EP2046496A2 - Catalyseur d'hydrotraitement et procédé d'utilisation - Google Patents

Catalyseur d'hydrotraitement et procédé d'utilisation

Info

Publication number
EP2046496A2
EP2046496A2 EP07813564A EP07813564A EP2046496A2 EP 2046496 A2 EP2046496 A2 EP 2046496A2 EP 07813564 A EP07813564 A EP 07813564A EP 07813564 A EP07813564 A EP 07813564A EP 2046496 A2 EP2046496 A2 EP 2046496A2
Authority
EP
European Patent Office
Prior art keywords
catalyst composition
zeolite
acidic
component
range
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP07813564A
Other languages
German (de)
English (en)
Other versions
EP2046496A4 (fr
Inventor
Theodorus Maesen
Darren Fong
Roger Vogel
Bowmann Lee
Dennis Dykstra
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Chevron USA Inc
Original Assignee
Chevron USA Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Chevron USA Inc filed Critical Chevron USA Inc
Publication of EP2046496A2 publication Critical patent/EP2046496A2/fr
Publication of EP2046496A4 publication Critical patent/EP2046496A4/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/80—Mixtures of different zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/04—Oxides
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/16—Crystalline alumino-silicate carriers
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/16—Crystalline alumino-silicate carriers
    • C10G47/18—Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/16—Crystalline alumino-silicate carriers
    • C10G47/20—Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/12—Silica and alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/084—Y-type faujasite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J29/166—Y-type faujasite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7007—Zeolite Beta
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J29/7815—Zeolite Beta
    • 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
    • C10G2400/10—Lubricating oil

Definitions

  • This invention is directed to a catalyst effective in hyd reprocessing and a process employing this catalyst.
  • the literature of the refining arts contains examples of two acidic components of a hydroprocessing catalyst exhibiting synergy. The two components together are more effective than either component alone in hydroprocessing hydrocarbon feeds.
  • U.S. Pat. No. 3,535,225 discloses a hydroprocessing catalyst comprising a zeolite such as Y, a faujasite, in combination with an amorphous aluminosilicate.
  • This application discloses a catalyst composition suitable for hydroprocessing a hydrocarbonaceous feedstock, said catalyst composition comprising three acidic components acting in synergy to provide enhanced catalytic activity when compared to any of the components alone or in combinations of two. It was discovered that addition of a zeolite having a cage window in the range from about 0.47 nm to about 0.85 nm in diameter (such as zeolite beta), to a combination of a zeolite in the range from about 0.47 nm to about 0.85 nm in diameter, (such as zeolite Y) and amorphous aluminosiltcate (ASA) or delaminated clay (such as saponite) significantly enhances the activity, the diesel yield, the heavy diesel cold flow properties, the hydrodenitrification effects, and the base oil yield of the combinations of Y and ASA alone.
  • a zeolite having a cage window in the range from about 0.47 nm to about 0.85 nm in diameter such as zeolite
  • Figure 1 illustrates the improved base oil yield that occurs when employing the catalyst of this invention.
  • Figure 2 illustrates the improved dewaxed oil viscosity index that occurs when employing the catalyst of this invention.
  • the feedstocks that may be hydroprocessed using the catalyst of this invention are selected from the group consisting of petroleum distillates, solvent-deasphalted petroleum residua, shale oils, Fischer-Tropsch derived feedstocks and coal tar distillates.
  • the feedstocks contain substantial amounts of materials boiling above 200 ° F, preferably substantial amounts of materials boiling in the range 350 ° to 1100 0 F, and more preferably in the range 400 ° to 1000 ° F.
  • Suitable feedstocks include those heavy distillates normally defined as heavy straight-run gas oils and heavy cracked cycle oils, as well as conventional FCC feed and portions thereof.
  • Cracked stocks mav be obtained from thermal or catalytic cracking of various stocks, including those obtained from petroleum, gilsonite, shale and coal tar
  • the feedstocks may have been subjected to a hydrofining and/or hydrogenation treatment, which may have been accompanied by some hydrocracking, before being supplied to the hydroprocessing zone organic nitrogen content be less than 100 Parts per million organic nitroen-
  • organic nitrogen content be less than 100 Parts per million organic nitroen-
  • a preferred range is 0.5 to 1000 parts per million; more preferably, 0.5 to 100 parts per million.
  • it is preferable to maintain the organic sulfur content of the feed to a range of from 0 to 3 weight percent, preferably from 0 to 1 weight percent.
  • oils and base oils are used interchangeably in this application and refer to products boiling at or above 700° F. “Fuels” boil in the range from C 5 + to below 700° F.
  • the hydroprocessing zone containing the catalyst of this invention is preferably operated at hydrocracking conditions including a temperature in the range 400 ° to 950 ° F preferably 500 ° to 850 ° F, a pressure in the range 800 to 3500psig, preferably 1000 to 3000 psig, a liquid hourly space velocity in the range 0.1 to 5.0, preferably 0.5 to 5.0, and more preferably 0.5 to 3.0.
  • the total hydrogen supply rate (makeup and recycle hydrogen) to the hydroprocessing zone is 200 to 20,000 s.c.f preferably 2000 to 20000 scf of hydrogen per barrel of said feedstock.
  • the operating conditions in the separate hydrotreating zone include a temperature of 400 ° to 900 ° F, preferably 500 ° to 800 ° F, a pressure of 800 to 3500 psig preferably 1000 to 2500 p.s.i.g and a liquid hourly space velocity of 0.1 to 5.0, preferably 0.5 to 3.0.
  • the total hydrogen supply rate (makeup and recycle hydrogen) is 200 to 20,000 s.c.f. of hydrogen per barrel of feedstock, preferably 2000 to 20,000 s.c.f. of hydrogen per barrel of feedstock.
  • the catalyst of this invention comprises three acidic components acting in synergy to provide enhanced catalytic activity.
  • One acidic component is a zeolite having a cage window in the range from about 0.47 nm to about 0.85 nm in diameter.
  • the cage window is the narrowest part of a nanopore system, and the cage is the widest part of the nanopore system.
  • Nanopores are defined as pores smaller than 0.2 nm in diameter.
  • BEA- (beta), ISV-, BEC-, IWR-, MTW-, SSZ-31-, OFF- (offretite), MAZ- (mazzite), MOR- (mordenite), MOZ-, AFI-, ZSM-48-, and SSY-type zeolites fit this description.
  • BEA possesses a Si/AI molar ratio in the range from about 100 to about 300, preferably in the range from about 100 to about 200.
  • the website defines pore diameters of the zeolites mentioned.
  • the 2 nd acidic component is a zeolite having a cage in the range from about 0.9 nm to about 2.0 in diameter.
  • This category includes large pore zeolites such as FAU-, EMT-, ITQ-21-, ERT-, and ITQ-33-type zeolites.
  • FAU, EMT and ERT are further described at the sources indicated above.
  • ITQ-21 is described in an article, "A large-cavity zeolite with wide pore windows, and potential as an oil refining catalyst.” Corma, Avelino; Diaz-Cabanas, Maria J.; Martinez-Triguero, Joaquin; Rey, Fermando; Rius, Jordi.
  • UPV-CSIC 1 Instit ⁇ to de Tecnologia Quimica, Universidad Politecnica de Valencia, Valencia, Spain. Nature (London, United Kingdom) (2002), 418(6897), 514-517.
  • iTQ-33 is described in the article, "High-throughput synthesis and catalytic properties of a molecular sieve with 18- and 10-member rings.” Corma, Avelino; Diaz- Cabanas, Maria J.; Jorda, Jose Luis; Martinez, Columbia; Moliner, Manuel. lnstituto de Tecnologia Quimica, UPV-CSIC, Universidad Politecnica de Valencia, Valencia, Spain. Nature (London, United Kingdom) (2006), 443(7113), 842-845.
  • the FAU-type zeolite has a Si/AI molar ratio in the range from about 10 to about 100, preferably in the range from about 10 to about 80.
  • the catalyst composition of the instant invention comprises active zeolite components ranging from about 1% to about 50% of the catalyst composition.
  • the 3 rd acidic component ranges from about 10% to about 90% of the catalyst composition, and is selected from the group comprising clays and amorphous silicayalumina. If an amorphous silica-alumina component is used, it is preferably selected from the group comprising silica, alumina, titania, zirconia, magnesia and their binary and tertiary compounds. Amorphous silica-alumina component is mesoporous, comprising pores in the range from 2.0 to 50 nm. If a clay is used as the third acidic component, it is preferably selected from a group comprising saponites, vermiculites, biotites, stevensites, hectorite, beidellite, montmorillonites, and nontronites.
  • the first acidic component is beta zeolite
  • the second acidic component is Y zeolite or USY zeolite
  • the third acidic component is amorphous silica/alumina.
  • the catalyst composition of this invention may further comprise a hydrogenation component from the Periodic Table which is selected from a Group VIB metal, a Group VIU metal, or mixtures thereof.
  • a hydrogenation component from the Periodic Table which is selected from a Group VIB metal, a Group VIU metal, or mixtures thereof.
  • the hydrogenation component is a combination of nickel and tungsten, nickel and molybdenum or cobalt and molybdenum.
  • a hydrocracking catalyst containing beta/Y/ASA/alumina was prepared per following procedure. 1.4 wt-% beta zeolite (CP81 1C-300 powder from S ⁇ d Chemie), 5.8 wt-% USY (CBV 760 zeolite powder from the PQ corporation), 71.3 wt-% ASA powder (Siral-40 obtained from Sasol), and 21.5 wt-% pseudo-boehmite alumina powder were mixed well.
  • nickel nitrate hexahydrate dissolved in diluted nitric acid were added, so that the total mix contained 0.64 wt-% HNO3, 12.5 wt-% Ni(NO3)2.6H2O, 43 % H2O.
  • an ammonium metatungstate solution (54.5 wt-% ammonium metatungstentate in water) was added, and enough water to yield an extrudable mix.
  • the paste was extruded in 1/20" asymmetrical quadrulobes, dried at 130 C for one hour and calcined at 510 C for one hour with purging excess dry air. After cooling down to room temperature the catalyst contained 5.1 wt-% NiO and 25.2 wt-% WO3 on a dry basis.
  • a hydrocracking catalyst containing beta/Y/alumina was prepared as above, but by starting with a powder mix consisting of 5.8 wt.% USY, 72.7 wt.% ASA powder and 21.5 wt.% pseudo-boehmite alumina powder.
  • Table 1 demonstrates that a catalyst comprising a combination of zeolite beta, zeolite Y and amorphous silica-alumina (ASA) has a higher activity in fuels hydroprocessing applications than a combination of zeolite Y and ASA alone. It results in a larger volume of heavier products.
  • a catalyst comprising a combination of zeolite beta, zeolite Y and amorphous silica-alumina (ASA) has a higher activity in fuels hydroprocessing applications than a combination of zeolite Y and ASA alone. It results in a larger volume of heavier products.
  • ASA amorphous silica-alumina
  • Table 2 illustrates improved cold flow improvement properties in fuels hydroprocessing for the catalyst comprising a combination of zeolite beta, zeolite Y and amorphous aluminosilicate(ASA) when compared against a catalyst combination of zeolite Y and ASA alone.
  • Table 3 illustrates that a catalyst comprising a combination of zeolite beta, zeolite Y and amorphous aluminosilicate (ASA) has a higher activity in tubes hydroprocessing applications than a combination of zeolite Y and ASA alone.
  • a catalyst comprising a combination of zeolite beta, zeolite Y and amorphous aluminosilicate (ASA) has a higher activity in tubes hydroprocessing applications than a combination of zeolite Y and ASA alone.
  • Table 4 illustrates improved viscosity index and pour point in lubes hydroprocessing for the catalyst comprising a combination of zeolite beta, zeolite Y and amorphous aluminosilicate (ASA) when compared against a catalyst combination of zeolite Y and ASA alone.
  • zeolite beta zeolite beta
  • zeolite Y zeolite Y
  • ASA amorphous aluminosilicate
  • Figure 1 illustrates the improved base oil yield that occurs when employing the catalyst of this invention.
  • Figure 2 illustrates the improved dewaxed oil viscosity index that occurs when employing the catalyst of this invention.

Abstract

Cette invention concerne une composition de catalyseur efficace dans l'hydrotraitement et un procédé employant ce catalyseur. La composition de catalyseur comprend trois composants acides agissant en synergie pour fournir une activité catalytique améliorée, par comparaison avec des composants individuels ou en combinaison de deux. Deux des composants sont des zéolites à pores de grande dimension, et le troisième composant est choisi dans le groupe constitué par des argiles et la silice/alumine amorphe.
EP07813564.7A 2006-07-31 2007-07-31 Catalyseur d'hydrotraitement et procédé d'utilisation Withdrawn EP2046496A4 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US82090706P 2006-07-31 2006-07-31
US82898307A 2007-07-26 2007-07-26
PCT/US2007/074782 WO2008016888A2 (fr) 2006-07-31 2007-07-31 Catalyseur d'hydrotraitement et procédé d'utilisation

Publications (2)

Publication Number Publication Date
EP2046496A2 true EP2046496A2 (fr) 2009-04-15
EP2046496A4 EP2046496A4 (fr) 2014-08-06

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JP (1) JP2009545441A (fr)
WO (1) WO2008016888A2 (fr)

Families Citing this family (8)

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Publication number Priority date Publication date Assignee Title
CN102451744B (zh) * 2010-10-15 2014-03-05 中国石油化工股份有限公司 一种加氢裂化催化剂的制备方法
CN104588121B (zh) * 2013-11-03 2017-04-12 中国石油化工股份有限公司 加氢裂化催化剂载体及其制备方法
US10183286B2 (en) 2015-08-11 2019-01-22 Chevron U.S.A. Inc. Noble metal zeolite catalyst for second-stage hydrocracking to make middle distillate
US10046317B2 (en) * 2015-08-11 2018-08-14 Chevron U.S.A. Inc. Middle distillate hydrocracking catalyst containing zeolite beta with low OD acidity and large domain size
US10040058B2 (en) * 2015-08-11 2018-08-07 Chevron U.S.A. Inc. Middle distillate hydrocracking catalyst containing zeolite USY, and zeolite beta with low acidity and large domain size
CN109304226B (zh) * 2017-07-28 2021-06-01 中国石油天然气股份有限公司 一种多产重石脑油和航煤的加氢裂化催化剂及其制备方法和应用
CN109423336B (zh) * 2017-08-31 2020-09-11 中国石油化工股份有限公司 一种加氢裂化方法
WO2020119754A1 (fr) 2018-12-13 2020-06-18 中国石油化工股份有限公司 Catalyseur d'hydrocraquage, son procédé de préparation et son application

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EP2046496A4 (fr) 2014-08-06
JP2009545441A (ja) 2009-12-24
WO2008016888A3 (fr) 2008-08-07
WO2008016888A2 (fr) 2008-02-07

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