WO1998056740A1 - Systeme multireacteur de production amelioree d'olefines legeres - Google Patents

Systeme multireacteur de production amelioree d'olefines legeres Download PDF

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Publication number
WO1998056740A1
WO1998056740A1 PCT/US1998/011874 US9811874W WO9856740A1 WO 1998056740 A1 WO1998056740 A1 WO 1998056740A1 US 9811874 W US9811874 W US 9811874W WO 9856740 A1 WO9856740 A1 WO 9856740A1
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zsm
effluent
zeolite
catalyst
range
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PCT/US1998/011874
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English (en)
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J. F. Carpency
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Exxon Chemical Patents Inc.
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Priority to AU79563/98A priority Critical patent/AU7956398A/en
Publication of WO1998056740A1 publication Critical patent/WO1998056740A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • 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
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/18—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/50—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the eroionite or offretite type, e.g. zeolite T
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/65—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/86—Borosilicates; Aluminoborosilicates
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/87—Gallosilicates; Aluminogallosilicates; Galloborosilicates
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/88—Ferrosilicates; Ferroaluminosilicates
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/89—Silicates, aluminosilicates or borosilicates of titanium, zirconium or hafnium
    • 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

  • the invention provides a process for increasing yield of ethylene and propylene in a catalytic cracking process by use of a thermal cracking step before catalytic cracking.
  • Zeolites are complex crystalline aluminosilicates which form a network of AIO 4 and SiO 4 tetrahedra linked by shared oxygen atoms.
  • the negative charge of the tetrahedra is balanced by the inclusion of protons or cations such as alkali or alkaline earth metal ions.
  • the interstitial spaces or channels formed by the crystalline network enable zeolites to be used as molecular sieves in separation processes.
  • the ability of zeolites to adsorb materials also enables them to be used in catalysis. There are a large number of both natural and synthetic zeolitic structures.
  • Typical catalysts include ZSM-5 zeolite described and claimed in U.S. Pat. No. 3,702,886, and ZSM-11 described in U.S. Pat. No. 3,709,979, and the numerous variations on these catalysts disclosed and claimed in later patents.
  • GB 2,105,362 teaches a two stage thermal cracking process in a catalyst free system wherein the first reaction zone heats the steam/feedstock from 800°C to 1000°C and then passes the feedstock to a second catalyst free zone where it is heated 850°C to 1150°C.
  • Mauleon et al., U.S. Patent Nos. 5,506,365 and 5,264,115 teach a multiple zone process wherein hot catalyst is used in a mild steam thermal cracking process and reacted further downstream with additional catalyst at a lower temperature in a process aimed at gasoline production. Mao, U.S.
  • Patent 4,732,881 teaches steam cracking of hydrocarbons (propane is exemplified) followed by contact with a multi-component zeolite- containing catalyst comprising a zeolite of the ZSM-5 type coupled with a metallic oxide having a hydrogenation/dehydrogenation function.
  • the thermal cracking unit is operated at a higher temperature than the downstream catalytic cracker.
  • Adams, U.S. Patent No. 3,360,587 also teaches a steam cracking step followed by a catalytic cracker, again the catalytic cracker is at a lower temperature than the upstream thermal cracker.
  • the present invention provides a process for improving the conversion of a hydrocarbon feedstock to light olefins comprising a catalyst-free thermal cracking step followed by contacting the effluent from the thermal cracking step with a light olefin-producing cracking catalyst comprising a zeolite free of added metal oxides having hydrogenation/dehydrogenation functions, in a catalyst contact zone.
  • Light naphtha means a hydrocarbon fraction that is predominantly C 5 to C 7 hydrocarbons.
  • “Virgin naphtha” means a hydrocarbon fraction obtained from crude oil or natural gas without additional conversion processing.
  • Cat naphtha means a refinery distillate fraction obtained by catalytic cracking of a heavier hydrocarbon fraction.
  • BTX means a mixture containing benzene, toluene, and xylenes.
  • Light olefins or “prime olefins” means ethylene, propylene or mixtures thereof.
  • Improved conversion means producing an increase in production that is a greater yield within the precision of the measurement system over cracking the same feedstock in a thermal cracking step alone.
  • Hydrocarbon feedstock means a stream comprising one or more hydrocarbons to be broken into fragments by thermal, chemical or catalytic action, the fragments forming light olefins.
  • Substantial amounts of ethylene and propylene can be produced by cracking refining or chemical feedstocks such as light cat naphtha (LCN) or light virgin naphtha (LVN) over catalysts; particularly zeolite containing catalysts such as those which contain ZSM-5.
  • the present invention provides a method for enhancing ethylene and propylene yields which comprises thermal cracking a hydrocarbon feedstream followed by contacting the effluent from the thermal cracking step with an acidic zeolite catalyst free of added metal oxides having hydrogenation/dehydrogenation functions.
  • the key to the invention is separating the ethylene generation reactor from a downstream catalytic reactor or reactors that takes the effluent of the first reactor and runs it at different conditions in order to enhance further overall light olefin (ethylene plus propylene) make.
  • the downstream catalytic reaction also results in a significant reduction in the amount of acetylenes and diolefins produced in the overall reaction system, which has additional benefits in the downstream olefins recovery process.
  • An example of the process is as follows where the thermal cracking is carried out in a conventional steam cracking furnace.
  • a steam cracking hydrocarbon feedstock is fed to a steam cracking furnace in the presence of steam (usually between 0.2 and 0.5 wt steam/wt hydrocarbon feedstock), and is run to a coil outlet temperature of between 760°C and 860°C.
  • Suitable hydrocarbon feedstocks for a steam cracking furnace when practicing the present invention would include any feedstock typically feeding steam crackers. Examples are ethane, propane, butane, naphthas, gasoils, Fischer- Tropsch liquids, raffinates, field natural gasolines, petrolatum, waxes, and vacuum gasoils.
  • the reactor effluent needs to be quickly quenched via quench hydrocarbon injection and/or heat removal via transfer line exchangers typical in a steam cracker to lower the temperature to about 600°C to 720°C in order to mitigate unwanted reactions that would result in lowering the ethylene yield.
  • any hydrocarbon may be used as a quench hydrocarbon to lower temperature, although the preferred quench hydrocarbon would come from the group of normal steam cracking feedstocks such as ethane, propane, butane, naphthas, gasoils, Fischer-Tropsch liquids, and streams containing olefins or diolefins such as butenes, butadiene, steam cracked naphtha, cat cracked naphtha, and coker naphtha. More preferred quench hydrocarbon materials are light cat naphtha (LCN), unhydrogenated C 4 or C 5 from normal steam cracker effluent, or portions of the effluent from the process of this invention as a recycle, or light virgin naphtha (LVN).
  • LPN light cat naphtha
  • the amount of quenching accomplished with direct injection of quench hydrocarbon versus the amount done with heat removal may be determined by one skilled in the art as a function of the amount of additional hydrogen required, which is further a function of the hydrocarbon feed to the first reactor and its operating conditions, as well as the desired temperature in the downstream reactor(s). A further consideration would be the availability of suitable quench hydrocarbon material.
  • the effluent from the first reactor after quenching then enters the downstream catalytic reactor(s).
  • the purpose of this reactor is to make additional ethylene and/or propylene out of the reactive species (namely C 2 + paraffins, C 2 + acetylenes, C 3 + diolefins, C 4 + olefins, and C 5 + naphthenes) remaining in the first reactor effluent, as well as the hydrocarbon material used as quench.
  • the catalytic reactor or reactors can be fixed bed, moving bed, fluidized bed, such as a riser or dense fluid bed system or stationary fluid bed system, although the present invention is not limited to these types of reactors.
  • ethylene generation reactors such as steam cracking furnaces and the downstream catalytic reactor(s); for example, it is possible to an ethylene generation reactor feeding numerous downstream catalytic reactors.
  • the temperature in this downstream catalytic reactor(s) is optimized to achieve different ratios of ethylene to propylene as desired, with a normal operating temperature range in the range of about 500°C to 750°C; more preferably in the range of 550°C to 725°C; most preferably in the range of 600°C to 700°C.
  • the thermal step is carried out within the range of 700°C to 1000°C; more preferably in the range of 720°C to 900°C.
  • the residence time is maintained in the range of 0.02 to 20 seconds, preferably 0.05 to 5 seconds, and most preferably for 0.1 to 1 seconds.
  • the catalyst contacting process is preferably carried out at a weight hourly space velocity (WHSV) in the range of about 0.1 Hr 1 WHSV to about 100 Hr 1 WHSV, more preferably in the range of about 1.0 Hr 1 WHSV to about 50 Hr 1 WHSV, and most preferably in the range of about 10 Hr 1 WHSV to about 40 Hr 1 WHSV.
  • WHSV weight hourly space velocity
  • Any cracking catalyst free of added metal oxides having hydrogenation/dehydrogenation functions that is operable to selectively produce prime olefins may be used in the catalytic cracking step after the thermal cracking step.
  • Suitable zeolites for use as the cracking catalyst are typically the acid form of any of the naturally-occurring or synthetic crystalline zeolites, especially those having a silica to alumina molar ratio within the range of about 2.0:1 to 2000:1.
  • zeolites useful in the claimed process include gallium silicate zeolite, zeolite beta, zeolite rho, ZK5, titanosilicate zeolite, ferrosilicate zeolite, borosilicate zeolite, zeolites designated by the Linde Division of Union Carbide by the letters of X, Y, A, L (these zeolites are described in U.S. Pat. Nos.
  • Such medium and small pore zeolites are considered to have a Constraint Index from about 1 to about 12.
  • the method by which Constraint Index is determined is described fully in U.S. Pat. No. 4,016,218.
  • Zeolites which conform to the specified values of Constraint Index for medium pore zeolites include ZSM-5, ZSM-11 , ZSM-5/ZSM-11 intermediate, ZSM-12, ZSM- 21 , ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-50, MCM-22 and zeolite Beta which are described, for example, in U.S. Pat. Nos. 3,702,886 and Re. No.
  • zeolites may be produced with differing silica to alumina molar ratios ranging from 12:1 upwards. They have been, in fact, produced from reaction mixtures from which alumina is intentionally excluded, so as to produce materials having extremely high silica to alumina ratios which, in theory at least, may extend up to infinity.
  • Preferred medium pore zeolites include ZSM-5, ZSM- 11 , ZSM-12, ZSM-35 and MCM-22. Particularly preferred is ZSM-5.
  • Small pore zeolites include such crystalline aluminosilicate zeolites as erionite, chabazite, ferrierite, heulandite, phillipsite, and such synthetic counterparts thereof as zeolites A and ZK5, as described in U.S. Pat. Nos. 2,882,243 and 3,247,195, respectively.
  • the zeolite catalyst is selected from the group consisting of faujasite, chabazite, erionite, mordenite, offretite, gmelinite, analcite, phillipsite, ZSM-5, ZSM-11 , ZSM-5/ZSM-11 intermediate, ZSM-12, ZSM-21 , ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-50, MCM-22, gallium silicate zeolite, zeolite Beta, zeolite rho, ZK5, titanosilicate, and zeolites having a silica to alumina ratio within the range of about 2.0:1 to 2000:1 ferrosilicate; borosilicate and zeolites designated by the Linde Division of Union Carbide by the letters of X, Y, and A.
  • An especially favored zeolite is ZSM-5.
  • a blend of model compounds consisting of hydrogen, methane, ethylene, ethane, propylene, butenes, butadiene, hexane and benzene was used to simulate the effluent from a steam cracking step.
  • a first run was conducted at 680°C, 24 Hr 1 WHSV over a fixed bed of 0.6 g ZCAT40, a ZSM-5 zeolite catalyst commercially available from Intercat. Inc., of Sea Girt, New Jersey. Prior to the cracking tests, ZCAT40 was steamed with 100% steam at 704°C and 1 atmosphere for 16 hours for the purpose of aging the catalyst..
  • a second run under the same conditions treated the same model compound blend spiked with additional hexane to simulate a hydrocarbon quenching stream.
  • steam to hydrocarbon weight ratio was 0.33.
  • the effluent stream was analyzed by on-line gas chromatography. A column having a length of 60m packed with fused silica was used for the analysis.
  • the GC used was a dual FID Hewlett-Packard Model 5880. The results are tabulated below.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un procédé d'amélioration de la conversion d'une charge d'alimentation d'hydrocarbures en oléfines légères comprenant les étapes consistant à convertir thermiquement la charge d'alimentation d'hydrocarbures afin de produire un effluent, à refroidir rapidement l'effluent pour produire un effluent refroidi, et à mettre l'effluent refroidi en contact avec un catalyseur de craquage producteur d'oléfines légères. Le craquage thermique d'équilibre est exécuté entre 700 °C et 1000 °C pendant 0,1 à 20 secondes. Le catalyseur de craquage de production d'oléfines légères est un catalyseur à zéolite exempt d'oxyde métallique ajouté ayant une fonction d'hydrogénation/déshydrogénation, et il est mis en contact à une température comprise dans la plage allant d'environ 500 °C à environ 750 °C. Les flux de charge d'alimentation vont à une vitesse spatiale horaire pondérale comprise dans la plage allant d'environ 0,1 Hr-1 WHSV à environ 100 Hr-1 WHSV.
PCT/US1998/011874 1997-06-10 1998-06-08 Systeme multireacteur de production amelioree d'olefines legeres WO1998056740A1 (fr)

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AU79563/98A AU7956398A (en) 1997-06-10 1998-06-08 Multi-reactor system for enhanced light olefin make

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US87253797A 1997-06-10 1997-06-10
US08/872,537 1997-06-10

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1061118A1 (fr) * 1999-06-17 2000-12-20 Fina Research S.A. Production d' oléfines
EP1063274A1 (fr) * 1999-06-17 2000-12-27 Fina Research S.A. Production d'oléfines
WO2001051590A1 (fr) * 2000-01-12 2001-07-19 Mg Technologies Ag Procede de production d'olefines c2 et c3 a partir d'hydrocarbures
US6867341B1 (en) 2002-09-17 2005-03-15 Uop Llc Catalytic naphtha cracking catalyst and process
US6872752B2 (en) 2003-01-31 2005-03-29 Chevron U.S.A. Inc. High purity olefinic naphthas for the production of ethylene and propylene
US6933323B2 (en) 2003-01-31 2005-08-23 Chevron U.S.A. Inc. Production of stable olefinic fischer tropsch fuels with minimum hydrogen consumption
US7150821B2 (en) 2003-01-31 2006-12-19 Chevron U.S.A. Inc. High purity olefinic naphthas for the production of ethylene and propylene
US7431821B2 (en) 2003-01-31 2008-10-07 Chevron U.S.A. Inc. High purity olefinic naphthas for the production of ethylene and propylene
EP2336275A1 (fr) * 2008-09-17 2011-06-22 Asahi Kasei Chemicals Corporation Procédé de production d'oléfines et appareil utilisable à cet effet
US10099210B2 (en) 2013-04-29 2018-10-16 Saudi Basic Industries Corporation Catalytic methods for converting naphtha into olefins
US20190023998A1 (en) * 2017-07-18 2019-01-24 Lummus Technology Llc Integrated thermal cracking and dehydrogenation process for olefin production
WO2019162392A1 (fr) 2018-02-22 2019-08-29 Total Research & Technology Feluy Conversion sélective de naphta paraffinique en propane en présence d'hydrogène
CN110997876A (zh) * 2017-07-18 2020-04-10 鲁姆斯科技有限责任公司 烯烃生产的一体化热裂化和催化裂化

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US3973832A (en) * 1973-01-30 1976-08-10 Minolta Camera Kabushiki Kaisha Retro-focus type wide angle lens system
EP0109059A1 (fr) * 1982-11-10 1984-05-23 MONTEDIPE S.p.A. Procédé pour convertir des oléfines ayant de 4 à 12 atomes de carbone en propène
US4732881A (en) * 1986-09-25 1988-03-22 The Abestos Institute Catalysts for up-grading steam-cracking products
EP0511013A2 (fr) * 1991-04-26 1992-10-28 ARCO Chemical Technology, L.P. Fabrication d'oléfines

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3973832A (en) * 1973-01-30 1976-08-10 Minolta Camera Kabushiki Kaisha Retro-focus type wide angle lens system
EP0109059A1 (fr) * 1982-11-10 1984-05-23 MONTEDIPE S.p.A. Procédé pour convertir des oléfines ayant de 4 à 12 atomes de carbone en propène
US4732881A (en) * 1986-09-25 1988-03-22 The Abestos Institute Catalysts for up-grading steam-cracking products
EP0511013A2 (fr) * 1991-04-26 1992-10-28 ARCO Chemical Technology, L.P. Fabrication d'oléfines

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6410813B1 (en) 1999-06-17 2002-06-25 Fina Research, S.A. Production of olefins
EP1061118A1 (fr) * 1999-06-17 2000-12-20 Fina Research S.A. Production d' oléfines
WO2000078894A1 (fr) * 1999-06-17 2000-12-28 Atofina Research Production d'olefines
WO2001000749A1 (fr) * 1999-06-17 2001-01-04 Atofina Research Productions d'olefines
JP2001031980A (ja) * 1999-06-17 2001-02-06 Fina Res Sa オレフィン類の製造
EP1857526A1 (fr) * 1999-06-17 2007-11-21 Total Petrochemicals Research Feluy Production d'oléfines
EP1063274A1 (fr) * 1999-06-17 2000-12-27 Fina Research S.A. Production d'oléfines
EP1840189A3 (fr) * 1999-06-17 2007-10-10 Total Petrochemicals Research Feluy Production d'oléfines
EP1840189A2 (fr) * 1999-06-17 2007-10-03 Total Petrochemicals Research Feluy Production d'oléfines
CZ302128B6 (cs) * 2000-01-12 2010-11-03 Lurgi Gmbh Zpusob výroby C2- a C3-alkenu z uhlovodíku
WO2001051590A1 (fr) * 2000-01-12 2001-07-19 Mg Technologies Ag Procede de production d'olefines c2 et c3 a partir d'hydrocarbures
US7446071B2 (en) 2002-09-17 2008-11-04 Uop Llc Catalytic naphtha cracking catalyst and process
US7585489B2 (en) 2002-09-17 2009-09-08 Uop Llc Catalytic naphtha cracking catalyst and process
US7314964B2 (en) 2002-09-17 2008-01-01 Uop Llc Catalytic naphtha cracking catalyst and process
US6867341B1 (en) 2002-09-17 2005-03-15 Uop Llc Catalytic naphtha cracking catalyst and process
US7431821B2 (en) 2003-01-31 2008-10-07 Chevron U.S.A. Inc. High purity olefinic naphthas for the production of ethylene and propylene
US7179364B2 (en) 2003-01-31 2007-02-20 Chevron U.S.A. Inc. Production of stable olefinic Fischer-Tropsch fuels with minimum hydrogen consumption
US7150821B2 (en) 2003-01-31 2006-12-19 Chevron U.S.A. Inc. High purity olefinic naphthas for the production of ethylene and propylene
US6933323B2 (en) 2003-01-31 2005-08-23 Chevron U.S.A. Inc. Production of stable olefinic fischer tropsch fuels with minimum hydrogen consumption
US6872752B2 (en) 2003-01-31 2005-03-29 Chevron U.S.A. Inc. High purity olefinic naphthas for the production of ethylene and propylene
EP2336275A1 (fr) * 2008-09-17 2011-06-22 Asahi Kasei Chemicals Corporation Procédé de production d'oléfines et appareil utilisable à cet effet
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WO2019162393A1 (fr) 2018-02-22 2019-08-29 Total Research & Technology Feluy Conversion sélective de naphta paraffinique en propylène en présence d'hydrogène

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