WO1998056873A1 - Hydrocarbon cracking with positive reactor temperature gradient - Google Patents
Hydrocarbon cracking with positive reactor temperature gradient Download PDFInfo
- Publication number
- WO1998056873A1 WO1998056873A1 PCT/US1998/011875 US9811875W WO9856873A1 WO 1998056873 A1 WO1998056873 A1 WO 1998056873A1 US 9811875 W US9811875 W US 9811875W WO 9856873 A1 WO9856873 A1 WO 9856873A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- temperature
- contact zone
- catalyst contact
- zsm
- Prior art date
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Classifications
-
- 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
- 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
- C07C2529/60—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the type L
-
- 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 yields of ethylene and/or propylene in a catalytic cracking process by use of a positive reactor temperature gradient.
- 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.
- Patent No. 4,388,175 discloses a two stage system for production of aromatics from heavy oil. The second stage is operated at a higher temperature than the first to produce light naphtha, gasoline and needle coke. There was no indication of any application to prime olefins production.
- Tabak U.S. Patent No. 4,487,985 and its divisional U.S. Patent No. 4,560,536 teaches oligomerization of lower olefins in a multistage series of reactors wherein catalyst partially inactivated in the primary stage is employed at a higher temperature in a secondary stage prior to catalyst regeneration.
- European Patent Application 0 262 049 teaches steam cracking of hydrocarbons (propane is exemplified) followed by contact with a multi- component zeolite containing catalyst with added metal oxides having a hydrogenation/dehydrogenation function.
- the thermal cracking unit is operated at a higher temperature than the 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.
- 3,702,292 discloses an integrated refinery apparatus wherein various streams are separated and feed to both a hydrocracking unit and a thermal cracking unit.
- Derwent WPI Accession No. 88-053890/08 for Japanese patent 60235890 discloses thermal cracking of hydrocarbons in a two stage system.
- Derwent WPI Accession No. 86-011144/02 for Japanese patent 63010693 discloses feeding by-product light oil containing olefins from a catalytic cracking unit to a thermal cracking furnace with prime olefins recovered in high purity.
- the present invention provides a process for improving the conversion of a hydrocarbon feedstock to light olefins comprising the step of contacting a hydrocarbon feedstock with a cracking catalyst in a reactor operated at a positive temperature gradient.
- the invention provides a process for producing ethylene and propylene in a catalytic cracking process wherein a hydrocarbon feedstock is contacted with a cracking catalyst, the improvement which comprises providing a first catalyst contact zone at a first temperature and providing a second catalyst contact zone at a second temperature downstream from the first catalyst contact zone and maintaining the second catalyst contact zone at a higher temperature than the first catalyst contact zone and passing the cracked hydrocarbon feedstock from the first catalyst contact zone to the second catalyst contact zone.
- the downstream catalyst may be the same or a different catalyst to produce the desired product mix.
- the second embodiment may comprise a plurality of reactor vessels so long as at least one down stream vessel is operated at a higher temperature than an upstream reactor, and both provide catalytic cracking zones.
- Light naphtha means a hydrocarbon distillate fraction that is predominantly C 5 to C 7 hydrocarbons.
- Virtual naphtha means a hydrocarbon distillate fraction obtained from crude oil or natural gas without additional conversion processing.
- Cat naphtha means a hydrocarbon 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.
- Improve conversion means producing an increase in production that is a greater light olefin yield within the precision of the measurement system over cracking the same feedstock with the same catalyst(s) at a constant temperature.
- Hydrocarbon feedstock means a hydrocarbon stream comprising one or more hydrocarbons to be broken into fragments by thermal, chemical or catalytic action, the fragments forming light olefins.
- “Positive temperature gradient” means a temperature change from a lower temperature at a first location to a higher temperature at a second location, the second location being downstream from the first location.
- Substantial amounts of ethylene and propylene are produced by cracking hydrocarbon feedstocks such as light cat naphtha (LCN) or light virgin naphtha (LVN) over catalysts particularly zeolite containing catalysts which contain ZSM-5.
- the present invention provides a method for enhancing ethylene and propylene yields which comprises contacting a feed stream with a catalyst in a reactor bed operated with a positive temperature gradient.
- the feed stream is LCN or LVN, but any catalyst crackable hydrocarbon stream may be used. Any cracking catalyst operable to selectively produce prime olefins may be improved by use of the reactor temperature gradient method.
- 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-alumina ratio within the range of about 2.0:1 to 2000:1.
- any catalyst capable of cracking hydrocarbons to light olefins, having an improved conversion by the use of a temperature gradient is suitable for use in the process.
- zeolites useful in the claimed process include gallium silicate zeolites such as those described in U.S. Patent No. 5,096,686, zeolite beta, zeolite rho, ZK5, titanosilicate, ferrosilicate; 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.
- 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- ⁇ which are described, for example, in U.S. Pat. Nos. 3,702,886 and Re. No. 29,949, 3,709,979, 3,832,449, 4,046,859, 4,556,447, 4,076,842, 4,016,245, 4,229,424, 4,397,827, 4,954,325, 3,308,069, Re.
- 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-22, ZSM-35 and MCM-22. Particularly preferred is ZSM-5.
- Small pore zeolites include such crystalline aluminosilicate zeolites as erionite, chabazite, 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- ⁇ , zeolite-rho, ZK5, and titanosilicate, and zeolites having a silica to alumina molar ratio within the range of about 2.0:1 to 2,000:1 ferrosilicate; borosilicate zeolite such as those described in Belgian Pat.
- the cracking procedure can be carried out with any conventional equipment, which can be a fixed bed, moving bed, fluidized bed, such as a riser or dense fluid bed system or stationary fluid bed system, and with typical hydrocarbon feed streams.
- the catalyst is contacted at a temperature within the range of 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 reactor temperature gradient preferably will be in the range of 10° to 150°C, more preferably in the range of 50°C to 100°C; most preferably in the range of about 60°C to 80°C.
- the gradient may be uniform across a portion of the catalyst bed, where each downstream portion is at a slightly higher temperature than the adjacent upstream portion.
- the gradient may be non-uniform, wherein the temperature of a downstream zone is higher than the temperature of an upstream zone.
- the process is preferably carried out at a weight hourly space velocity (WHSV) in the range of about 0.1 Hr 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, most preferably in the range of about 1.0 Hr 1 WHSV to about 30 Hr 1 WHSV.
- WHSV weight hourly space velocity
- hydrocarbon streams which may be used to obtain high yields of light olefins include 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 and kerosene.
- a preferred feedstock is light cat naphtha (LCN) or light virgin naphtha (LVN).
- An alternative embodiment to a positive temperature gradient within a single reaction vessel is the use of a plurality of reactors in series with at least one down stream reactors maintained at a higher temperature than the upstream reactor.
- one may use several reactors to approximate a uniform gradient, or may make large temperature steps between olefin production reactors.
- the catalyst in each reactor may be the same or different depending on the preferred product mix to be obtained. By choice of catalyst and magnitude of the temperature gradient selection between ethylene and propylene can be improved.
- a series of runs in a small bench reactor was conducted on a light cat naphtha.
- a control run was conducted at 650°C, 1.9 Hr 1 WHSV over a fixed bed of 2.4 g ZCAT40 , a ZSM-5 zeolite catalyst commercially available from Intercat, Inc. of Sea Girt, New Jersey.
- ZCAT40 was steamed with 100% steam, at 704°C and one atmosphere for 16 hours to age the catalyst.
- steam to hydrocarbon weight ratio of 0.85 was used while reactor pressure was controlled at 6 psig.
- the effluent stream was analyzed by on-line gas chromatography.
- the data for key product yields are illustrated in Table 1.
- the 65°C positive temperature gradient results in an increase to 32.0 Wt. % yield for ethylene compared to an average about 26.9 Wt. % at a uniform 650°C.
- the propylene yield in this run is slightly lower, about 21.7 Wt. % compared to 23.2 Wt. % at the uniform temperature.
- the run at 2.5 Hr 1 WHSV and slightly less catalyst demonstrates that selectivity for propylene is a function of temperature and residence time (other factors being held constant). In the 2.5 Hr 1 WHSV run, ethylene yield dropped to 28.3% while propylene rose to 30.9% with a small penalty in conversion reflecting the shorter residence time.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU78285/98A AU7828598A (en) | 1997-06-10 | 1998-06-08 | Hydrocarbon cracking with positive reactor temperature gradient |
JP50306699A JP2002504169A (en) | 1997-06-10 | 1998-06-08 | Hydrocarbon cracking with positive reactor temperature gradient |
EP98926448A EP0988354A1 (en) | 1997-06-10 | 1998-06-08 | Hydrocarbon cracking with positive reactor temperature gradient |
CA002290460A CA2290460A1 (en) | 1997-06-10 | 1998-06-08 | Hydrocarbon cracking with positive reactor temperature gradient |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US87258597A | 1997-06-10 | 1997-06-10 | |
US08/872,585 | 1997-06-10 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1998056873A1 true WO1998056873A1 (en) | 1998-12-17 |
Family
ID=25359901
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US1998/011875 WO1998056873A1 (en) | 1997-06-10 | 1998-06-08 | Hydrocarbon cracking with positive reactor temperature gradient |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP0988354A1 (en) |
JP (1) | JP2002504169A (en) |
CN (1) | CN1259983A (en) |
AU (1) | AU7828598A (en) |
CA (1) | CA2290460A1 (en) |
WO (1) | WO1998056873A1 (en) |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
US7235172B2 (en) | 2004-02-25 | 2007-06-26 | Conocophillips Company | Olefin production from steam cracking using process water as steam |
WO2008034596A1 (en) * | 2006-09-20 | 2008-03-27 | Lignosol Gmbh & Co. Kg | Installation and method for the production of fuels made of biogenic raw material |
US7431821B2 (en) | 2003-01-31 | 2008-10-07 | Chevron U.S.A. Inc. | High purity olefinic naphthas for the production of ethylene and propylene |
US20090288985A1 (en) * | 2004-03-08 | 2009-11-26 | Jun Long | Process for producing light olefins and aromatics |
WO2012071137A1 (en) * | 2010-11-01 | 2012-05-31 | Shell Oil Company | Process for hydrocracking butane or naphtha in the presence of a combination of two zeolites |
US10099210B2 (en) | 2013-04-29 | 2018-10-16 | Saudi Basic Industries Corporation | Catalytic methods for converting naphtha into olefins |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0921180A1 (en) * | 1997-12-05 | 1999-06-09 | Fina Research S.A. | Production of olefins |
US7692057B2 (en) * | 2005-08-15 | 2010-04-06 | China Petroleum & Chemical Corporation | Process for producing lower olefins by using multiple reaction zones |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1156193B (en) * | 1956-12-31 | 1963-10-24 | Hercules Powder Co Ltd | Process for splitting at least partially unsaturated hydrocarbon oils |
FR2140515A1 (en) * | 1971-06-09 | 1973-01-19 | Topsoe Haldor | |
US4282085A (en) * | 1978-10-23 | 1981-08-04 | Chevron Research Company | Petroleum distillate upgrading process |
US4620051A (en) * | 1985-07-25 | 1986-10-28 | Philips Petroleum Company | Dehydrogenation and cracking of C3 and C4 hydrocarbons to less saturated hydrocarbons |
EP0395345A1 (en) * | 1989-04-25 | 1990-10-31 | ARCO Chemical Technology, L.P. | Production of olefins |
-
1998
- 1998-06-08 AU AU78285/98A patent/AU7828598A/en not_active Abandoned
- 1998-06-08 JP JP50306699A patent/JP2002504169A/en active Pending
- 1998-06-08 CN CN 98805992 patent/CN1259983A/en active Pending
- 1998-06-08 WO PCT/US1998/011875 patent/WO1998056873A1/en not_active Application Discontinuation
- 1998-06-08 CA CA002290460A patent/CA2290460A1/en not_active Abandoned
- 1998-06-08 EP EP98926448A patent/EP0988354A1/en not_active Withdrawn
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1156193B (en) * | 1956-12-31 | 1963-10-24 | Hercules Powder Co Ltd | Process for splitting at least partially unsaturated hydrocarbon oils |
FR2140515A1 (en) * | 1971-06-09 | 1973-01-19 | Topsoe Haldor | |
US4282085A (en) * | 1978-10-23 | 1981-08-04 | Chevron Research Company | Petroleum distillate upgrading process |
US4620051A (en) * | 1985-07-25 | 1986-10-28 | Philips Petroleum Company | Dehydrogenation and cracking of C3 and C4 hydrocarbons to less saturated hydrocarbons |
EP0395345A1 (en) * | 1989-04-25 | 1990-10-31 | ARCO Chemical Technology, L.P. | Production of olefins |
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7314964B2 (en) | 2002-09-17 | 2008-01-01 | Uop Llc | Catalytic naphtha cracking catalyst and process |
US7585489B2 (en) | 2002-09-17 | 2009-09-08 | Uop Llc | Catalytic naphtha cracking catalyst and process |
US7446071B2 (en) | 2002-09-17 | 2008-11-04 | 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 |
US7235172B2 (en) | 2004-02-25 | 2007-06-26 | Conocophillips Company | Olefin production from steam cracking using process water as steam |
US20090288985A1 (en) * | 2004-03-08 | 2009-11-26 | Jun Long | Process for producing light olefins and aromatics |
US8778170B2 (en) * | 2004-03-08 | 2014-07-15 | China Petroleum Chemical Corporation | Process for producing light olefins and aromatics |
US20140275673A1 (en) * | 2004-03-08 | 2014-09-18 | China Petroleum Chemical Corporation | Process for producing light olefins and aromatics |
US9771529B2 (en) | 2004-03-08 | 2017-09-26 | China Petroleum & Chemical Corporation | Process for producing light olefins and aromatics |
WO2008034596A1 (en) * | 2006-09-20 | 2008-03-27 | Lignosol Gmbh & Co. Kg | Installation and method for the production of fuels made of biogenic raw material |
WO2012071137A1 (en) * | 2010-11-01 | 2012-05-31 | Shell Oil Company | Process for hydrocracking butane or naphtha in the presence of a combination of two zeolites |
US10099210B2 (en) | 2013-04-29 | 2018-10-16 | Saudi Basic Industries Corporation | Catalytic methods for converting naphtha into olefins |
Also Published As
Publication number | Publication date |
---|---|
EP0988354A1 (en) | 2000-03-29 |
CA2290460A1 (en) | 1998-12-17 |
JP2002504169A (en) | 2002-02-05 |
AU7828598A (en) | 1998-12-30 |
CN1259983A (en) | 2000-07-12 |
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