactor oil reactor Temp F. 350 353 975 075 l, 150 M#/hr 4(14) 1, S 14. 4 1, 860 6, 030(1,070) ACF/miu Supplemcntary Gasifier Euair (or stage trained oxygen) Gasifier product coke to to upper Product feed gas heater zone gas 'Iemp., F 1,150 1,800 1,800 360 1,150 Mi /hm--- 136(132) (96) =Mol/hr 8,100(3, 917) 1, 630(460) 9, 980(4, 445) MACF/min- 82. 3(39. 9) 83. 7(37. 4)

Heater section heat balance Air/steam Oxygen/steam Heat load:

Heat to circulating coke 130. 0 130. 0 Entrained oil heat of cracking 6. 0 5. 0 Heat to transfer line steam 3. 4 3. 4 Heater heat losses 3. 6 3. 6

Total 142. 0 142.0

Heat supply:

Gas from gasifier 42. 0 20. 1 Entrained coke 28. 6 28.6 Combustion of C0 and H2111 heater.. 7]. 4 93. 4

Total 142. 0 142. 0

It will be appreciated that operating conditions, product gas composition and the overall heat and material can vary substantially from the above data, depending on such variables as the coker reactor feed and the coker product objectives.

The nature and advantages of the present invention having been fully set forth and examples of the same given, what is claimed as new, useful, and unobvious and desired to be secured by Letters Patent is:

1. An integrated fluid coking-gasification process which comprises:

treating a carbonaceous material in a low pressure fluid coking zone comprising a fluid bed of particles operating at a temperature between about 900 and about l,200 F. to produce coke and light hydrocarbon material, some of which may adhere to said coke; i a a? heating to a higher temperature said coke in a low pressure heating zone comprising a separate fluid bed of particles;

passing a portion of said heated coke to said fluid coking zone and another portion of said heated coke to a low pressure gasification zone;

contacting said heated coke in said gasifying zone with steam and an oxygen-containing gas to produce a metalrich ash and a gaseous stream containing hydrogen and carbon oxide gases;

passing said ash and gaseous stream to said heating zone to provide a substantial part of the heat required in said heating zone;

recovering said gaseous stream of said heating zone.

2. A process according to claim 1 wherein the pressure in said fluid coking zone, said heating zone and said gasifying zone is less than about 3.0 atmospheres.

3. A process according to claim 1 wherein said gasifying zone comprises a separate bed of fluidized particles.

4. A process according to claim 3 wherein said gaseous stream leaving said gasifying zone passes through a distributing zone before entering said heating zone to provide for more even gas flow in said heating zone, as well as, better fluidizing of said heating zone bed.

5. A process according to claim 4 wherein additional oxygen-containing gases are mixed with said gaseous stream and said mixture passed through said distributing zone and then into said heating zone.

6. A process according to claim 1 wherein said coke produced in said fluid coking zone is passed through a stripping zone and contacted with a stripping gas to remove a major portion of said adhering light hydrocarbon material before said coke is heated in said heating zone.

7. A process according to claim 6 wherein said stripping gas is steam.

8. A process according to claim 1 wherein said metal-rich ash is recovered from said heating zone by cyclone means.

9. A process according to claim 5 wherein a portion of said metal-rich ash is recovered from said gasifying zone.

10. A process according to claim 1 wherein a portion of said steam treated, heated coke in said gasifying zone is removed from said gasifying zone.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2600430 *Aug 9, 1947Jun 17, 1952Hydrocarbon Research IncConversion of carbonaceous materials
US2605215 *Jan 15, 1949Jul 29, 1952Texas CoConversion of heavy carbonaceous oils to motor fuels, fuel gas, and synthesis gas
US2702267 *Apr 27, 1951Feb 15, 1955Hydrocarbon Research IncHydrocarbon conversion process and the stripping of the fouled catalyst with regeneration gases containing hydrogen
US2984618 *Jul 21, 1958May 16, 1961Exxon Research Engineering CoCoking and fractionating process
US3542532 *Jan 11, 1968Nov 24, 1970Exxon Research Engineering CoProcess for the production of hydrogen from petroleum coke
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3816084 *May 4, 1972Jun 11, 1974Exxon Research Engineering CoCokeless coker with recycle of coke from gasifier to heater
US3907662 *Feb 14, 1974Sep 23, 1975Mitsui Shipbuilding EngProcess of preparing desulfurized light oil and fuel gas from heavy oil
US3933445 *Oct 15, 1973Jan 20, 1976Exxon Research And Engineering CompanyProcess and apparatus for preventing deposits on a gas inlet nozzle
US4039392 *May 27, 1975Aug 2, 1977Singh Alamjit DProcess and apparatus for producing char and co-products from coal and the like
US4055484 *May 14, 1976Oct 25, 1977Exxon Research & Engineering Co.Elutriation in a fluid coking process
US4077869 *Oct 21, 1975Mar 7, 1978Exxon Research & Engineering Co.Hydrogen gas reactant
US4097361 *Aug 24, 1976Jun 27, 1978Arthur G. Mckee & CompanyProduction of liquid and gaseous fuel products from coal or the like
US4113602 *Jun 8, 1976Sep 12, 1978Exxon Research & Engineering Co.Integrated process for the production of hydrocarbons from coal or the like in which fines from gasifier are coked with heavy hydrocarbon oil
US4172857 *Apr 3, 1978Oct 30, 1979Arthur G. Mckee & CompanyProcess and apparatus for ethylene production
US4203759 *May 1, 1978May 20, 1980Exxon Research & Engineering Co.Process for the preparation of a vanadium-containing metallic ash concentrate
US4213848 *Jul 27, 1978Jul 22, 1980Exxon Research & Engineering Co.Fluid coking and gasification process
US4331529 *Nov 5, 1980May 25, 1982Exxon Research & Engineering Co.Multizones; synthesis gas; fuel gas
US4379046 *Jun 11, 1981Apr 5, 1983Exxon Research & Engineering Co.Integrated two stage coking and steam cracking process and apparatus therefor
US4411769 *Mar 23, 1982Oct 25, 1983Exxon Research & Engineering Co.Low temperature steam is used to cool separated solids, after coring, and superheat steam
US4497705 *Aug 17, 1983Feb 5, 1985Exxon Research & Engineering Co.Fluid coking with solvent separation of recycle oil
US4528088 *Nov 30, 1983Jul 9, 1985Exxon Research And Engineering Co.Coking with solvent separation of recycle oil using coker naphtha and solvent recovery
US4530755 *Oct 31, 1983Jul 23, 1985Exxon Research And Engineering Co.Separating heavy hydrocarbons from vapor phase product
US4542114 *Apr 13, 1984Sep 17, 1985Air Products And Chemicals, Inc.Regeneration of cracking catalyst
US4711968 *Oct 3, 1986Dec 8, 1987Exxon Research & Engineering Co.Process for the hydrofomylation of sulfur-containing thermally cracked petroleum residua
US4863586 *May 6, 1988Sep 5, 1989Veba Oel Entwicklungs-Gesellschaft MbhProcess for recovery of low-temperature carbonization oil
US4914246 *Oct 26, 1987Apr 3, 1990Exxon Research & Engineering CompanyReacting phenol and linear olefins using acid catalyst
US4922028 *Mar 10, 1989May 1, 1990Exxon Research & Engineering CompanyProcess for the hydroformylation of sulfur-containing thermally cracked petroleum residue and novel products thereof
US6168709Aug 20, 1998Jan 2, 2001Roger G. EtterProduction and use of a premium fuel grade petroleum coke
US8206574Feb 11, 2009Jun 26, 2012Etter Roger GAddition of a reactor process to a coking process
US8361310Feb 17, 2009Jan 29, 2013Etter Roger GSystem and method of introducing an additive with a unique catalyst to a coking process
US8372264Feb 16, 2009Feb 12, 2013Roger G. EtterSystem and method for introducing an additive into a coking process to improve quality and yields of coker products
US8372265Nov 19, 2007Feb 12, 2013Roger G. EtterCatalytic cracking of undesirable components in a coking process
US8394257Jun 26, 2012Mar 12, 2013Roger G. EtterAddition of a reactor process to a coking process
US20120063961 *May 17, 2011Mar 15, 2012Exxonmobil Research And Engineering CompanyFluid injection nozzle for fluid bed reactors
Classifications
U.S. Classification48/206, 201/44, 201/31, 208/127, 48/63
International ClassificationC10J3/46, C01B3/42, C10B49/10, C10B49/22, C10J3/54, C10G9/32, C10B55/10
Cooperative ClassificationC10J3/482, C10B55/10, C10B49/22, C10J2300/0933, C10J3/84
European ClassificationC10J3/48B, C10B55/10, C10B49/22