EP0654520B1 - Integriertes katalytisches Krack- und Olefinen Herstellungsverfahren - Google Patents

Integriertes katalytisches Krack- und Olefinen Herstellungsverfahren Download PDF

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Publication number
EP0654520B1
EP0654520B1 EP19940308423 EP94308423A EP0654520B1 EP 0654520 B1 EP0654520 B1 EP 0654520B1 EP 19940308423 EP19940308423 EP 19940308423 EP 94308423 A EP94308423 A EP 94308423A EP 0654520 B1 EP0654520 B1 EP 0654520B1
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Prior art keywords
catalyst
dehydrogenation
catalytic cracking
olefin
alkane
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EP19940308423
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English (en)
French (fr)
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EP0654520A1 (de
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Michael Charld Kerby
Roby Bearden, Jr.
Stephen Mark Davis
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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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
    • C10G11/14—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
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • This invention relates to a combined catalytic cracking and olefin producing process.
  • US-A-4,830,728 discloses a fluid catalytic cracking (FCC) unit which is operated to maximize olefin production.
  • the FCC unit has two separate risers in which different feed streams are introduced.
  • the operation of the risers is designed so that a certain catalyst will act to convert a heavy gas oil in one riser and a different catalyst will act to crack a lighter olefin/naphtha feed in the other riser.
  • Conditions within the heavy gas oil riser are modified to maximize either gasoline or olefin production.
  • the primary means of maximizing production of the desired product is by using a specified catalyst.
  • a problem inherent in producing olefin products using FCC units is that the process depends upon a specific catalyst balance to maximize production.
  • olefin selectivity is generally low due to undesirable side reactions such as extensive cracking, isomerization, aromatization and hydrogen transfer reactions. It is, therefore, desirable that olefin production be maximized in a process which allows a high degree of control over olefin selectivity.
  • EP-A-0325437 describes and claims a process for regenerating a coke-contaminated fluid cracking catalyst in a regeneration zone at a pressure in the range from above 240 kPa to 446 kPa and a temperature in the range from 650°C to 815°C while injecting the regeneration zone with enough oxygen-containing regeneration gas to maintain a dense fluid bed of regeneration catalyst, and regenerate the catalyst before returning it to a fluid cracker, comprising,
  • the process comprises withdrawing a controlled stream of spent catalyst from the fluid cracker and introducing the spent catalyst directly into the dehydrogenation zone, and transporting the cooled catalyst for flow-controlled introduction into a riser of the fluid cracker, in the lower portion thereof, and in addition, introducing a minor amount relative to the alkanes, of steam into the dehydrogenation zone, the amount being sufficient, in combination with the alkanes to strip hydrocarbons remaining in the spent catalyst.
  • the present invention provides an integrated catalytic cracking and alkane-dehydrogenation process according to claim 1.
  • the catalytic cracking catalyst may comprise a zeolite crystalline framework oxide.
  • the feed may comprise at least one component selected from the group consisting of ethane, propane, butane, pentane, hexane, heptane, octane, nonane, decane, isobutane, isopentanes, isohexanes, isoheptanes and iso-octanes.
  • the dehydrogenation catalyst may comprise from 0.2-10 wt% carbon.
  • the alkane feed may be dehydrogenated to an olefin product stream which comprises at least 1 wt% total olefin.
  • the reactivated catalytic cracking catalyst may comprise less than about 0.2 wt% carbon.
  • the dehydrogenation of the alkane feed stream with the dehydrogenation catalyst may form a coked dehydrogenation catalyst, and the coked dehydrogenation catalyst may be regenerated under regeneration conditions in the plug flow regeneration system.
  • the plug flow regeneration system may comprise a tubular or empty tower regenerator.
  • the process may comprise performing step (a) using fully-regenerated catalyst from step (b). Spent catalyst from step (c) may be passed to the plug-flow regenerator for regeneration.
  • Fig. 1 is a schematic representation of an embodiment of the invention.
  • Catalytic cracking is a process which is well known in the art of petroleum refining and generally refers to converting a large hydrocarbon molecule to a smaller hydrocarbon molecule by breaking at least one carbon to carbon bond.
  • large paraffin molecules can be cracked to a paraffin and an olefin, and a large olefin molecule can be cracked to two or more smaller olefin molecules.
  • Long side chain molecules which may be present on aromatic rings or naphthenic rings can also be cracked.
  • a coked catalytic cracking catalyst can be used to enhance the dehydrogenation of an alkane feed stream to produce an olefin stream.
  • this aspect of the invention can be integrated into the catalytic cracking process to increase olefin yield in the overall reaction scheme.
  • This increased olefin yield is advantageous since the olefin product can be used as a feedstock in other reaction processes to either increase the octane pool in a refinery, or the olefins can be used in the manufacture of gasoline additives which are required to reduce undesirable hydrocarbon emissions.
  • the process of this invention allows for high olefin selectivity such that a portion of the olefin stream can also be used in other chemicals processes such as polyolefin production.
  • the hydrocarbon feed is preferably a petroleum hydrocarbon.
  • the hydrocarbon is preferably a distillate fraction having an initial ASTM boiling range of about 400°F (204.4°C).
  • Such hydrocarbon fractions include gas oils, thermal oils, residual oils, cycle stocks, topped and whole crudes, tar sand oils, shale oils, synthetic fuels, heavy hydrocarbon fractions derived from the destructive hydrogenation of coal, tar, pitches, asphalts, and hydrotreated feed stocks derived from any of the foregoing.
  • the hydrocarbon feed is preferably introduced into a riser which feeds a catalytic cracking reactor vessel.
  • the feed is mixed in the riser with catalytic cracking catalyst that is continuously recycled.
  • the hydrocarbon feed can be mixed with steam or an inert type of gas at such conditions so as to form a highly atomized stream of a vaporous hydrocarbon-catalyst suspension.
  • this suspension flows through the riser into the reactor vessel.
  • the reactor vessel is preferably operated at a temperature of about 800-1200°F (426.7 to 648.9°C) and a pressure of about 0-100 psig (1.014 to 7.910 bar).
  • the catalytic cracking reaction is essentially quenched by separating the catalyst from the vapor.
  • the separated vapor comprises the cracked hydrocarbon product, and the separated catalyst comprises a carbonaceous material (i.e., coke) as a result of the catalytic cracking reaction.
  • the coked catalyst is preferably recycled to contact additional hydrocarbon feed after the coke material has been removed.
  • the coke is removed from the catalyst in a regenerator vessel by combusting the coke from the catalyst under standard regeneration conditions.
  • the coke is combusted at a temperature of about 900-1400°F (482.2 to 760°C) and a pressure of about 0-100 psig (1.014 to 7.910 bar).
  • the regenerated catalyst is recycled to the riser for contact with additional hydrocarbon feed.
  • the catalyst which is used in this invention can be any catalyst which is typically used to catalytically "crack" hydrocarbon feeds. It is preferred that the catalytic cracking catalyst comprise a crystalline tetrahedral framework oxide component. This component is used to catalyze the breakdown of primary products from the catalytic cracking reaction into clean products such as naphtha for fuels and olefins for chemical feedstocks.
  • the crystalline tetrahedral framework oxide component is selected from the group consisting of zeolites, tectosilicates, tetrahedral aluminophophates (ALPOs) and tetrahedral silicoaluminophosphates (SAPOs). More preferably, the crystalline framework oxide component is a zeolite.
  • Zeolites which can be employed in accordance with this invention include both natural and synthetic zeolites. These zeolites include gmelinite, chabazite, dachiardite, clinoptilolite, faujasite, heulandite, analcite, levynite, erionite, sodalite, cancrinite, nepheline, lazurite, scolecite, natrolite, offretite, mesolite, mordenite, brewsterite, and ferrierite.
  • zeolites X, Y, A, L, ZK-4, ZK-5, B, E, F, H, J, M, Q, T, W, Z, alpha and beta, ZSM-types and omega are included among the synthetic zeolites.
  • aluminosilicate zeolites are effectively used in this invention.
  • the aluminum as well as the silicon component can be substituted for other framework components.
  • the aluminum portion can be replaced by boron, gallium, titanium or trivalent metal compositions which are heavier than aluminum. Germanium can be used to replace the silicon portion.
  • the catalytic cracking catalyst used in this invention can further comprise an active porous inorganic oxide catalyst framework component and an inert catalyst framework component.
  • an active porous inorganic oxide catalyst framework component Preferably, each component of the catalyst is held together by attachment with an inorganic oxide matrix component.
  • the active porous inorganic oxide catalyst framework component catalyzes the formation of primary products by cracking hydrocarbon molecules that are too large to fit inside the tetrahedral framework oxide component.
  • the active porous inorganic oxide catalyst framework component of this invention is preferably a porous inorganic oxide that cracks a relatively large amount of hydrocarbons into lower molecular weight hydrocarbons as compared to an acceptable thermal blank.
  • a low surface area silica e.g., quartz
  • the extent of cracking can be measured in any of various ASTM tests such as the MAT (microactivity test, ASTM # D3907-8). Compounds such as those disclosed in Greensfelder. B. S., et al. , Industrial and Engineering Chemistry , pp. 2573-83, Nov. 1949, are desirable.
  • Alumina, silica-alumina and silica-alumina-zirconia compounds are preferred.
  • the inert catalyst framework component densifies, strengthens and acts as a protective thermal sink.
  • the inert catalyst framework component used in this invention preferably has a cracking activity that is not significantly greater than the acceptable thermal blank.
  • Kaolin and other clays as well as ⁇ -alumina, titania, zirconia, quartz and silica are examples of preferred inert components.
  • the inorganic oxide matrix component binds the catalyst components together so that the catalyst product is hard enough to survive interparticle and reactor wall collisions.
  • the inorganic oxide matrix can be made from an inorganic oxide sol or gel which is dried to "glue" the catalyst components together.
  • the inorganic oxide matrix will be comprised of oxides of silicon and aluminum. It is also preferred that separate alumina phases be incorporated into the inorganic oxide matrix.
  • Species of aluminum oxyhydroxides- ⁇ -alamina, boehmite, diaspore, and transitional aluminas such as ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, and ⁇ -alumina can be employed.
  • the alumina species is an aluminum trihydroxide such as gibbsite, bayerite, nordstrandite, or doyelite.
  • an olefin reaction is commenced by contacting an alkane feed stream with a dehydrogenation catalyst.
  • the alkane feed stream of this invention is preferably a C 2 -C 10 alkane composition.
  • the alkane composition can be either branched or unbranched.
  • Such compositions include ethane. propane, butane, pentane, hexane, heptane, octane, nonane, decane, isobutane, isopentanes, isohexanes, isoheptanes and iso-octanes.
  • a coked catalytic cracking catalyst serves as the dehydrogenation catalyst.
  • the coked catalytic cracking catalyst is a catalytic cracking catalyst, as described above, which contains a measurable content of carbonaceous material (i.e., coke) on the catalyst, and which will effectively enhance dehydrogenation of the alkane feed stream to selectively form an olefin product.
  • the carbon content of the dehydrogenation catalyst will be in a range of from about 0.2-10 wt %, more preferably from about 0.3-5.0 wt %, most preferably from about 0.4-2.5 wt %.
  • the dehydrogenation catalyst can be obtained by any of numerous means. Such means are the subject-matter of further applications EP-A-0 654 519, EP-A-0 564 521, EP-A-0 564 522 and EP-A-0 654 523, all having the same filing date.
  • the dehydrogenation catalyst can be obtained as a result of a partial or incomplete regeneration of at least a portion of the spent catalyst stream in a FCC unit.
  • One of ordinary skill in the art will be able to attain the desired concentration of coke on the catalytic cracking catalyst using well known means of adjusting temperature, oxygen content or burn time within the regenerator portion of the FCC unit.
  • the conversion of alkane to olefin in this invention generally involves a dehydrogenation reaction.
  • alkanes are converted to olefins and molecular hydrogen.
  • This reaction is highly endothermic.
  • the dehydrogenation reaction is carried out at a temperature in a range of from about 800-1600°F (426.7 to 871.1 °C), more preferably about 800-1400°F (426.7 to 760°C).
  • the dehydrogenation reaction is somewhat dependent upon pressure. In general, the higher the pressure, the lower the conversion of alkane to olefin. Preferably, the process is carried out at about 0-100 psig (1.014 to 7.910 bar).
  • the contact time between the alkane stream and the dehydrogenation catalyst will also affect the yield of olefin product.
  • optimal contact between the coked catalyst and the alkane stream is attained when the olefin product stream contains a concentration of at least about 1 wt % total iso-olefin.
  • alkane vapor residence time will be in a range of from about 0.5-10 seconds, more preferably, about 1.0-5.0 seconds.
  • Fig. 1 An embodiment of this invention is shown in Fig. 1 in which the dehydrogenation reaction is incorporated into a catalytic cracking process.
  • a petroleum hydrocarbon is catalytically cracked with an active catalytic cracking catalyst to form a cracked hydrocarbon product.
  • the active catalytic cracking catalyst becomes coked (i.e., coated with a carbonaceous material).
  • the activity of the catalytic cracking catalyst decreases as the concentration of the coke deposited on the catalyst increases.
  • the catalytic cracking catalyst is deactivated to the point where the catalyst is essentially ineffective in enhancing the equilibrium balance of the cracking reaction under the standard cracking conditions. At this point. the catalytic cracking catalyst is considered to be a deactivated cracking catalyst.
  • the deactivated cracking catalyst can be reactivated by regenerating the catalyst under standard regeneration conditions.
  • part of the deactivated catalyst can be regenerated and reused as the dehydrogenation catalyst.
  • part of the deactivated catalyst can be fully reactivated and reused in a continuous catalytic cracking reaction.
  • regeneration and recovery of a plurality of catalyst streams need be performed in only one regenerator vessel.
  • the plug flow regeneration system of this invention comprises a regenerator in which there is little or no significant back mixing of the reaction mixture, including catalyst components.
  • the plug flow regenerator is of a tubular or empty tower design which provides for effectively overall laminar flow of the reaction mixture.
  • regenerators are of the same type of general configuration as typical tubular and tower reactors, such as those described in Perry's Chemical Engineers' Handbook , sixth edition, McGraw-Hill, 1984.
  • the plug flow regenerator has means for distributing an oxygen containing stream throughout the entire length of the regenerator. This will provide a balanced flow of oxygen within the regenerator to evenly combust carbonaceous material from the deactivated cracking catalyst. Since there is no significant back mixing, the amount of carbon material combusted from the spent catalyst increases as the catalyst progressively flows through the regeneration system. Therefore. the amount of carbonaceous material that is desired to be removed from the deactivated catalyst can be primarily controlled by the residence time within the regenerator as long as the other operating conditions remain relatively constant. Residence times can be selected according to the amount of carbon material that is desired to be removed.
  • At least two regenerated streams are recovered requiring at least two different residence times.
  • One regenerated stream is partially regenerated for use as a dehydrogenation catalyst, and another regeneration stream is a fully regenerated catalyst.
  • the partially regenerated catalyst has a carbon content of about 0.2-10 wt %
  • the fully reactivated catalyst has a carbon content of less than about 0.2 wt%, based on the total weight of the catalyst.
  • FIG. 1 A preferred embodiment is shown in Fig. 1 in which the integrated catalytic cracking and alkane dehydrogenation process takes place generally in a FCC unit 10 which includes a tubular or empty tower plug flow regenerator 11, a cracking reactor 12 and a satellite reactor 13.
  • the cracking reactor 12 comprises a main reactor vessel and preferably includes a riser conduit where hydrocarbon feed is injected and initially contacts reactivated catalytic cracking catalyst from the plug flow regenerator 11.
  • the catalytic cracking reaction is initiated as the hydrocarbon feed contacts the catalyst, and continues until the catalyst is separated from the hydrocarbon, typically within the cracking reactor 12. Separation can be accomplished using any of the acceptable FCC separation devices such as cyclone separators.
  • the cracked hydrocarbon product leaves the reactor 12 through a product line 14.
  • the separated catalyst which has become coked (i.e.. spent) in the cracking reaction, leaves the reactor 12 through a recycle line 15 where the catalyst is sent to the plug flow regenerator 11.
  • the plug flow regenerator 11 preferably includes a series of injection means 16a-d for distributing an oxygen containing stream evenly throughout the plug flow regenerator 11 to minimize back mixing.
  • injection means 16a-d for distributing an oxygen containing stream evenly throughout the plug flow regenerator 11 to minimize back mixing.
  • any of various designs for injecting an oxygen containing stream can be used as long as back mixing is kept to a minimum.
  • the satellite reactor 13 can be any type of reactor vessel that is operable under dehydrogenation conditions.
  • the satellite reactor 13 can be a transfer line riser reactor, a slumped bed reactor, a spouting bed reactor or a moving bed reactor.
  • the satellite reactor 13 will be capable of supporting a fluid bed catalyst at a density in a range of from about 1-45 lbs of catalyst per cubic foot (16.02 to 720.84 kg catalyst/m 3 ) of reactor volume.
  • alkane feed is injected to initiate the dehydrogenation reaction.
  • the reaction continues until the catalyst is separated from the olefin products within the satellite reactor 13. Separation can be accomplished using any of the acceptable fluidized type of catalyst separation devices such as cyclone separators.
  • the olefin product leaves the satellite reactor 13 through an olefin product line 18.
  • the separated catalyst which is further spent in the dehydrogenation reaction leaves the reactor 13 through a recycle line 19 where it is combined with the spent catalyst in the recycle line 15 and sent back to the plug flow regenerator 11 to repeat the cycle.
  • EXAMPLE 1 illustrates the suitability of partially-coked cracking catalyst for use in dehydrogenating alkanes to yield olefin-containing products.
  • An equilibrium zeolite beta FCC catalyst (SiO 2 65.1 wt %; Al 2 O 3 wt %; Na 2 O 0.28 wt %; REO 2 2.14 wt %) was placed in a fixed bed quartz reactor. The temperature of the reactor was maintained at 1250°F (676.7°C), and the pressure was maintained at 0 psig (0 bar gauge). Six runs were made varying the total carbon content on the catalyst from 0.2 wt % to 2.7 wt %. The catalyst in runs 2-6 was pretreated with a hydrocarbon to increase the base level carbon content, thereby representing a partially regenerated spent catalyst. Iso-butane feed was passed through the reactor at 1 second residence time and GHSV of 1066.
  • EXAMPLE 2 illustrates partial regeneration of spent (coked) catalyst in a plug flow regenerator.
  • Spent zeolite catalytic cracking catalyst is passed through a tubular plug flow regenerator, which is operated at 1 atm (1.014 bar gauge) and 1280°F (693.3°C). At various residence times within the regenerator, cracking catalyst is recovered and the amount of carbon material removed during the regeneration process is calculated. The results are shown in Table 1. Time. min. wt % coke removed 0 0 1.25 43.8 2.5 74.0 3.75 86.3 5.0 92.3

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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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Claims (10)

  1. Integriertes katalytisches Crack- und Alkan-Dehydrierungsverfahren, das die folgenden Schritte umfaßt:
    (a) katalytisches Cracken eines Erdölkohlenwasserstoffs mit einem aktiven katalytischen Crackkatalysator, um ein gecracktes Kohlenwasserstoffprodukt und deaktivierten Crackkatalysator zu bilden,
    (b) Führen des deaktivierten Katalysators in ein Pfropfenströmungsregenerationssystem und separate Gewinnen daraus eines partiell regenerierten Katalysators, der als Alkan-Dehydrierungskatalysator brauchbar ist, und eines vollständig regenerierten Katalysators, der als Erdölkohlenwasserstoffcrackkatalysator brauchbar ist,
    (c) Dehydrieren eines Einsatzmaterials, das ein oder mehrere C2- bis C10-Alkane umfaßt, wobei in Schritt (b) gewonnener partiell regenerierter Katalysator verwendet wird.
  2. Verfahren nach Anspruch 1, bei dem der katalytische Crackkatalysator ein kristallines Zeolithgerüstoxid umfaßt.
  3. Verfahren nach Anspruch 1 oder Anspruch 2, bei dem das Einsatzmaterial mindestens eine Komponente ausgewählt aus der Gruppe bestehend aus Ethan, Propan, Butan, Pentan, Hexan, Heptan, Octan, Nonan, Decan, Isobutan, Isopentanen, Isohexanen, Isoheptanen und Isooctanen umfaßt.
  4. Verfahren nach einem der vorhergehenden Ansprüche, bei dem der Dehydrierungskatalysator 0,2 bis 10 Gew.-% Kohlenstoff umfaßt.
  5. Verfahren nach einem der vorhergehenden Ansprüche, bei dem das Alkaneinsatzmaterial zu einem Olefinproduktstrom dehydriert wird, der insgesamt mindestens 1 Gew.-% an Olefin umfaßt.
  6. Verfahren nach einem der vorhergehenden Ansprüche, bei dem der reaktivierte katalytische Crackkatalysator weniger als etwa 0,2 Gew.-% Kohlenstoff umfaßt.
  7. Verfahren nach einem der vorhergehenden Ansprüche, bei dem die Dehydrierung des Alkaneinsatzmaterialstroms mit dem Dehydrierungskatalysator einen verkokten Dehydrierungskatalysator bildet und der verkokte Dehydrierungskatalysator unter Regenerationsbedingungen in dem Pfropfenstömungsregenerationssystem regeneriert wird.
  8. Verfahren nach einem der vorhergehenden Ansprüche, bei dem das Pfropfenströmungsregenerationssystem einen Rohr- oder leeren Turm-Regenerator umfaßt.
  9. Verfahren nach einem der vorhergehenden Ansprüche, bei dem Schritt (a) unter Verwendung von vollständig regeneriertem Katalysator aus Schritt (b) durchgeführt wird.
  10. Verfahren nach einem der Ansprüche 1 bis 9, bei dem verbrauchter Katalysator aus Schritt (c) zu dem Pfropfenströmungsregenerator für die Regeneration geführt wird.
EP19940308423 1993-11-19 1994-11-15 Integriertes katalytisches Krack- und Olefinen Herstellungsverfahren Expired - Lifetime EP0654520B1 (de)

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US15482993A 1993-11-19 1993-11-19
US154829 1993-11-19

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3894935A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US4554260A (en) * 1984-07-13 1985-11-19 Exxon Research & Engineering Co. Two stage process for improving the catalyst life of zeolites in the synthesis of lower olefins from alcohols and their ether derivatives
JPS6384632A (ja) * 1986-09-03 1988-04-15 モービル・オイル・コーポレイション 流動接触分解方法
US4840928A (en) * 1988-01-19 1989-06-20 Mobil Oil Corporation Conversion of alkanes to alkylenes in an external catalyst cooler for the regenerator of a FCC unit
US4968401A (en) * 1988-06-27 1990-11-06 Mobil Oil Corp. Aromatization reactor design and process integration
CA2097219A1 (en) * 1992-06-18 1993-12-19 Michael C. Kerby, Jr. Process for the dehydrogenation of hydrocarbons using a carbonaceous catalyst

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CA2135102C (en) 2004-05-25
CA2135102A1 (en) 1995-05-20
DE69419872T2 (de) 2000-04-20
EP0654520A1 (de) 1995-05-24
DE69419872D1 (de) 1999-09-09

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