WO2001064760A2 - Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process - Google Patents
Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process Download PDFInfo
- Publication number
- WO2001064760A2 WO2001064760A2 PCT/US2001/006684 US0106684W WO0164760A2 WO 2001064760 A2 WO2001064760 A2 WO 2001064760A2 US 0106684 W US0106684 W US 0106684W WO 0164760 A2 WO0164760 A2 WO 0164760A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- propylene
- products
- olefins
- catalyst
- paraffins
- Prior art date
Links
Classifications
-
- 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
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
- C10G57/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with polymerisation
-
- 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
- C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
- C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
- C10G51/026—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only catalytic cracking steps
-
- 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 present invention relates to a process for producing polypropylene from C 3 olefins selectively produced from a catalytically cracked or thermally cracked naphtha stream.
- a problem inherent in producing olefins products using FCC units is that the process depends on a specific catalyst balance to maximize production of light olefins while also achieving high conversion of the 650° F + ( ⁇ 340°C +) feed components.
- olefins selectivity is generally low because of undesirable side reactions, such as extensive cracking, isomerization, aromatization and hydrogen transfer reactions. Light saturated gases produced from undesirable side reactions result in increased costs to recover the desirable light olefins. Therefore, it is desirable to maximize olefins production in a process that allows a high degree of control over the selectivity to C 2 - C olefins that are processed and polymerized to form products such as polypropylene and polyethylene.
- An embodiment of the present invention comprises a process for producing polypropylene comprising the steps of (a) contacting a naphtha feed containing less than 40 wt.% paraffins and between about 15 and about 70 wt.% olefins with a catalyst to form a cracked product, the catalyst comprising about 10 to about 50 wt.% of a crystalline zeolite having an average pore diameter less than about 0.7 nm, the reaction conditions including a temperature from about 500° to 650° C, a hydrocarbon partial pressure of 10 to 40 psia (70-280 kPa), a hydrocarbon residence time of 1 to 10 seconds, and a catalyst to feed ratio, by weight, of about 4 to 10, wherein no more than about 20 wt.% of paraffins are converted to olefins and wherein propylene comprises at least 90 mol.% of the total C 3 products; and, (b) separating the propylene from the cracked product and polymerizing the propylene to form poly
- the catalyst is a ZSM-5 type catalyst.
- the feed contains about 5 to 35 wt.% paraffins, and from about 20 to 70 wt.% olefins.
- reaction zone is operated at a temperature from about 525° C to about 600° C.
- Suitable hydrocarbons feeds for producing the relatively high C 2 , C 3 , and C olefins yields are those streams boiling in the naphtha range and containing less than about 40 wt.% paraffins, preferably from about 5 wt.% to about 35 wt.%, more preferably from about 10 wt.% to about 30 wt.%, and most preferably from about 10 to 25 wt.% paraffins, and from about 15 wt.%, preferably from about 20 wt.% to about 70 wt.% olefins.
- the feed may also contain naphthenes and aromatics.
- Naphtha boiling range streams are typically those having a boiling range from about 65° F to about 430° F (18-225° C), preferably from about 65° F to about 300° F ( 18- 150° C).
- the naphtha feed can be a thermally-cracked or catalytically-cracked naphtha derived from any appropriate source, including fluid catalytic cracking (FCC) of gas oils and resids or delayed- or fluid-coking of resids.
- FCC fluid catalytic cracking
- the naphtha streams used in the present invention derive from the fluid catalytic cracking of gas oils and resids because the product naphthas are typically rich in olefins and/or diolefins and relatively lean in paraffins.
- the process of the present invention is performed in a process unit comprising a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone.
- the naphtha feed is fed into the reaction zone where it contacts a source of hot, regenerated catalyst.
- the hot catalyst vaporizes and cracks the feed at a temperature from about 500° C to 650° C, preferably from about 525° C to 600° C.
- the cracking reaction deposits coke on the catalyst, thereby deactivating the catalyst.
- the cracked products are separated from the coked catalyst and sent to a fractionator.
- the coked catalyst is passed through the stripping zone where volatiles are stripped from the catalyst particles with steam.
- the stripping can be preformed under low severity conditions to retain a greater fraction of adsorbed hydrocarbons for heat balance.
- the stripped catalyst is then passed to the regeneration zone where it is regenerated by burning coke on the catalyst in the presence of an oxygen containing gas, preferably air. Decoking restores catalyst activity and simultaneously heats the catalyst to between about 650° C and about 750° C.
- the hot catalyst is then recycled to the reaction zone to react with fresh naphtha feed. Flue gas formed by burning coke in the regenerator may be treated for removal of particulates and for conversion of carbon monoxide.
- the cracked products from the reaction zone are sent to a fractionation zone where various products are recovered, particularly a C 3 fraction and a C fraction.
- the crystalline zeolite be selected from the family of medium-pore-size ( ⁇ 0.7 nm) crystalline aluminosilicates, otherwise referred to as zeolites.
- zeolites are the medium-pore zeolites with a silica to alumina molar ratio of less than about 75:1, preferably less than about 50: 1, and more preferably less than about 40: 1, although some embodiments incorporate silica-to-alumina ratios greater than 40: 1.
- the pore diameter also referred to as effective pore diameter, is measured using standard adsorption techniques and hydrocarbonaceous compounds of known minimum kinetic diameters. See Breck, Zeolite Molecular Sieves, 1974 and Anderson et al., J. Catalysis 58, 114 (1979), both of which are incorporated herein by reference.
- Medium-pore-size zeolites that can be used in the practice of the present invention are described in "Atlas of Zeolite Structure Types," eds. W.H. Meier and D.H. Olson, Butterworth-Heineman, Third Edition, 1992, which is hereby incorporated by reference.
- the medium-pore-size zeolites generally have a pore size from about 0.5 nm, to about 0.7 nm and include for example, MFI, MFS, MEL, MTW, EUO, MTT, HEU, FER, and TON structure type zeolites (IUPAC Commission of Zeolite Nomenclature).
- Non-limiting examples of such medium- pore-size zeolites include ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-34, ZSM- 35, ZSM-38, ZSM-48, ZSM-50, silicalite, and silicalite 2.
- ZSM-5 which is described in U.S. Patent Nos. 3,702,886 and 3,770,614.
- ZSM- 11 is described in U.S. Patent No. 3,709,979; ZSM-12 in U.S. Patent No. 3,832,449; ZSM-21 and ZSM-38 in U.S. Patent No. 3,948,758; ZSM-23 in U.S. Patent No. 4,076,842; and ZSM-35 in U.S. Patent No.
- Suitable medium- pore-size zeolites include the silicoaluminophosphates (SAPO), such as SAPO-4 and SAPO-11 which is described in U.S. Patent No. 4,440,871; chromosilicates; gallium silicates; iron silicates; aluminum phosphates (ALPO), such as ALPO- 11 described in U.S. Patent No. 4,310,440; titanium aluminosilicates (TASO), such as TASO-45 described in EP-A No. 229,295; boron silicates, described in U.S. Patent No. 4,254,297; titanium aluminophosphates (TAPO), such as TAPO- 11 described in U.S. Patent No. 4,500,651; and iron aluminosilicates.
- SAPO silicoaluminophosphates
- SAPO-4 and SAPO-11 which is described in U.S. Patent No. 4,440,871
- chromosilicates such as SAPO-4
- the medium-pore-size zeolites can include "crystalline admixtures" which are thought to be the result of faults occurring within the crystal or crystalline area during the synthesis of the zeolites.
- Examples of crystalline admixtures of ZSM-5 and ZSM-11 are disclosed in U.S. Patent No. 4,229,424, which is incorporated herein by reference.
- the crystalline admixtures are themselves medium-pore-size zeolites and are not to be confused with physical admixtures of zeolites in which distinct crystals of crystallites of different zeolites are physically present in the same catalyst composite or hydrothermal reaction mixtures.
- the catalysts of the present invention are held together with an inorganic oxide matrix material component.
- 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 "bind" the catalyst components together.
- the inorganic oxide matrix is not catalytically active and will be comprising oxides of silicon and aluminum.
- separate alumina phases are incorporated into the inorganic oxide matrix.
- Species of aluminum oxyhydroxides- ⁇ -alumina, boehmite, diaspore, and transitional aluminas such as ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, ⁇ -alumina, and p- alumina can be employed.
- the alumina species is an aluminum trihydroxide such as gibbsite, bayerite, nordstrandite, or doyelite.
- the matrix material may also contain phosphorous or aluminum phosphate.
- Process conditions include temperatures from about 500° C to about 650° C, preferably from about 525° C to 600° C, hydrocarbon partial pressures from about 10 to 40 psia (70-280 kPa), preferably from about 20 to 35 psia (140-245 kPa); and a catalyst to naphtha (wt/wt) ratio from about 3 to 12, preferably from about 4 to 10, where catalyst weight is total weight of the catalyst composite.
- steam is concurrently introduced with the naphtha stream into the reaction zone and comprises up to about 50 wt.% of the hydrocarbon feed.
- the feed residence time in the reaction zone be less than about 10 seconds, for example from about 1 to 10 seconds.
- ethylene comprises at least about 90 mol.% of the C 2 products, with the weight ratio of propylene:ethylene being greater than about 4, and that the "full range" C 5 + naphtha product is enhanced in both motor and research octanes relative to the naphtha feed. It is within the scope of this invention to pre-coke the catalysts before introducing the feed to further improve the selectivity to propylene. It is also within the scope of this invention to feed an effective amount of single ring aromatics to the reaction zone to also improve the selectivity of propylene versus ethylene.
- the aromatics may be from an external source such as a reforming process unit or they may consist of heavy naphtha recycle product from the instant process.
- Example 1 shows that increasing Cat/Oil ratio improves propylene yield, but sacrifices propylene purity.
- Comparison of Examples 3 and 4 and 5 and 6 shows reducing oil partial pressure greatly improves propylene purity without compromising propylene yield.
- Comparison of Examples 7 and 8 and 9 and 10 shows increasing temperature improves both propylene yield and purity.
- Comparison of Examples 11 and 12 shows decreasing cat residence time improves propylene yield and purity.
- Example 13 shows an example where both high propylene yield and purity are obtained at a reactor temperature and cat/oil ratio that can be achieved using a conventional FCC reactor/regenerator design for the second stage.
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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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Polymerisation Methods In General (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Polymerization Catalysts (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
- Catalysts (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA002400524A CA2400524A1 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process |
EP01916344A EP1259555A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process |
AU2001243379A AU2001243379A1 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from C3 olefins selectively produced in a fluid catalytic cracking process |
MXPA02008553A MXPA02008553A (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3. |
JP2001564252A JP2004516334A (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from C3 olefins selectively produced from naphtha / steam feed in a fluid catalytic cracking process |
Applications Claiming Priority (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/517,503 | 2000-03-02 | ||
US09/517,554 | 2000-03-02 | ||
US09/517,551 | 2000-03-02 | ||
US09/517,503 US6339180B1 (en) | 1998-05-05 | 2000-03-02 | Process for producing polypropylene from C3 olefins selectively produced in a fluid catalytic cracking process |
US09/517,497 US6258990B1 (en) | 1998-05-05 | 2000-03-02 | Process for producing polypropylene from C3 olefins selectively produced in a fluid catalytic cracking process from a naphtha/steam feed |
US09/517,497 | 2000-03-02 | ||
US09/517,554 US6388152B1 (en) | 1998-05-05 | 2000-03-02 | Process for producing polypropylene from C3 olefins selectively produced in a fluid catalytic cracking process |
US09/517,551 US6258257B1 (en) | 1998-05-05 | 2000-03-02 | Process for producing polypropylene from C3 olefins selectively produced by a two stage fluid catalytic cracking process |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2001064760A2 true WO2001064760A2 (en) | 2001-09-07 |
WO2001064760A3 WO2001064760A3 (en) | 2002-01-03 |
Family
ID=27504537
Family Applications (4)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2001/006686 WO2001064762A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced by a two stage fluid catalytic cracking process |
PCT/US2001/006684 WO2001064760A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process |
PCT/US2001/006685 WO2001064761A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process from a naphtha/steam feed |
PCT/US2001/006687 WO2001064763A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process |
Family Applications Before (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/US2001/006686 WO2001064762A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced by a two stage fluid catalytic cracking process |
Family Applications After (2)
Application Number | Title | Priority Date | Filing Date |
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PCT/US2001/006685 WO2001064761A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process from a naphtha/steam feed |
PCT/US2001/006687 WO2001064763A2 (en) | 2000-03-02 | 2001-03-01 | Process for producing polypropylene from c3 olefins selectively produced in a fluid catalytic cracking process |
Country Status (7)
Country | Link |
---|---|
EP (3) | EP1261648A2 (en) |
JP (3) | JP2004516335A (en) |
CN (3) | CN1406254A (en) |
AU (4) | AU2001241916A1 (en) |
CA (3) | CA2400598A1 (en) |
MX (3) | MXPA02008552A (en) |
WO (4) | WO2001064762A2 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021133895A1 (en) * | 2019-12-23 | 2021-07-01 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polypropylene and lubricating oil via refinery fcc and isomerization dewaxing units |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7270739B2 (en) | 2003-02-28 | 2007-09-18 | Exxonmobil Research And Engineering Company | Fractionating and further cracking a C6 fraction from a naphtha feed for propylene generation |
US7425258B2 (en) * | 2003-02-28 | 2008-09-16 | Exxonmobil Research And Engineering Company | C6 recycle for propylene generation in a fluid catalytic cracking unit |
US8920630B2 (en) | 2007-04-13 | 2014-12-30 | Shell Oil Company | Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock |
US20100324232A1 (en) * | 2007-10-10 | 2010-12-23 | Weijian Mo | Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock |
RU2474605C2 (en) * | 2007-11-29 | 2013-02-10 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Plants and methods for obtaining middle-distillate product and low molecular weight olefins from initial hydrocarbon raw material |
CN101747129B (en) * | 2008-11-28 | 2013-09-04 | 中国石油化工股份有限公司 | Method for producing light olefins through catalytic conversion |
CN102531821B (en) | 2010-12-28 | 2015-03-25 | 中国科学院大连化学物理研究所 | Method for catalyzing catalytic cracking reaction of methanol coupled with naphtha using modified ZSM-5 molecular sieve based catalyst |
CN103121894A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Combined method for producing low-carbon olefin |
CN105582997B (en) * | 2014-10-21 | 2018-05-18 | 中国石油化工股份有限公司 | The method of catalyst of naphtha catalytic cracking production propylene and preparation method thereof and naphtha catalytic cracking production propylene |
KR20210135329A (en) * | 2019-03-18 | 2021-11-12 | 엑손모빌 리서치 앤드 엔지니어링 컴퍼니 | Mesoporous catalyst compounds and uses thereof |
BR112022011762A2 (en) * | 2019-12-23 | 2022-08-30 | Chevron Usa Inc | CIRCULAR SAVINGS FOR PLASTIC WASTE FOR POLYPROPYLENE VIA REFINERY FCC UNIT |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1999057086A1 (en) * | 1998-05-05 | 1999-11-11 | Exxon Research And Engineering Company | Process for selectively producing light olefins in a fluid catalytic cracking process |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6118035A (en) * | 1998-05-05 | 2000-09-12 | Exxon Research And Engineering Co. | Process for selectively producing light olefins in a fluid catalytic cracking process from a naphtha/steam feed |
US6106697A (en) * | 1998-05-05 | 2000-08-22 | Exxon Research And Engineering Company | Two stage fluid catalytic cracking process for selectively producing b. C.su2 to C4 olefins |
US6093867A (en) * | 1998-05-05 | 2000-07-25 | Exxon Research And Engineering Company | Process for selectively producing C3 olefins in a fluid catalytic cracking process |
-
2001
- 2001-03-01 MX MXPA02008552A patent/MXPA02008552A/en unknown
- 2001-03-01 EP EP01913235A patent/EP1261648A2/en not_active Withdrawn
- 2001-03-01 WO PCT/US2001/006686 patent/WO2001064762A2/en active Application Filing
- 2001-03-01 AU AU2001241916A patent/AU2001241916A1/en not_active Abandoned
- 2001-03-01 AU AU2001239990A patent/AU2001239990A1/en not_active Abandoned
- 2001-03-01 CA CA002400598A patent/CA2400598A1/en not_active Abandoned
- 2001-03-01 CN CN 01805874 patent/CN1406254A/en active Pending
- 2001-03-01 CA CA002400524A patent/CA2400524A1/en not_active Abandoned
- 2001-03-01 CA CA002400382A patent/CA2400382A1/en not_active Abandoned
- 2001-03-01 JP JP2001564253A patent/JP2004516335A/en not_active Withdrawn
- 2001-03-01 AU AU2001239991A patent/AU2001239991A1/en not_active Abandoned
- 2001-03-01 WO PCT/US2001/006684 patent/WO2001064760A2/en not_active Application Discontinuation
- 2001-03-01 EP EP01914623A patent/EP1261649A2/en not_active Withdrawn
- 2001-03-01 MX MXPA02008553A patent/MXPA02008553A/en unknown
- 2001-03-01 AU AU2001243379A patent/AU2001243379A1/en not_active Abandoned
- 2001-03-01 JP JP2001564252A patent/JP2004516334A/en not_active Withdrawn
- 2001-03-01 MX MXPA02008554A patent/MXPA02008554A/en unknown
- 2001-03-01 EP EP01916344A patent/EP1259555A2/en not_active Withdrawn
- 2001-03-01 CN CN 01805862 patent/CN1406253A/en active Pending
- 2001-03-01 WO PCT/US2001/006685 patent/WO2001064761A2/en not_active Application Discontinuation
- 2001-03-01 JP JP2001564255A patent/JP2003525323A/en not_active Withdrawn
- 2001-03-01 CN CN 01805858 patent/CN1406252A/en active Pending
- 2001-03-01 WO PCT/US2001/006687 patent/WO2001064763A2/en not_active Application Discontinuation
Patent Citations (1)
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WO1999057086A1 (en) * | 1998-05-05 | 1999-11-11 | Exxon Research And Engineering Company | Process for selectively producing light olefins in a fluid catalytic cracking process |
Non-Patent Citations (2)
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021133895A1 (en) * | 2019-12-23 | 2021-07-01 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polypropylene and lubricating oil via refinery fcc and isomerization dewaxing units |
US11518945B2 (en) | 2019-12-23 | 2022-12-06 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polypropylene and lubricating oil via refinery FCC and isomerization dewaxing units |
US11959025B2 (en) | 2019-12-23 | 2024-04-16 | Chevron U.S.A Inc. | Circular economy for plastic waste to polypropylene and lubricating oil via refinery FCC and isomerization dewaxing units |
Also Published As
Publication number | Publication date |
---|---|
WO2001064762A3 (en) | 2002-01-24 |
WO2001064761A2 (en) | 2001-09-07 |
EP1261648A2 (en) | 2002-12-04 |
AU2001239991A1 (en) | 2001-09-12 |
EP1259555A2 (en) | 2002-11-27 |
MXPA02008554A (en) | 2003-04-22 |
JP2004516334A (en) | 2004-06-03 |
WO2001064762A2 (en) | 2001-09-07 |
MXPA02008552A (en) | 2003-03-12 |
WO2001064761A3 (en) | 2002-01-03 |
CA2400524A1 (en) | 2001-09-07 |
CN1406252A (en) | 2003-03-26 |
CN1406254A (en) | 2003-03-26 |
EP1261649A2 (en) | 2002-12-04 |
AU2001239990A1 (en) | 2001-09-12 |
JP2004516335A (en) | 2004-06-03 |
WO2001064763A2 (en) | 2001-09-07 |
JP2003525323A (en) | 2003-08-26 |
AU2001243379A1 (en) | 2001-09-12 |
WO2001064763A3 (en) | 2002-01-31 |
CA2400382A1 (en) | 2001-09-07 |
MXPA02008553A (en) | 2003-03-12 |
AU2001241916A1 (en) | 2001-09-12 |
CA2400598A1 (en) | 2001-09-07 |
CN1406253A (en) | 2003-03-26 |
WO2001064760A3 (en) | 2002-01-03 |
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