US3896024A - Process for producing light fuel oil - Google Patents

Process for producing light fuel oil Download PDF

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Publication number
US3896024A
US3896024A US457281A US45728174A US3896024A US 3896024 A US3896024 A US 3896024A US 457281 A US457281 A US 457281A US 45728174 A US45728174 A US 45728174A US 3896024 A US3896024 A US 3896024A
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Prior art keywords
catalyst
conversion
oil
cracking
cycle oil
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US457281A
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English (en)
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Donald M Nace
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Mobil Oil AS
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Mobil Oil AS
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Priority to US457281A priority Critical patent/US3896024A/en
Priority to CA75220019A priority patent/CA1048434A/en
Priority to ZA00751350A priority patent/ZA751350B/xx
Priority to GB10539/75A priority patent/GB1480182A/en
Priority to FR7509048A priority patent/FR2265843B1/fr
Priority to DE19752513469 priority patent/DE2513469A1/de
Priority to IT21911/75A priority patent/IT1034773B/it
Priority to AU79712/75A priority patent/AU490513B2/en
Priority to JP50038623A priority patent/JPS5848597B2/ja
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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

Definitions

  • the present invention relates to the production of light fuel oil and lower boiling products by catalytic cracking. More particularly, the present invention relates to improving the yield of light fuel oil product of a fluid catalyst cracking operation by contacting a fresh gas oil boiling range feed with a coked catalyst of reduced activity characteristics in the upper portion of a riser cracking zone at a temperature within the range of 800 to 900F. and subsequent to contacting freshly regenerated catalystpassed to a lower inlet of the same riser cracking zone with a heavy cycle oil product of the cracking operation at a temperature within the range of 900 to I000F.
  • a fresh gas oil feed preheated to an elevated temperature in the range of about 700F. to about 800F. is charged to an upper portion of a riser conversion zone wherein it is brought in contact with a hydrocarbon-catalyst suspension partially deactivated by hydrocarbonaceous deposits of recycle oil cracking to form a second oil-catalyst suspension comprising from about 0.5 to about 1.2 weight percent of carbonaceous deposits identified as carbon.
  • a mix temperature of the fresh gas oil feed with the recycle oil product-catalyst suspension above identified of about 800F. to about 900F. is desirable.
  • conversion of the fresh gas oil feed is considerably restricted not to exceed about 35 vol. percent and preferably is less than about 30 vol.%.
  • the more dilute suspension thus formed with the fresh gas oil feed traverses the remaining portion of the riser conversion zone for a limited contact time within the range of 1 to 4 seconds before it is discharged into suitable separating means such as cyclonic separating means for separating a hydrocarbon phase from a catalyst phase.
  • suitable separating means such as cyclonic separating means for separating a hydrocarbon phase from a catalyst phase.
  • the catalyst phase is stripped with stripping gasiform material such as steam to remove entrained hydrocar bon before it is passed to a catalyst regeneration zone.
  • the deposited carbonaceous material is substantially completely removed from the catalyst by burning with an oxygen containing gas thereby heating the catalyst to an elevated temperature within the range of l200F. up to about I400F.
  • the carbonaceous deposits substantially completely removed from the catalyst during regeneration and remaining as residual coke, is reduced to at least about 0.2 weight percent.
  • the hydrocarbon phase separated as above provided or by any other suitable separating arrangement is passed to the product fractionator wherein a separation is made for the separate recovery of a naphtha stream and lower boiling gasiform materials, a light fuel oil stream and a heavy cycle oil stream.
  • a clarified slurry stream may also be recovered from the lower portion of the fractionator.
  • the heavy cycle oil comprising an initial boiling point within the range of 650 to 720F. is passed as charge to the bottom portion of a riser reactor or conversion zone for admixture with hot freshly regenerated catalyst to form a suspension.
  • the heavy cycle oil at a relatively low temperature in the range of about 350F. up to about 500F. is combined with the hot freshly regenerated catalyst to form a suspension at a mix temperature less than about 1000F.
  • the conversion conditions maintained in the lower portion of the riser conversion zone are selected to provide a conversion of the heavy cycle oil to lower boiling products including gasoline and particularly a light fuel oil product.
  • carbonaceous deposits are formed on the catalyst in an amount of at leat 0.5 weight percent.
  • conversion of the heavy cycle oil to gasoline and lower boiling products is restricted usually not to exceed about vol.%.
  • conversion of the heavy cycle oil may be restricted to produce about 10 weight percent (wt.%) gas, 35 wt.% gasoline, 20 wt.% light fuel oil, 5 wt.% coke and 30 wt.% of unconverted 650F. plus material.
  • the combination operation of the present invention is unique in several respects and particularly unique in that fresh gas oil feed contacts a process generated catalyst of reduced activity at a lower catalyst to oil ratio than that used for converting heavy cycle oil product of the combination operation. Furthermore, the overall conversion of the hydrocarbon feeds can be maintained at a selected high level with a low steady state concentration of heavy cycle oil and the light fuel oil product thereof will be maximized because of the particularly selected low severity conditions that it encounters as a result of its first pass contact with the catalyst of reduced activity particularly employed in the operation.
  • the catalyst employed in the combination operation of this invention may be substantially any cracking cat alyst known in the art provided its activity is selectively combination thereof.
  • a preferred catalyst is a rare earth exchanged Y-type crystalline faujasite in an amount up to about 15 weight percent and more usually within the range of 2 to 10 weight percent dispersed in a suitable matrix material.
  • a more preferred catalyst comprises as much as about 10 weight percent of a rare earth exchanged Y-faujasite crystalline zeolite dispersed in a silica clay matrix and provided with a small amount of zirconia.
  • Such preferred catalysts are more completely defined in U.S. Pat. No. 3,556,988 issued Jan. 17. 1971.
  • the catalyst may be an amorphous silica-alumina cracking catalyst, a crystalline zeolite cracking catalyst, or a product of the Durban gas oil cracking in the presence of a more active regenerated catalyst composition, clean burned and containing a small amount of residual carbon thereon is presented in Table II.
  • Table 111 Maximum Total Yield of 650F. End Point LFO with Recycle of 650F.+ Btms from Single Pass 30% Fresh Feed Conversion 1 11 111 Charge Fresh Feed at 30% 6S0F.+ HCO Combination Single Conv. 430F) from 30% FF Run Pass FF at 30% at wt. Conv. 650F.+ Recycle at 430F) 50 Wt.% Conv. I+ll (based on fresh feed) Conditions 850F., 7 do, 5 sec. 850F., l2 c/0 4 sec.
  • Table III combines two comparisons of products obtained when processing a fresh gas oil feed over a coke containing catalyst and the heavy fuel oil (recycle) product thereof over regenerated catalyst at two different conversion levels. From the data presented in Table III, it will be observed that the combination of I, II and III produced higher yields of light fuel oil than the combination of I, IV and V.
  • FIG. I graphically presents the response of conversion to catalyst/oil ratio in cracking a 650F. heavy cycle oil and a Durban fresh feed with a 55-57 FAI catalyst comprising a rare earth exchanged Y-crystalline faujasite cracking catalyst.
  • FIG. II graphically presents the product selectively from cracking 650F.+ heavy cycle oil and Durban fresh feed over a 55 FAI REY type crystalline zeolite cracking catalyst.
  • FIG. IlI graphically presents the effect of 650F.+ heavy recycle on the overall yield of products on a fresh feed basis.
  • FIG. IV graphically presents a comparison of the C gasoline products octane number.
  • FIG. V graphically presents the pour point and AP] gravity of the 430-650F. light fuel oil (LFO) fraction made from cracking Durban fresh feed and from 650F.+ heavy cycle oil.
  • LFO light fuel oil
  • FIG. VI graphically presents a yield and pour point comparison of the 690F. end point light fuel oil (LFO) obtained from Durban fresh feed and from a 650F.+ heavy cycle oil (HCO) by cracking with coked and clean REY type zeolite cracking catalysts.
  • LFO end point light fuel oil
  • HCO heavy cycle oil
  • FIG. VII is a diagrammatic sketch in elevation of one arrangement of apparatus comprising a riser cracking zone and a catalyst regeneration zone interconnected by suitable catalyst transfer conduit means and a prod uct recovery zone for separation, recovery and recycle of desired hydrocarbon product material to the cracking operation.
  • FIGS. I through VI herein presented are essentially self-explanatory and clearly represent the processing advantages of the concept of the present invention with respect to product yield and quality.
  • FIG. I for example, it is shown that the fresh feed hydrocarbon charge is more conversion responsive than the 650F. plus heavy cycle oil feed to catalyst to oil ratio and temperature variations for a given activity crystalline zeolite cracking catalyst.
  • FIG. II it is graphically shown that the fresh feed converted at 1000F. produced greater yields than the 650F.+ heavy cycle oil processed at 850F. and 950F. Also the gasoline yield was generally higher from the fresh feed cracking operation. Very little difference. if any, is noted in the yields of dry gas and C hydrocarbons. Variations in the coke yields for different conversion levels is readily observed.
  • FIG. III the data of Table III is graphically presented.
  • the 850F. single pass operation combined with the 850F. recycle operation produced similar levels of light fuel oil product at conversion levels in the range of 45 to 55 and was much better than the single pass operations graphically depicted. Also at conversion levels less than 50 weight percent the yields of C, hydrocarbons, dry gas and coke are not materially different.
  • FIG. V it is graphically shown that the pour point of the light fuel oil (430-650F) and obtained from the fresh feed and the heavy cycle oil is satisfactory and rel-
  • FIG. Vl graphically shows the influence of tempera-- ture and conversion on cracking the fresh feed and recracking a heavy cycle oil product thereof on the yield.
  • the operating parameters be selected to deposit an amount of carbonaceous material on the catalyst to reduce its activity within the range of 20 to 40 (FA!) fluid activity index before contact is made with the fresh gas oil feed under selected conversion 900F.
  • the preheated feed is then passed by conduit 6 to an upper portion of riser conversion zone 8 identitied at B.
  • a suspension is formed with previously used catalyst of reduced activity and comprising from about 0.5 to about 1.2 weight percent carbon deposit.
  • the suspension thus formed will comprise a catalyst to fresh feed weight ratio within the range of 3 to 9 to give a fresh feed conversion to gasoline and lower boiling products within the range of 10 to 40 weight percent.
  • the suspension thus formed and diluted with the products of heavy cycle oil recracking obtained as discussed below pass upwardly through the remaining portion of the riser into a catalyst separation zone 10.
  • the fresh feedcatalyst-suspension is provided a hydrocarbon contact time within the range of l to 4 seconds under the conditions specified above.
  • ln separation zone 10 provided with cyclonic separating means 12, separation of the suspension into a catalyst phase and a hydrocarbon phase is accomplished.
  • the hydrocarbon phase is recovered and withdrawn by conduit 14 communicating with fractionation zone 16.
  • the separated catalyst phase is collected and passed down, usually through an annular stripping zone 18 countercurrent to stripping gas introduced to a lower portion thereof by conduit 20.
  • Catalyst stripped of entrained hydrocarbon vapors but deactivated with carbonaceous products of cracking is then passed by conduit 22 to regeneration zone 24.
  • regeneration zone 24 the catalyst activity is restored by burning carbonaceous deposits with. for example, air introduced to the lower portion of the regeneration zone by conduit 26. Gaseous products of combustion comprising flue gas are withdrawn from the regeneration zone by conduit 28.
  • the catalyst of restored activity by the regeneration procedure and heated to an elevated temperature up to about l400F. is withdrawn by conduit 30 and passed to the lower portion of riser 8.
  • the freshly regenerated catalyst comprising a small amount of residual carbon is admixed with a heavy cycle oil product of the cracking operation in conduit 32, boiling above about 650F. to form a catalyst/oil suspension at a mix temperature within the range of 900 to about l0O0F.
  • Preheating of the cycle oil product of cracking before forming the suspension is contemplated.
  • the catalyst to oil ratio is prefer-- ably selected from within the range of IO to 20. Under the conditions above defined the cycle oil catalyst suspension is provided a contact time within the range of 4 to 8 seconds before the suspension is diluted with the fresh gas oil feed as defined above.
  • fractionator 16 The products of converting heavy cycle oil and fresh gas oil feedstocks under the above recited conversion conditions are conveyed by conduit 14 to fractionator In fractionator 16, the hydrocarbon products of catalytic cracking are separated into a gaseous phase re moved by conduit 34. a naphtha phase removed by conduit 36, a light fuel oil phase removed by conduit 38, a heavy cycle oil phase removed by conduit 32 and a bottom or clarified slurry oil phase removed by conduit 40.
  • A-rnethod forrproducing light fuel oil and lower boilinghydrocarbons which. comprises:
  • a method for cracking gas oils and higher boiling material which comprises:
  • a method for converting hydrocarbons to gasoline and fuel oil products which comprises:
  • the hydrocarbon phase in the lower portion of the riser conversion zone initially limited to a heavy cycle oil product of the conversion operation
  • the hydrocarbon phase in an upper portion of the riser conversion zone comprising fresh gas oil feed material
  • restricting conversion of the gas oil feed in the upper portion of the riser conversion zone by limiting the conversion condition to a temperature within the range of 800 to 900F.
  • the crystalline zeolite is a rare earth exchanged Y faujasite crystalline zeolite.

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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)
US457281A 1974-04-02 1974-04-02 Process for producing light fuel oil Expired - Lifetime US3896024A (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US457281A US3896024A (en) 1974-04-02 1974-04-02 Process for producing light fuel oil
CA75220019A CA1048434A (en) 1974-04-02 1975-02-13 Process for producing light fuel oil
ZA00751350A ZA751350B (en) 1974-04-02 1975-03-05 A process for producing light fuel oil
GB10539/75A GB1480182A (en) 1974-04-02 1975-03-13 Process for producing light fuel oil
FR7509048A FR2265843B1 (it) 1974-04-02 1975-03-24
DE19752513469 DE2513469A1 (de) 1974-04-02 1975-03-26 Verfahren zur umwandlung von kohlenwasserstoffen
IT21911/75A IT1034773B (it) 1974-04-02 1975-04-01 Procedimento per la produzione di olio combustibile leggero
AU79712/75A AU490513B2 (en) 1974-04-02 1975-04-01 A process FOR PRODUCING LIGHT FUEL OIL
JP50038623A JPS5848597B2 (ja) 1974-04-02 1975-04-01 炭化水素をガソリン及び燃料油に転化する方法

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US457281A US3896024A (en) 1974-04-02 1974-04-02 Process for producing light fuel oil

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US (1) US3896024A (it)
JP (1) JPS5848597B2 (it)
CA (1) CA1048434A (it)
DE (1) DE2513469A1 (it)
FR (1) FR2265843B1 (it)
GB (1) GB1480182A (it)
IT (1) IT1034773B (it)
ZA (1) ZA751350B (it)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4147617A (en) * 1978-04-06 1979-04-03 Mobil Oil Corporation Processing hydrocarbon feed of high carbon residue and high metals content
US4218306A (en) * 1979-01-15 1980-08-19 Mobil Oil Corporation Method for catalytic cracking heavy oils
EP0131912A1 (en) * 1983-07-16 1985-01-23 Research Association For Petroleum Alternatives Development A method for the hydrogenation treatment of heavy oils
EP0208609A1 (fr) * 1985-07-10 1987-01-14 Total Raffinage Distribution S.A. Procédé et dispositif pour le craquage catalytique de charges d'hydrocarbures, avec contrôle de la température de réaction
EP0265347A1 (fr) * 1986-10-24 1988-04-27 Compagnie De Raffinage Et De Distribution Total France Procédé et dispositif pour le craquage catalytique en lit fluidisé d'une charge d'hydrocarbures
US5271826A (en) * 1988-03-03 1993-12-21 Mobil Oil Corporation Catalytic cracking of coke producing hydrocarbons
WO1995016761A1 (en) * 1993-12-17 1995-06-22 Mobil Oil Corporation Catalytic cracking process
US5582711A (en) * 1994-08-17 1996-12-10 Exxon Research And Engineering Company Integrated staged catalytic cracking and hydroprocessing process
US5770043A (en) * 1994-08-17 1998-06-23 Exxon Research And Engineering Company Integrated staged catalytic cracking and hydroprocessing process
US5770044A (en) * 1994-08-17 1998-06-23 Exxon Research And Engineering Company Integrated staged catalytic cracking and hydroprocessing process (JHT-9614)
US5824208A (en) * 1994-05-27 1998-10-20 Exxon Research & Engineering Company Short contact time catalytic cracking process
US6123830A (en) * 1998-12-30 2000-09-26 Exxon Research And Engineering Co. Integrated staged catalytic cracking and staged hydroprocessing process
US20030150775A1 (en) * 2000-04-17 2003-08-14 Stuntz Gordon F. Cycle oil conversion process
EP1935965A1 (en) * 2006-12-20 2008-06-25 Petroleo Brasileiro S.A. Petrobras Process for catalytic cracking of petroleum hydrocarbons in a fluidized bed with maximum production of light olefins
CN113301987A (zh) * 2018-12-19 2021-08-24 Ifp 新能源公司 原油在包括具有不同接触时间的区域的流化床中的转化

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS624784A (ja) * 1985-07-16 1987-01-10 コンパニ−・フランセ−ズ・ド・ラフイナ−ジユ 炭化水素仕込物の接触クラツキングのための方法および装置の改良
JPH0177599U (it) * 1987-11-13 1989-05-25

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2882218A (en) * 1953-12-09 1959-04-14 Kellogg M W Co Hydrocarbon conversion process
US2908680A (en) * 1957-04-04 1959-10-13 Merck & Co Inc Process for preparing crystalline antibiotic
US3182011A (en) * 1961-06-05 1965-05-04 Sinclair Research Inc Cracking a plurality of hydrocarbon stocks
US3186805A (en) * 1961-11-06 1965-06-01 Phillips Petroleum Co Catalytic apparatus
US3689402A (en) * 1970-10-29 1972-09-05 Texaco Inc Furnace oil from waxy gas oils
US3801493A (en) * 1972-10-25 1974-04-02 Texaco Inc Slack wax cracking in an fccu with a satellite reactor
US3847793A (en) * 1972-12-19 1974-11-12 Mobil Oil Conversion of hydrocarbons with a dual cracking component catalyst comprising zsm-5 type material
US3856659A (en) * 1972-12-19 1974-12-24 Mobil Oil Corp Multiple reactor fcc system relying upon a dual cracking catalyst composition

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3158562A (en) * 1961-10-27 1964-11-24 Exxon Research Engineering Co Transfer line catalytic cracking
US3751359A (en) * 1971-09-27 1973-08-07 Texaco Inc Conversion of hydrocarbons

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2882218A (en) * 1953-12-09 1959-04-14 Kellogg M W Co Hydrocarbon conversion process
US2908680A (en) * 1957-04-04 1959-10-13 Merck & Co Inc Process for preparing crystalline antibiotic
US3182011A (en) * 1961-06-05 1965-05-04 Sinclair Research Inc Cracking a plurality of hydrocarbon stocks
US3186805A (en) * 1961-11-06 1965-06-01 Phillips Petroleum Co Catalytic apparatus
US3689402A (en) * 1970-10-29 1972-09-05 Texaco Inc Furnace oil from waxy gas oils
US3801493A (en) * 1972-10-25 1974-04-02 Texaco Inc Slack wax cracking in an fccu with a satellite reactor
US3847793A (en) * 1972-12-19 1974-11-12 Mobil Oil Conversion of hydrocarbons with a dual cracking component catalyst comprising zsm-5 type material
US3856659A (en) * 1972-12-19 1974-12-24 Mobil Oil Corp Multiple reactor fcc system relying upon a dual cracking catalyst composition

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4147617A (en) * 1978-04-06 1979-04-03 Mobil Oil Corporation Processing hydrocarbon feed of high carbon residue and high metals content
US4218306A (en) * 1979-01-15 1980-08-19 Mobil Oil Corporation Method for catalytic cracking heavy oils
JPS55112293A (en) * 1979-01-15 1980-08-29 Mobil Oil Riser cracking method
EP0131912A1 (en) * 1983-07-16 1985-01-23 Research Association For Petroleum Alternatives Development A method for the hydrogenation treatment of heavy oils
EP0208609A1 (fr) * 1985-07-10 1987-01-14 Total Raffinage Distribution S.A. Procédé et dispositif pour le craquage catalytique de charges d'hydrocarbures, avec contrôle de la température de réaction
FR2584732A1 (fr) * 1985-07-10 1987-01-16 Raffinage Cie Francaise Procede et dispositif pour le craquage catalytique de charges d'hydrocarbures, avec controle de la temperature de reaction
US4818372A (en) * 1985-07-10 1989-04-04 Compagnie De Raffinage Et De Distribution Total France Process and apparatus for the catalytic cracking of hydrocarbon feedstocks with reaction-temperature control
AU585035B2 (en) * 1985-07-10 1989-06-08 Compagnie De Raffinage Et De Distribution Total France Process and device for catalytic cracking of charges of hydrocarbons, with temperature control of the reaction
EP0265347A1 (fr) * 1986-10-24 1988-04-27 Compagnie De Raffinage Et De Distribution Total France Procédé et dispositif pour le craquage catalytique en lit fluidisé d'une charge d'hydrocarbures
FR2605643A1 (fr) * 1986-10-24 1988-04-29 Total France Procede et dispositif pour le craquage catalytique en lit fluidise d'une charge d'hydrocarbures
US5271826A (en) * 1988-03-03 1993-12-21 Mobil Oil Corporation Catalytic cracking of coke producing hydrocarbons
WO1995013337A1 (en) * 1988-03-03 1995-05-18 Mobil Oil Corporation A catalytic cracking process
WO1995016761A1 (en) * 1993-12-17 1995-06-22 Mobil Oil Corporation Catalytic cracking process
US5824208A (en) * 1994-05-27 1998-10-20 Exxon Research & Engineering Company Short contact time catalytic cracking process
US5582711A (en) * 1994-08-17 1996-12-10 Exxon Research And Engineering Company Integrated staged catalytic cracking and hydroprocessing process
US5770043A (en) * 1994-08-17 1998-06-23 Exxon Research And Engineering Company Integrated staged catalytic cracking and hydroprocessing process
US5770044A (en) * 1994-08-17 1998-06-23 Exxon Research And Engineering Company Integrated staged catalytic cracking and hydroprocessing process (JHT-9614)
US6123830A (en) * 1998-12-30 2000-09-26 Exxon Research And Engineering Co. Integrated staged catalytic cracking and staged hydroprocessing process
US20030150775A1 (en) * 2000-04-17 2003-08-14 Stuntz Gordon F. Cycle oil conversion process
US6837989B2 (en) * 2000-04-17 2005-01-04 Exxonmobil Research And Engineering Company Cycle oil conversion process
EP1935965A1 (en) * 2006-12-20 2008-06-25 Petroleo Brasileiro S.A. Petrobras Process for catalytic cracking of petroleum hydrocarbons in a fluidized bed with maximum production of light olefins
CN113301987A (zh) * 2018-12-19 2021-08-24 Ifp 新能源公司 原油在包括具有不同接触时间的区域的流化床中的转化

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Publication number Publication date
DE2513469A1 (de) 1975-10-23
CA1048434A (en) 1979-02-13
IT1034773B (it) 1979-10-10
FR2265843A1 (it) 1975-10-24
JPS5116302A (it) 1976-02-09
AU7971275A (en) 1976-10-07
FR2265843B1 (it) 1978-08-18
GB1480182A (en) 1977-07-20
ZA751350B (en) 1976-10-27
JPS5848597B2 (ja) 1983-10-29

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