EP0148024A2 - Katalytisches Wirbelschicht-Krackverfahren - Google Patents

Katalytisches Wirbelschicht-Krackverfahren Download PDF

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Publication number
EP0148024A2
EP0148024A2 EP84309081A EP84309081A EP0148024A2 EP 0148024 A2 EP0148024 A2 EP 0148024A2 EP 84309081 A EP84309081 A EP 84309081A EP 84309081 A EP84309081 A EP 84309081A EP 0148024 A2 EP0148024 A2 EP 0148024A2
Authority
EP
European Patent Office
Prior art keywords
catalyst
reactor
process according
cracking
zsm
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP84309081A
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English (en)
French (fr)
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EP0148024A3 (de
Inventor
Frederick John Krambeck
Hartley Owen
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ExxonMobil Oil Corp
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Mobil Oil Corp
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Filing date
Publication date
Application filed by Mobil Oil Corp filed Critical Mobil Oil Corp
Publication of EP0148024A2 publication Critical patent/EP0148024A2/de
Publication of EP0148024A3 publication Critical patent/EP0148024A3/de
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Definitions

  • This invention relates to an improvement in hydrocarbon conversion processes wherein a catalyst is contacted with a hydrocarbon feedstock in a fluidized bed reactor.
  • the fluidized catalytic cracking process is well known. Cracked hydrocarbon vapours from the reactor pass to various product fractionators wherein the hydrocarbon mixture is separated into fractions. Some catalyst is usually carried along with the hydrocarbon vapours into the fraction-' ator. This catalyst tends to accumulate in the fractionator with the heaviest hydrocarbon fraction contained in the reactor effluent.
  • US-A-4,059,498 teaches an improved device in which a central tubular electrode extends downwardly through the filter bed.
  • An outer vertical perforated cylindrical electrode is concentric with the central electrode. Radial liquid flow is provided, permitting increased flow rate as compared to longitudinal flow.
  • zeolites characterised by a Constraint Index in the range 1 to 12 (the significance and manner of determination of which term is set forth in our GB 1,446,522).
  • zeolite denotes the class of porotectosilicates, i.e., porous crystalline silicates that contain silicon and oxygen atoms. as the major components.
  • Other components may be present in minor amounts, usually less than 14 mole % and preferably less than 4 mole %. These components include aluminium, gallium, iron, chromium, boron and the like with aluminium being preferred and used herein for illustration purposes. The minor components may be present separately or in mixtures.
  • Constraint Index (CI) values for some typical materials are:
  • a crystalline zeolite when identified by any combination of conditions within the testing definition set forth in the aforesaid GB 1,446,522 as having a Constraint Index in the approximate range of 1 to 12 is intended to be included in the instant zeolite definition whether or not the identical zeolite, when tested under other of the defined conditions, may give a Constraint Index value outside of the approximate range of 1 to 12.
  • novel class of zeolites defined herein is exemplified by ZSM-5, ZSM-11, ZSM-5/ZSM-11 intermediate, ZSM-12, ZSM-23, ZSM-35, ZSM-38 and ZSM-48, defined respectively by the x-ray data set forth in UA-A-3,702,886; 3,709,979; 4,229,424; 3,832,449; 4,076,842; 4,016,245; 4,046,859; and 4,377,497.
  • the present invention contemplates utilization of such zeolites wherein the mole ratio of silica to alumina is essentially unbounded.
  • Reference to the above-identified patents should not be construed as limiting the disclosed crystalline zeolites to those having the specific silica-alumina mole ratios discussed therein, it now being known that such zeolites may be substantially aluminium-free and yet, having the same crystal structure as the disclosed materials, may be useful or even preferred in some applications, as may zeolites which contain trivalent lattice elements other than aluminium.
  • ZSM-5 is a preferred catalyst because it is exceedingly active.
  • Successful FCC processes may use catalysts containing relatively small amounts of ZSM-5 in an amorphous base such as silica, alumina, or silica-alumina.
  • ZSM-5 material its great activity, causes some operations problems.
  • its high activity is tempered by incorporation of the ZSM-5 in an amorphous base, the ratio of ZSM-5 to amorphous material is fixed.
  • additional particulate material containing neat ZSM-5 or enriched amounts of ZSM-5, as compared to the equilibrium catalyst in the FCC reactor.
  • ZSM-5 embedded in. an amorphous matrix Another problem with operation of ZSM-5 embedded in. an amorphous matrix, is that the deactivation/reactivation characteristics of the ZSM-5 and amorphous material are different.
  • the ZSM-5 material is relatively stable, as regards activity, in the FCC reactor.
  • the ZSM-5 needs very little regeneration.
  • the amorphous material rapidly deactivates after only a few minutes of operation due to coke deposition.
  • the only way to restore the activity of the amorphous material is to burn the coke therefrom in an FCC regenerator. Regeneration of the amorphous material tends to age, prematurely, the ZSM-5 catalyst passing through the regenerator, necessitating a continuing program of ZSM-5 addition to the FCC reactor to replace that ZSM-5 damaged by the regeneration process.
  • US-A-4,309,280 teaches adding a finely divided powder of zeolite additive promoter to coat the surface of FCC catalyst. This reference discloses that "the additive promoter can also be introduced to and/or recycled through the recycle feed”. See column 3, lines 28/29.
  • the additive is of such a size as to coat the catalyst, the additive is locked onto the FCC catalyst, and behaves as FCC catalyst. Recycle of FCC catalyst from the main column bottoms will result in additive recycle, plus recycle of a refractory slurry oil.
  • a fluidised catalytic cracking process of the cyclic, regenerative kind in which a cracking feed contacts in a reactor a cracking catalyst having an average particle size of 30 to 80 ⁇ m and a pore size sufficient to provide access to cracking sites for at least the majority of feed components, the catalyst being continuously withdrawn from the reactor, regenerated, and returned to the reactor, hydrocarbon effluent being continuously withdrawn from the reactor and subjected to fractionation, is characterised in that a catalyst comprising a crystalline zeolite having a constraint index in the range 1 to 12 and of average particle size 3 to 30 ⁇ m is continuously added to said reactor and is withdrawn in entrainment in said effluent at at least 50% of the rate of its addition.
  • added catalyst is withdrawn in entrainment in said effluent at at least 90% of the rate of its addition, and the quantity of said added catalyst in the reactor is 0.1 to 5% wt. of the quantity of said cracking catalyst in the reactor.
  • the added catalyst is recovered from entrainment in said effluent and recycled to the reactor, and at least 99% wt. of said added catalyst present in the reactor can be recycled added catalyst.
  • the cracking catalyst usually comprises from 5 to 50% wt. of a synthetic faujasite suspended within and distributed throughout an inorganic oxide matrix, whilst the added catalyst usually comprises from 10 to 40% wt. of a zeolite having the structure of zeolite ZSM-5 composited with an amorphous binder.
  • the present invention provides a fluidized catalytic conversion process wherein a feedstream is charged to a fluidized bed reactor containing a fluidized bed of equilibrium catalyst to produce cracked product, and a converted feedstream is removed as a product from the process, wherein the improvement comprises addition of an entrainable catalyst additive to said fluid bed, and removing a majority of said entrainable additive with said product removed from the fluid bed reaction zone.
  • the present invention provides a process for fluidized catalytic conversion of a hydrocarbon feed comprising charging to a fluidized bed reactor containing equilibrium fluid cat cracking catalyst a hydrocarbon feed and an entrainable catalyst additive to produce vapourized cat cracking products; removing said vapourized products containing at least 90 % wt. of said entrainable catalyst additive from said FCC reactor; recovering from said vapourized product at least a portion of said entrainable catalyst additive; and recycling at least a portion of said entrainable catalyst additive to said reactor.
  • the present invention provides a process for fluidized catalytic cracking of hydrocarbons comprising charging to a fluidized bed reactor a hydrocarbon feed and hot regenerated equilibrium catalyst from a source hereafter specified; adding to said reactor fresh entrainable catalyst additive and recycle entrainable catalyst additive from a source hereafter specified; converting in said fluid bed reactor said hydrocarbon feed to hydrocarbon products; removing from said reactor equilibrium catalyst, regenerating same in an oxygen-containing regenera-' tion zone to to produce regenerated catalyst, and recycling: said regenerated catalyst to said FCC reactor as said hot regenerated catalyst; removing from said reactor a reactor effluent vapour stream comprising hydrocarbon products and at least 50% wt.
  • the single figure is a simplified diagram representing an FCC unit with a reactor, regenerator and main fractionator.
  • the present invention solves two independent problems.
  • the first problem solved is the fact that ZSM-5 catalyst, or other entrainable catalyst additive, can be continuously added to the catalyst contained in a fluid bed reactor, and quickly removed from the reactor independently of the equilibrium catalyst.
  • the effect of catalyst additive addition can be made permanent by continuing to add it.
  • the second problem solved by this invention is the ability to recover the ZSM-5 catalyst or other entrainable catalyst additive, and recycle it to the reactor, without passing through the high temperature FCC regenerator. Avoiding the FCC catalyst regenerator prevents premature aging of the catalyst additive.
  • the FCC reactor may be an entirely dense phase fluid bed, or may operate with all riser cracking, with a dilute phase bed, or some mixture of both modes of operation.
  • the FCC regenerator can be a single dense bed, or two dense beds connected by a dilute phase transport riser connected to a second dense bed within the regenerator.
  • the regenerator can operate in a CO afterburning mode, or may be operated to produce substantial amounts of CO.
  • the practice of the present invention will be most beneficial when the regenerator is run relatively hot; usually this is associated with a CO afterburning type of operation. Hot catalyst regeneration promotes rapid deactivation of the ZSM-5 materials.
  • the equilibrium catalyst which will comprise the bulk of the catalyst within the fluid bed reactor, may be any conventional fluid bed, or FCC catalyst, either amorphous or crystalline, or a mixture of both. Catalysts having an average particle size of 10 to 100 micrometers diameter are commonly used in fluidized beds. The particle size distribution of the catalyst will be that required for good fluidization characteristics in the reactor.
  • a good FCC equilibrium catalyst will have the following properties:
  • An acceptable catalyst additive is any which can be added to the fluid bed reactor and removed with the vapourised reactor effluent.
  • the exact size of the entrainable catalyst additive will vary with operating conditions within the reactor, and will be affected to some extent by the size of the equilibrium catalyst and by the efficiency of the cyclones used to return the bulk of the equilibrium catalyst to the reactor.
  • a preferred additive is ZSM-5, either neat or . dispersed in an amorphous base.
  • the practice of the present invention is most advantageous when a relatively concentrated ZSM-5 material, e.g., typically 10 to 50% wt. Z SM-5, is added as an entrainable catalyst additive.
  • a relatively concentrated ZSM-5 material e.g., typically 10 to 50% wt. Z SM-5
  • an entrainable catalyst additive with an average particle size of 3 to 30, and preferably 5 to 20 micrometers will give good results.
  • the retention time of the entrainable catalyst additive will vary from the residence time of the gas to about ten times as long as the gas residence time. Usually the entrainable catalyst particles will be swept along with the gas, so the entrainable catalyst particle residence time will be on the order of 100 to 200 percent of the gas residence time within the reactor.
  • the entrainable catalyst additive is disproportionately effective within, e.g., the FCC reactor because of its small particle size. Even operating in a throwaway mode of operation, in the absence of recycle, the practice of our invention makes better use of the ZSM-5 because the ZSM-5 is in a highly divided state.
  • ZSM-5 is the entrainable additive, it should have the following composition and properties.
  • the fractionation facilities are conventional. Any commonly used method of recovering valuable products from material contained in the reactor effluent can be used. 'Usually the reactor effluent vapours are cooled and compressed and sent through a variety of absorber and fractionators. The heaviest material contained in the reactor effluent is usually removed as the bottom stream from a large fractionator, typically called the main fractionator. 1.
  • the catalyst can be recovered from the slurry oil by filtration, settling, addition of an antisolvent, or any other known means of separating a finely divided powder from a liquid.
  • fractionate the recycled catalyst i.e., separate large fines from small fines by using staged filtration, or other conventional means.
  • fraction most enriched in ZS M -5, or other desired catalyst additive can be recycled to the reactor, without sending other catalyst fines or the entire stream from the main column bottoms back to the reactor.
  • staged cyclone separators a baghouse, electrostatic precipitators, or equivalent means.
  • the entrainable catalyst additive recovery and recycle would occur upstream , of the product fractionator.
  • staged cyclones to recover and recycle to the reactor entrainable particles of ZSM-5 that would otherwise be removed from the reactor, rather than tolerate the problems introduced with a large slurry oil recycle.
  • Staged cyclonic separation of fine particles contained in reactor effluent q vapour could also accomplish the desired goal, namely recycle of entrainable ZSM-5 to the reactor without sending the ZSM-5 material or other entrainable additive through the regenerator.
  • the additive could additionally be treated to recover any lost activity, such as by combustion of coke deposits under milder conditions than those prevailing in the main regenerator.
  • the preferred method of recovering entrainable catalyst involves use of an electrostatic filter, such as the ones disclosed in US-A-3,928,158 and 4,059,498, the entire contents of which are incorporated herein by reference.
  • UA-A-3,928,158 describes an electrostatic filter in which an electrostatic gradient is imposed across a bed of glass beads. Liquid flows through the bed while the electrical gradient is imposed across the bed. Solids are deposited in the filter bed at the point of contact of the glass beads. The filter can be repeatedly and readily reconditioned for further use by backflushing.
  • the feed is mixed with a heavy recycle stream contained in line 2.
  • Catalyst additive may be added from two sources, fresh in line 3, recycled along with the heavy recycle stream in line 2, or both. Catalyst additive may also be added in other parts of the plant, so long as the additive eventually enters the reactor.
  • Regenerated equilibrium catalyst in line 11 is mixed with the incoming feed in the base of the riser 5 of reactor 4.
  • Catalyst and reactor effluent vapours are discharged from riser reactor 5 via discharge means 6, shown schematically as a short length of pipe with a downfacing discharge, although cyclones may also be used.
  • the equilibrium catalyst falls to the bottom of reactor 4 to form a dense bed of catalyst 7, while the entrainable catalyst additive is removed along with the reactor effluent vapour via line 13.
  • the riser reactor shown is merely illustrative of one suitable reactor. A single dense bed reactor, a series of fluid bed reactors, and ebullating bed reactor, or a moving bed reactor may also be used. All of these reactors operate with an equilibrium catalyst, and all may benefit by adding an entrainable catalyst additive.
  • the reactor effluent vapour in line 13 is charged to main column 14. Depending on the feed and catalyst, different products will be recovered. A typical product mix obtained by charging oil to an FCC unit is shown, but should not be limiting.
  • Removed overhead from main column 14 is a wet gas via line 16, a light naphtha via line 17 and a heavy . naphtha stream via line 18.
  • a light cycle oil is removed via line 20.
  • Heavy cycle oil is removed via line 22 or via line 23 if it is to he recycled to the reactor mixed with the recycled additive.
  • a main column bottom stream is withdrawn via line 24 and charged to electrofilter 26 wherein a heavy fraction enriched in catalyst fines and entrainable catalyst additive is recovered via line 27 and recycled via line 32 to line 23 containing heavy cycle oil, and from there it is charged via line 2 to mix with the fresh feed.
  • a portion of the main column bottom steam is withdrawn from the process via line 30 as clarified slurry oil, while the remaining portion of it is recycled via line 28 to the bottom of the main column.
  • a portion of the catalyst fines and entrainable catalyst additive is removed from the process via line 34.
  • the catalyst additive would have the following physical properties: and would be added to the plant by pumping it in as a slurry in a light cycle oil stream.
  • the amount of recycle additive present in the recycle catalyst stream from the main column bottoms would be 12,500 pounds (5,670 kg) per hour.
  • An electrofilter would be used to separate recycle additive from slurry oil so that recycle of the refractory slurry oil can be minimized.
  • Preferably at least 90% of the slurry oil is removed from the process, while at least 90-99% of the additive is recycled.
  • the riser feed would see a catalyst composition containing 0.25 weight percent ZSM-5 almost entirely due to recycle from the main column bottoms.
  • the amount of Z S M -5 going to the regenerator should of course be minimized, but a small amount will pass through the regenerator.
  • the significance of the present invention is that it gives refiners a way to change the catalyst characteristics in the FCC reactor without changing the catalyst inventory and without subjecting the entire catalyst inventory to the FCC regenerator.
  • the ZSM-5 additive it is possible to take advantage of the high activity and coke resistance of ZSM-5 without subjecting the ZSM-5 to the harsh conditions experienced in the modern CO afterburing regenerators associated with FCC units.
  • the ZSM-5 catalyst were added in a form where it behaved exactly as the equilibrium, the Z SM-5 would be subjected to high temperature regeneration every 3-10 minutes, and would lose most of its cracking activity within a few days, requiring very high ZSM-5 makeup rates to achieve the octane gains and gasoline plus alkylate yield gains described in the illustrative embodiment above.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
EP84309081A 1984-01-04 1984-12-27 Katalytisches Wirbelschicht-Krackverfahren Withdrawn EP0148024A3 (de)

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US56801484A 1984-01-04 1984-01-04
US568014 1984-01-04

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EP0148024A2 true EP0148024A2 (de) 1985-07-10
EP0148024A3 EP0148024A3 (de) 1986-12-17

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JP (1) JPS60158290A (de)
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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0259155A1 (de) * 1986-09-03 1988-03-09 Mobil Oil Corporation Strippverfahren für einen Katalysator aus eine katalytische Spaltzone
US4871446A (en) * 1986-09-03 1989-10-03 Mobil Oil Corporation Catalytic cracking process employing mixed catalyst system
WO2005017073A1 (en) * 2003-08-05 2005-02-24 Exxonmobil Chemical Patents Inc. Fines co-feed for maintaining efficient reactor hydrodynamics
US7223896B2 (en) 2004-04-29 2007-05-29 Exxonmobil Chemical Patents Inc. Fines co-feed for maintaining efficient reactor hydrodynamics
WO2009086107A2 (en) * 2007-12-20 2009-07-09 Chevron U.S.A. Inc. Heavy oil upgrade process including recovery of spent catalyst
US8178461B2 (en) 2008-12-30 2012-05-15 Chevron U.S.A. Inc Thermal treatment processes for spent hydroprocessing catalyst
CN106938849A (zh) * 2016-12-13 2017-07-11 江苏天诺新材料科技股份有限公司 利用废旧分子筛催化剂合成zsm‑5分子筛的方法
EP2618938A4 (de) * 2010-09-23 2017-11-22 Chevron U.S.A., Inc. Verfahren zur steuerung von feinstaubemissionen
CN109225320A (zh) * 2018-11-05 2019-01-18 宁夏大学 一种mfi结构废分子筛晶化再生的方法
WO2020069959A1 (en) * 2018-10-01 2020-04-09 Shell Internationale Research Maatschappij B.V. Process for removing catalyst fines by nanofiltration

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1264693A (en) * 1985-02-20 1990-01-23 Robert A. Lengemann Reducing the temperature in a regeneration zone of a fluid catalytic cracking process
FR2587629B1 (fr) * 1985-09-25 1993-07-16 Raffinage Cie Francaise Procede de separation de fines particules de catalyseur, d'une charge hydrocarbonee, par filtration au travers de barrieres minerales et boucle de filtration

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US3380911A (en) * 1966-02-15 1968-04-30 Mobil Oil Corp Method for converting hydrocarbons in two stages
US3527694A (en) * 1968-12-09 1970-09-08 Exxon Research Engineering Co Fluid solids system
DE2149218A1 (de) * 1970-10-06 1972-04-13 Mobil Oil Corp Verfahren zur katalytischen Crackung von Kohlenwasserstoffen
EP0021787A1 (de) * 1979-06-21 1981-01-07 Mobil Oil Corporation Verbesserung der Oktanzahl beim katalytischen Cracken
US4285805A (en) * 1980-03-20 1981-08-25 Phillips Petroleum Company Time-delay process and control system for electrostatic filter
EP0044631A1 (de) * 1980-07-18 1982-01-27 Mobil Oil Corporation Kohlenwasserstoff-Krackverfahren
US4345991A (en) * 1980-12-10 1982-08-24 Phillips Petroleum Company Catalytic cracking process
EP0127285A2 (de) * 1983-04-26 1984-12-05 Mobil Oil Corporation Sekundärinjektion von Zeolith vom ZSM-5-Typ in das katalytische Kracken

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US3338821A (en) * 1964-11-18 1967-08-29 Phillips Petroleum Co Quenching of catalytic cracking reactor vapors in feed line to fractionator
US3928158A (en) * 1973-05-22 1975-12-23 Gulf Research Development Co Electrofilter
US4022675A (en) * 1975-08-01 1977-05-10 Gulf Research & Development Company Filtering process
US4385805A (en) * 1978-05-03 1983-05-31 Rca Corporation Liquid crystal lens display system

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3380911A (en) * 1966-02-15 1968-04-30 Mobil Oil Corp Method for converting hydrocarbons in two stages
US3527694A (en) * 1968-12-09 1970-09-08 Exxon Research Engineering Co Fluid solids system
DE2149218A1 (de) * 1970-10-06 1972-04-13 Mobil Oil Corp Verfahren zur katalytischen Crackung von Kohlenwasserstoffen
EP0021787A1 (de) * 1979-06-21 1981-01-07 Mobil Oil Corporation Verbesserung der Oktanzahl beim katalytischen Cracken
US4285805A (en) * 1980-03-20 1981-08-25 Phillips Petroleum Company Time-delay process and control system for electrostatic filter
EP0044631A1 (de) * 1980-07-18 1982-01-27 Mobil Oil Corporation Kohlenwasserstoff-Krackverfahren
US4345991A (en) * 1980-12-10 1982-08-24 Phillips Petroleum Company Catalytic cracking process
EP0127285A2 (de) * 1983-04-26 1984-12-05 Mobil Oil Corporation Sekundärinjektion von Zeolith vom ZSM-5-Typ in das katalytische Kracken

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0259155A1 (de) * 1986-09-03 1988-03-09 Mobil Oil Corporation Strippverfahren für einen Katalysator aus eine katalytische Spaltzone
US4871446A (en) * 1986-09-03 1989-10-03 Mobil Oil Corporation Catalytic cracking process employing mixed catalyst system
WO2005017073A1 (en) * 2003-08-05 2005-02-24 Exxonmobil Chemical Patents Inc. Fines co-feed for maintaining efficient reactor hydrodynamics
EA009187B1 (ru) * 2003-08-05 2007-12-28 Эксонмобил Кемикэл Пейтентс Инк. Совместная подача мелочи для поддержания эффективной гидродинамики в реакторе
US7223896B2 (en) 2004-04-29 2007-05-29 Exxonmobil Chemical Patents Inc. Fines co-feed for maintaining efficient reactor hydrodynamics
CN101918516B (zh) * 2007-12-20 2013-06-12 雪佛龙美国公司 包括废催化剂回收的重油提质方法
WO2009086107A3 (en) * 2007-12-20 2009-09-24 Chevron U.S.A. Inc. Heavy oil upgrade process including recovery of spent catalyst
WO2009086107A2 (en) * 2007-12-20 2009-07-09 Chevron U.S.A. Inc. Heavy oil upgrade process including recovery of spent catalyst
US8178461B2 (en) 2008-12-30 2012-05-15 Chevron U.S.A. Inc Thermal treatment processes for spent hydroprocessing catalyst
US8470252B2 (en) 2008-12-30 2013-06-25 Chevron U.S.A. Inc. Thermal treatment system for spent hydroprocessing catalyst
EP2618938A4 (de) * 2010-09-23 2017-11-22 Chevron U.S.A., Inc. Verfahren zur steuerung von feinstaubemissionen
CN106938849A (zh) * 2016-12-13 2017-07-11 江苏天诺新材料科技股份有限公司 利用废旧分子筛催化剂合成zsm‑5分子筛的方法
WO2020069959A1 (en) * 2018-10-01 2020-04-09 Shell Internationale Research Maatschappij B.V. Process for removing catalyst fines by nanofiltration
CN112789100A (zh) * 2018-10-01 2021-05-11 国际壳牌研究有限公司 用于通过纳滤去除催化剂细粒的方法
CN109225320A (zh) * 2018-11-05 2019-01-18 宁夏大学 一种mfi结构废分子筛晶化再生的方法
CN109225320B (zh) * 2018-11-05 2021-09-21 宁夏大学 一种mfi结构废分子筛晶化再生的方法

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JPH0149439B2 (de) 1989-10-24
CA1241613A (en) 1988-09-06
EP0148024A3 (de) 1986-12-17
JPS60158290A (ja) 1985-08-19
AU3706184A (en) 1985-07-11
AU555438B2 (en) 1986-09-25

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