US3926778A - Method and system for controlling the activity of a crystalline zeolite cracking catalyst - Google Patents

Method and system for controlling the activity of a crystalline zeolite cracking catalyst Download PDF

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US3926778A
US3926778A US316632A US31663272A US3926778A US 3926778 A US3926778 A US 3926778A US 316632 A US316632 A US 316632A US 31663272 A US31663272 A US 31663272A US 3926778 A US3926778 A US 3926778A
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catalyst
hydrocarbon
cracking
regeneration
temperature
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Hartley Owen
Edward J Demmel
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Mobil Oil AS
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Mobil Oil AS
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Priority to US316632A priority Critical patent/US3926778A/en
Priority to GB4920573A priority patent/GB1417525A/en
Priority to FR7341771A priority patent/FR2210654B1/fr
Priority to DE2361142A priority patent/DE2361142A1/de
Priority to IT2998/73A priority patent/IT1000844B/it
Priority to NL7317400A priority patent/NL7317400A/xx
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Publication of US3926778A publication Critical patent/US3926778A/en
Priority to US06/827,183 priority patent/US5547910A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/084—Y-type faujasite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/90—Regeneration or reactivation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/40—Special temperature treatment, i.e. other than just for template removal
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the present invention is concerned with the conversion of hydrocarbon feed materials in one or more catalytic reaction zones and maintaining the activity of the catalyst employed therein. More particularly the present invention is concerned with the removal of carbonaceous material from the cracking sites of a crystalline zeolite containing cracking catalyst by the combination of catalyst regeneration in the presence of oxygen containing gaseous material and heat soaking of catalyst particles at least partially inactivated by deposited carbonaceous material.
  • the present invention involves the regeneration of catalyst comprising crystalline zeolite materials suitable for cracking hydrocarbon feed materials by the combina tion of riser regeneration of a carbon inactivated catalyst composition in the presence of sufficient oxygen to form combustion products substantially free of carbonmonoxide.
  • Oxygen regenerated cracking catalyst is used in a first hydrocarbon conversion zone under conditions to at least partially deactivate the catalyst by the deposition of carbonaceous material, the partially deactivated catalyst is then heat soaked at a tempera ture preferably in excess of the temperature of the catalyst as recovered from the first reaction zone whereby deposited carbonaceous material is substantially recovered from the active zeolite cracking catalyst and the zeolite catalyst thus improved in activity is used in a second hydrocarbon conversion reaction zone under elevated temperature cracking conditions.
  • Heat soaking of the catalyst is accomplished in the presence of added freshly regenerated catalyst provided in an amount to achieve a mixed catalyst temperature of about 50F. above the temperature of the catalyst as recovered from the first reaction zone and preferably 150F. above that temperature.
  • the mixed catalyst is heat soaked for a duration of at least 2 minutes and preferably at least 5 to minutes or more.
  • the method and system of this invention is concerned with the finding that heating of a crystalline aluminosilicate cracking catalyst containing fresh deposits of carbonaceous material of cracking will substantially restore the cracking activity of the catalyst.
  • the concepts of the present invention are widely applicable to crystalline zeolite cracking catalyst compositions and particularly those employing X and Y crystalline zeolites when alone or in combination with crystalline zeolites of the ZSM-S and ZSM-S type of materials.
  • Another suitable catalyst composition is known as Alderey.
  • the processing concepts of the present invention are particularly amenable to modem-day low coke producing crystalline aluminosilicate catalyst compositions and such catalyst may be used to advantage in both the hydrocarbon conversion operation of the process and the catalyst regeneration operation by developing a greater accumulation of carbonaceous deposits on the total mass of catalyst than heretofore obtained before regeneration thereof.
  • the reasons for this observed phenomenon is not readily explained and most unexpected.
  • the concepts going to the very essence of the present invention are applicable to other zeolite catalyst mixtures and particularly those comprising a mixture of a crystalline faujasite cracking component with a ZSM-5 type of crystalline material.
  • the catalyst mixture and/or compositions suitable for use in this invention comprise a mixture of small pore and large pore, crystalline aluminosilicate in combination with one another as separate discrete particles and these may be composited from substantially any high activity large pore crystalline zeolite cracking component in admixture with, for example, a ZSM-5 type of catalyst composition.
  • the ZSM-5 type catalyst composition is a relatively small average pore diameter material smaller than, for example, a rare earth exchanged X or Y crystalline zeolite.
  • the large and small pore crystalline zeolites above discussed may be dispersed within a separate or a common matrix material suitable for encountering relatively high temperatures contemplated in the fluid cracking operation of this invention with its attendant catalyst regeneration operation.
  • the catalyst mixture or composition contemplated for use in this invention will catalyze the conversion of the various components comprising the hydrocarbon feed including normal paraffins to produce for example gasoline as well as LPG types of gaseous materials.
  • the catalysts suitable for this invention have activity for'cracking several different kinds and types of hydrocarbons found in gas oil boiling range materials in combination with a very selective cracking of normal paraffins and singly branched hydrocarbons which are restructured and/or upgraded to desired higher boiling components.
  • novel process combination of this invention using a catalyst system comprising a mixture of separate catalyst particles or a homogeneous composition of one or more crystalline zeolite components dispersed in an amorphous matrix material wherein the zeolite component or components acts substantially independently as herein defined upon given hydrocarbon components and each catalyst component is relied upon substantially to support the function of the other.
  • a large pore crystalline aluminosilicate having a pore size in excess of about 9 Angstroms as a major component with the minor component being a small pore crystalline component having a maximum pore size not exceeding about 9 Angstroms and preferably being less than about 7 Angstroms.
  • the large and small pore zeolites may be used in substantially equal amounts or the smaller pore crystalline zeolite may be in a minor or major proportion.
  • either crystalline zeolite component may be used alone and dispersed in a suitable matrix material as herein defined.
  • the small pore crystalline zeolite is preferably a ZSM-S type of crystalline material such as that described in US. Pat. No. 3,702,886, issued Nov. 14, 1972 or copending application Ser. No. 257,983 a continuation of Ser. No. 865,418 filed Oct. 10, 1969 both now abandoned.
  • the large pore crystalline zeolite may be any of the now known crystalline aluminosilicates which are suitable for cracking hydrocarbons and providing a pore size in excess of 8 Angstroms. Such a composition has the structure and capability to act upon substantially all the components usually found in a gas oil feed boiling in the range of 500 up to 950 or llOF.
  • Large pore zeolites of this type are well known and include materials or synthetic faujasite of both the X and Y type as well as zeolite L. Of these materials zeolite Y is particularly preferred.
  • the crystalline zeolites above identified may be exchanged, combined, dispersed or otherwise intimately admixed with a porous matrix.
  • porous matrix it is intended to include inorganic and organic compositions with which the crystalline aluminosilicates may be affixed.
  • the matrix may be active or substantially inactive to the hydrocarbon conversion reactions encountered.
  • the preferred porous matrix may be selected from the group comprising inorganic oxides such as clay, acid treated clay, silica-alumina etc.
  • the small pore crystalline zeolite component of the catalyst is relied upon for promoting new ring formations and/or alkylation thereof in a manner which may be made to increase with reaction severity either by increasing temperatures or by increasing residence time thus encountering a corresponding decrease in alkylation reaction with the ZSM-5 crystalline component.
  • a significant observation contributing to the operational concepts of this invention is the finding that high temperature cracking of the gas oil feed above about lOO0F. does not significantly deactivate the activity and selectivity of a smaller pore ZSM-5 crystalline component combined with the larger pore size cracking component. Furthermore, it has been observed that combining a carbon monoxide oxidation promoter such as chromium oxide with the ZSM-5 catalyst component is not significantly deactivated by coke depositors and thus each component of the catalyst particle can function to independently perform its desired reaction mechanism, the ZSM-S component for olefin cyclization and the oxidation promoter for conversion of carbon monoxide to carbon dioxide in the regeneration steps of the overall combination herein described.
  • a carbon monoxide oxidation promoter such as chromium oxide
  • the total mass of catalyst circulated in the system desirably is a heat sink for promoting desired endothermic conversion reactions encountered in the operation.
  • the oxidation component such as copper, nickel, chromium, manganese oxide or copper chromite is combined with the catalyst as above described a significant heat benefit is realized by virtue of the exothermic conversion of CO to CO during regeneration of the catalyst and every opportunity for recovering this heat supply is taken advantage of in the processing concepts herein described.
  • the oxidation component may comprise from one tenth to three weight percent of the catalyst inventory.
  • the small pore size crystalline zeolite catalyst material preferred in the combination of this invention is preferably of the ZSM-5 type and as such the small pore has a uniform pore size varying because of its elliptical shape from about 5.5 Angstroms up to about 6 and about 9 Angstrom units.
  • the catalyst may comprise an aluminosilicate of the ZSM-S type blended with an aluminosilicate having a pore size generally larger than that of ZSM-5 and more usually greater activity 8 Angstrom units in a porous matrix as a homogenous mixture in such 'proportions that the resulting product contains from about 1 up to about by weight and preferably from about 10 to 50% by weight of total crystalline aluminosilicates in the final composite.
  • the particular proportions of one aluminosilicate component to the other in the catalyst system or composition herein defined is not narrowly critical and even though it can vary over an extremely wide range it has been found that the weight ratio of the ZSM-S type aluminosilicate to the large pore size aluminosilicate can range from 1:10 up to 3:1 and preferably should be 1 from about 1:3 to lzl.
  • Hydrocarbon charge stocks which may be converted by the combination and method of this invention comprise petroleum fractions having an initial boiling point of at least 400F. and an end point of at least 600F. and as high as 950 to 1l0OF.
  • the present invention also contemplates the cracking of naphtha boiling in the range of C hydrocarbons up to about 400F. to improve its octane rating in combination with producing significant quantities of LPG type materials which then can be used as part of the charge to the ZSM-S contact stage of the combination.
  • Hydrocarbons boiling above 400F. include gas oils, residual oils, cycle stocks, whole topped crudes and heavy hydrocarbon fractions derived by destructive hydogenation processes. These may be used alone or in combination as the first riser reactor hydrocarbon charge.
  • a cracking catalyst comprising a crystalline aluminosilicate such as a faujasite cracking component either alone or in admixture with a ZSM-S type material dispersed in matrix material of relatively low cracking activity is caused to circulate in a system of hydrocarbon conversion and catalyst regeneration shown in the drawing and herein de fined.
  • a catalyst contaminated with deposited carbonaceous material of cracking and obtained as hereinafter defined is passed by conduit 2 provided with flow control valve 4 at a temperature within the range of 800 up to about lOOOF. and more usually about 950F.
  • the mixing of hot regenerated catalyst with spent catalyst to raise the temperature of the spent catalyst can be further assisted by the addition of a combustion supporting fuel as by conduit 18 along with the oxygen containing regeneration gas.
  • the catalyst being regenerated in bed 10 in a relatively dense fluid condition is caused to move upwardly from the bed by combustion gases and carried into the restricted riser section with gaseous products of combustion for discharge from the end of the riser 8 into a combination of cyclone separators 24 and 26 arranged in parallel flow arrangement for separating regenerated catalyst from regeneration flue gases.
  • the regeneration system of this invention is particularly useful and desirable since additional oxygen containing regeneration gas is added to the suspension in riser 8 by one or more spaced apart conduits represented by conduits 20 and 22.
  • the additional oxygen rich gas causes further buming of carbonaceous deposits to be accomplished along with promoting the combustion of formed carbon monoxide (CO) so that the restricted riser section is an effective heat exchange zone of considerable magnitude between catalyst particles and combustion product gases passing therethrough.
  • CO carbon monoxide
  • Gaseous products of combustion pass overhead from cyclone separator 24 and 26 by open end conduits 34 and 36 discharging into a dispersed phase above a fluid bed of catalyst 32 and thence into cyclone separators 38 and 40 provided with diplegs 42 and 44.
  • Fucidizing gas and/or oxygen containing regeneration gas may be added by conduit 46 to the lower portion of catalyst bed 32 to effect a final burning of carbonaceous material if such is required and desired to further elevate the temperature of the catalyst.
  • Gaseous products of regeneration or flue gases are passed from cyclone separators 38 and 40 to chamber 48 from which they are withdrawn by conduit 50.
  • the hot regenerated catalyst comprising bed 32 being at an elevated temperature in excess of about lOOOF. and as high as 1400 or 1600F. is withdrawn from a lower portion thereof for distribution and use as discussed above and below.
  • a stream of hot regenerated catalyst is withdrawn from catalyst bed 32 by conduit 52 provided with flow control valve 54 and passed to the bottom portion of riser reactor 56 to which a suitable hydrocarbon feed is introduced by conduit 58.
  • a suspension is formed with the catalyst and hydrocarbon introduced to the riser providing a catalyst to oil ratio sufficient to obtain a suspension temperature of at least lOOOF.
  • the hydrocarbon feed may be preheated by means not shown up to about 800F. before admixture with the catalyst.
  • hydrocarbon residence time with the range of a fraction of a second up to several seconds such as 5 to 10 seconds or as high as about 15 seconds. More usually the hydrocarbon residence time within riser 56 will be in the range of 1 to 5 seconds.
  • the hydrocarbon-catalyst suspension passed through riser 56 discharges at the upper end thereof into one or more suitably arranged cyclone separator 60 provided with catalyst dipleg 62. Gasiform hydrocarbon material separated in cyclone 60 is carried overhead by conduit 64 into chamber 66 and thence by conduit 68 to a product fractionation zone not shown.
  • the catalyst separated by cyclone 60 is conveyed by dipleg 62 to a dense fluid bed of catalyst 70 therebelow.
  • hot freshly regenerated catalyst is added to fluid bed 70 by riser conduit 72 in an amount sufficient to achieve a desired temperature increase of at least 50F. and sufficient to provide a catalyst mix temperature of at least lOOOF.
  • the regenerated catalyst is supplied to riser 72 by conduit 74 provided with flow control valve 76.
  • Lift gas, substantially inert to the environment contacted is introduced to the base of riser 72 by conduit 78.
  • the catalyst is maintained at a temperature of at least lOOOF.
  • a stripping and/or fluidizing gas is introduced to the lower portion of bed 70 by steam conduit 80 to maintain the catalyst during its head soaking operation in a fluidized condition.
  • the heat soaked catalyst is then withdrawn at an elevated temperature in the range of 1000 to about l300F. from the bottom of the bed by conduit 82 provided with a flow control valve 84 for passage to the bottom portion of a second riser reactor 86 to which a second hydrocarbon feed is introduced by conduit 88.
  • Additional hot regenerated catalyst may also be withdrawn by conduit 90 provided with flow control valve 92 and mixed with the catalyst in conduit 82 passed to riser 86.
  • the catalyst and oil introduced to the lower portion of riser 86 is adjusted to form a suspension providing a temperature within the range of lOOO to l250F. which then moves upwardly through the riser during the conversion of the hydrocarbon charge.
  • the operating conditions in riser 86 may be the same as that employed in riser 56 or more severe by relying upon an increased catalyst to oil ratio within the range of 3 to and a hydrocarbon residence time within the range of 0.5 to 15 or more seconds.
  • a more dense catalyst phase suspension may be employed in riser reactor 86 than employed in riser reactor 56.
  • the suspension passed through riser 86 is separated in cyclone 94 provided with dipleg 96.
  • Separated gasiform hydrocarbon material is removed from separator 94 by conduit 98 and passed to chamber 66 wherein it is combined with hydrocarbons separated by cyclone 60.
  • Catalyst separated in cyclone 94 is passed by dipleg 96 to a separate dense fluid bed of catalyst 100 separated from catalyst bed 70 by a common baffle member 102. It is contemplated maintaining catalyst bed 100 and 70 as concentric cylindrical and annular beds within the lower portion of the vessel with bed 70 being retained preferably as the concentric cylindrical bed of catalyst.
  • Catalyst bed 100 is stripped with stripping gas such as steam introduced by conduit 104. Stripped catalyst is withdrawn from catalyst bed 100 and conveyed by conduit 2 to catalyst regeneration as defined above.
  • a further embodiment of this invention is concerned with utilizing a dual function catalyst such as a Y faujasite crystalline zeolite in conjunction with a ZSM-5 type of crystalline material to provide the capability of internally controlling to some considerable degree the activity level of each of the separate zeolite components. For example, varying the temperature and time of heat soaking the catalyst apparently yields a higher activity for the Y faujasite component. On the other hand, since the ZSM-S type component lays down very little coke by comparison it inherently retains much more of its initial cracking activity. Thus using no heat soaking between stages or after the first stage will maximize the activity of the ZSM5 component in the second riser. The amount of activity would be proportional to the ratio of recycled to freshly regenerated catalyst.
  • a Y faujasite crystalline zeolite containing cracking catalyst was coked for one minute at 925F., at a 6 weight hourly space velocity using a 10 catalyst to oil ratio with a gas oil feed boiling from 460 to 900F. of 22 API gravity.
  • the catalyst thus coked had a cracking activity of about 27.9. Determination of the catalyst cracking acitvity was obtained by contacting the catalyst with a Light East Texas Gas Oil (LETGO) at 850F., 2 catalyst/oil ratio, 6 weight hourly space veloc ity.
  • LETGO Light East Texas Gas Oil
  • the stripped catalyst was then heat soaked for 10 minutes at 1100F. and tested for activity.
  • the activity determined by the above recited LETGO test was 38.9. It is clear from the above that heat soaking of a crystalline zeolite containing catalyst used for cracking gas oil can restore its activity far beyond that obtained by high temperature stripping of the catalyst above.
  • the activity of a stabilized Y sieve cracking catalyst after regeneration is usually in the range of 40 to 45.
  • a method for converting hydrocarbons by cracking in the presence of a crystalline zeolite containing cracking catalyst which comprises a. passing a first hydrocarbon feed in admixture with a crystalline zeolite cracking catalyst obtained from a catalyst regeneration zone through a first cracking zone at an elevated cracking temperature in the range of lOOOF. up to about l30()F. at a hydrocarbon residence time less than about 10 seconds,
  • the crystalline zeolite containing cracking catalyst comprises a mixture of faujasite cracking catalyst particles and ZSM-5 type catalyst particles containing an oxidation promoter for converting carbon monoxide to carbon dioxide.
  • a method for improving the activity of a crystalline zeolite hydrocarbon conversion catalyst reduced in activity by deposited carbonaceous material which comprises heat soaking the crystalline zeolite hydrocarbon conversion catalyst at a temperature of at least 1lOOF. for about 10 minutes in the presence of a gas substantially inert to the environment.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
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US316632A 1972-12-19 1972-12-19 Method and system for controlling the activity of a crystalline zeolite cracking catalyst Expired - Lifetime US3926778A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
US316632A US3926778A (en) 1972-12-19 1972-12-19 Method and system for controlling the activity of a crystalline zeolite cracking catalyst
GB4920573A GB1417525A (en) 1972-12-19 1973-10-23 Method for converting hydrocarbons by cracking in the presence of a zeolite cracking catalyst
FR7341771A FR2210654B1 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1972-12-19 1973-11-23
DE2361142A DE2361142A1 (de) 1972-12-19 1973-12-07 Verfahren zur steuerung der aktivitaet eines kristallinen zeolith-crackkatalysators
IT2998/73A IT1000844B (it) 1972-12-19 1973-12-14 Procedimento per la conversione di idrocarburi mediante piroscissione in presenza di un catalizzatore contenente zeolite cristallina
NL7317400A NL7317400A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1972-12-19 1973-12-19
US06/827,183 US5547910A (en) 1972-12-19 1986-02-06 Method and system for controlling the activity of a crystalline zeolite cracking catalyst

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DE (1) DE2361142A1 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
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Cited By (75)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3970587A (en) * 1973-07-18 1976-07-20 Mobil Oil Corporation Combustion regeneration of hydrocarbon conversion catalyst with recycle of high temperature regenerated catalyst
US4035284A (en) * 1973-07-18 1977-07-12 Mobil Oil Corporation Method and system for regenerating fluidizable catalyst particles
US4051013A (en) * 1973-05-21 1977-09-27 Uop Inc. Fluid catalytic cracking process for upgrading a gasoline-range feed
US4062759A (en) * 1976-05-07 1977-12-13 Texaco Inc. Fluidized catalytic cracking regeneration process
US4064039A (en) * 1976-01-28 1977-12-20 Mobil Oil Corporation Fluid catalytic cracking
US4065269A (en) * 1973-12-28 1977-12-27 Uop Inc. Spent catalyst regeneration apparatus
US4072600A (en) * 1974-02-08 1978-02-07 Mobil Oil Corporation Catalytic cracking process
US4088568A (en) * 1976-01-15 1978-05-09 Mobil Oil Corporation Catalytic cracking of hydrocarbons
US4147617A (en) * 1978-04-06 1979-04-03 Mobil Oil Corporation Processing hydrocarbon feed of high carbon residue and high metals content
US4148751A (en) * 1976-02-02 1979-04-10 Uop Inc. Method of regenerating coke-contaminated catalyst with simultaneous combustion of carbon monoxide
US4159239A (en) * 1973-09-20 1979-06-26 Mobil Oil Corporation Catalytic cracking process
US4174272A (en) * 1973-09-20 1979-11-13 Mobil Oil Corporation Catalytic cracking of hydrocarbons
US4176084A (en) * 1975-07-08 1979-11-27 Exxon Research & Engineering Co. Process for regenerating metal-contaminated hydrocarbon conversion catalysts
US4197418A (en) * 1979-03-01 1980-04-08 Mobil Oil Corporation Heat disposed in lower alcohols and derivatives conversion to gasoline hydrocarbons in a crystaline zeolite fluidized bed
EP0021616A1 (en) * 1979-06-11 1981-01-07 Mobil Oil Corporation Catalytic cracking process
EP0021787A1 (en) * 1979-06-21 1981-01-07 Mobil Oil Corporation Octane improvements in catalytic cracking
US4252632A (en) * 1976-04-29 1981-02-24 Atlantic Richfield Company Catalyst and process for conversion of hydrocarbons
US4253939A (en) * 1976-06-21 1981-03-03 Atlantic Richfield Company Catalyst and process for conversion of hydrocarbons
US4257875A (en) * 1979-05-29 1981-03-24 Uop Inc. Fluid catalytic cracking process
US4283273A (en) * 1976-11-18 1981-08-11 Mobil Oil Corporation Method and system for regenerating fluidizable catalyst particles
US4312743A (en) * 1979-07-23 1982-01-26 Uop Inc. FCC Process using catalyst produced from used FCC catalyst
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CN109195697A (zh) * 2016-06-17 2019-01-11 陶氏环球技术有限责任公司 流体催化反应器系统的系统组件
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US10632439B2 (en) 2016-06-17 2020-04-28 Dow Global Technologies Llc System components of fluid catalytic reactor systems
RU2741554C2 (ru) * 2016-06-17 2021-01-26 Дау Глоубл Текнолоджиз Ллк Системные компоненты систем реактора с псевдоожиженным катализатором
CN109195697B (zh) * 2016-06-17 2022-05-27 陶氏环球技术有限责任公司 流体催化反应器系统的系统组件

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US5547910A (en) 1996-08-20
FR2210654A1 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1974-07-12
IT1000844B (it) 1976-04-10
FR2210654B1 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1977-03-11

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