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RU2009105256A - HYDROCRACKING CATALYST CONTAINING BETA- AND Y-ZEOLITES, AND METHOD OF ITS APPLICATION FOR OBTAINING A DISTILLATE - Google Patents

HYDROCRACKING CATALYST CONTAINING BETA- AND Y-ZEOLITES, AND METHOD OF ITS APPLICATION FOR OBTAINING A DISTILLATE Download PDF

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RU2009105256A
RU2009105256A RU2009105256/04A RU2009105256A RU2009105256A RU 2009105256 A RU2009105256 A RU 2009105256A RU 2009105256/04 A RU2009105256/04 A RU 2009105256/04A RU 2009105256 A RU2009105256 A RU 2009105256A RU 2009105256 A RU2009105256 A RU 2009105256A
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zeolite
composition according
beta
calcining
water vapor
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RU2009105256/04A
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Russian (ru)
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Ли ВАНГ (US)
Ли Ванг
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Юоп Ллк (Us)
Юоп Ллк
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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
    • 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
    • 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
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/28—Molybdenum
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/30—Tungsten
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/75—Cobalt
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/755—Nickel
    • 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
    • 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
    • B01J29/70—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
    • B01J29/80—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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/653—500-1000 nm
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/12—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

1. Композиция вещества, включающая катализатор, состоящий из гидрирующего компонента, бета-цеолита, имеющего общее молярное отношение диоксида кремния к оксиду алюминия меньше, чем 30, и адсорбционную способность по SF6, по меньшей мере, 28 мас.%, Y-цеолита, имеющего размер элементарной ячейки от 24,25 до 24,32 Å, и носителя, в котором Y-цеолит имеет общее молярное отношение диоксида кремния к оксиду алюминия от 5,0 до 11,0, причем катализатор содержит от более 2 мас.% до не более 5 мас.% бета-цеолита, в расчете на объединенный сухой вес бета-цеолита, Y-цеолита и носителя, и катализатор имеет отношение Y-цеолита к бета-цеолиту по массе от 2,5 до 12,5 в высушенном состоянии. ! 2. Композиция по п.1, в которой Y-цеолит имеет площадь поверхности меньше, чем 800 м2/г. ! 3. Композиция по п.1, в которой гидрирующий компонент выбирают из группы, состоящей из молибдена, вольфрама, никеля, кобальта и их оксидов и сульфидов. ! 4. Композиция по п.1, в которой Y цеолит получают посредством способа, включающего стадии: ! a) частичный аммониевый обмен натриевого Y цеолита; ! b) прокаливание цеолита, полученного на стадии (а), в присутствии водяных паров; ! c) аммониевый обмен цеолита, полученного от стадии (b); и ! d) прокаливание цеолита, полученного на стадии (с), в присутствии водяных паров. ! 5. Композиция по п.1, в которой Y цеолит получают посредством способа, включающего стадии: !a) частичный аммониевый обмен натриевого Y цеолита; ! b) прокаливание цеолита, полученного на стадии (а), в присутствии водяных паров; ! c) контактирование цеолита, полученного на стадии (b), с фторсиликатной солью в форме водного раствора; и ! d) прокаливание цеолита, полученного на стадии (с), в присутствии 1. Composition of a substance comprising a catalyst consisting of a hydrogenating component, beta-zeolite having a total molar ratio of silica to alumina less than 30, and an SF6 adsorption capacity of at least 28 wt%, Y-zeolite, having a unit cell size from 24.25 to 24.32 Å, and a support in which the Y-zeolite has a total molar ratio of silica to alumina from 5.0 to 11.0, and the catalyst contains from more than 2 wt.% to not more than 5 wt% zeolite beta, based on the combined dry weight of zeolite beta, zeolite Y and support, and the catalyst has a ratio of zeolite Y to zeolite beta by weight of 2.5 to 12.5 dry ... ! 2. The composition of claim 1, wherein the Y-zeolite has a surface area of less than 800 m2 / g. ! 3. The composition of claim 1, wherein the hydrogenating component is selected from the group consisting of molybdenum, tungsten, nickel, cobalt and their oxides and sulfides. ! 4. A composition according to claim 1, wherein the Y zeolite is produced by a method comprising the steps of:! a) partial ammonium exchange of sodium Y zeolite; ! b) calcining the zeolite obtained in step (a) in the presence of water vapor; ! c) ammonium exchange of the zeolite obtained from step (b); and ! d) calcining the zeolite obtained in step (c) in the presence of water vapor. ! 5. The composition according to claim 1, in which the Y zeolite is obtained by a method comprising the steps:! A) partial ammonium exchange of the sodium Y zeolite; ! b) calcining the zeolite obtained in step (a) in the presence of water vapor; ! c) contacting the zeolite obtained in step (b) with a fluorosilicate salt in the form of an aqueous solution; and ! d) calcining the zeolite obtained in step (c) in the presence of

Claims (10)

1. Композиция вещества, включающая катализатор, состоящий из гидрирующего компонента, бета-цеолита, имеющего общее молярное отношение диоксида кремния к оксиду алюминия меньше, чем 30, и адсорбционную способность по SF6, по меньшей мере, 28 мас.%, Y-цеолита, имеющего размер элементарной ячейки от 24,25 до 24,32 Å, и носителя, в котором Y-цеолит имеет общее молярное отношение диоксида кремния к оксиду алюминия от 5,0 до 11,0, причем катализатор содержит от более 2 мас.% до не более 5 мас.% бета-цеолита, в расчете на объединенный сухой вес бета-цеолита, Y-цеолита и носителя, и катализатор имеет отношение Y-цеолита к бета-цеолиту по массе от 2,5 до 12,5 в высушенном состоянии.1. The composition of the substance, including the catalyst, consisting of a hydrogenating component, beta zeolite, having a total molar ratio of silicon dioxide to alumina less than 30, and the adsorption capacity for SF 6 of at least 28 wt.%, Y-zeolite having a unit cell size of from 24.25 to 24.32 Å, and a carrier in which the Y-zeolite has a total molar ratio of silica to alumina from 5.0 to 11.0, and the catalyst contains from more than 2 wt.% up to no more than 5 wt.% beta zeolite, based on the combined dry weight of beta zeolite, Y zeolite carrier, and the catalyst has a ratio of Y-zeolite to the beta zeolite by weight from 2.5 to 12.5 in the dried state. 2. Композиция по п.1, в которой Y-цеолит имеет площадь поверхности меньше, чем 800 м2/г.2. The composition according to claim 1, in which the Y-zeolite has a surface area of less than 800 m 2 / g 3. Композиция по п.1, в которой гидрирующий компонент выбирают из группы, состоящей из молибдена, вольфрама, никеля, кобальта и их оксидов и сульфидов.3. The composition according to claim 1, in which the hydrogenating component is selected from the group consisting of molybdenum, tungsten, nickel, cobalt and their oxides and sulfides. 4. Композиция по п.1, в которой Y цеолит получают посредством способа, включающего стадии:4. The composition according to claim 1, in which Y zeolite is obtained by a method comprising the steps of: a) частичный аммониевый обмен натриевого Y цеолита;a) partial ammonium exchange of sodium Y zeolite; b) прокаливание цеолита, полученного на стадии (а), в присутствии водяных паров;b) calcining the zeolite obtained in stage (a) in the presence of water vapor; c) аммониевый обмен цеолита, полученного от стадии (b); иc) ammonium exchange of zeolite obtained from stage (b); and d) прокаливание цеолита, полученного на стадии (с), в присутствии водяных паров.d) calcining the zeolite obtained in step (c) in the presence of water vapor. 5. Композиция по п.1, в которой Y цеолит получают посредством способа, включающего стадии:5. The composition according to claim 1, in which Y zeolite is obtained by a method comprising the steps of: a) частичный аммониевый обмен натриевого Y цеолита;a) partial ammonium exchange of sodium Y zeolite; b) прокаливание цеолита, полученного на стадии (а), в присутствии водяных паров;b) calcining the zeolite obtained in stage (a) in the presence of water vapor; c) контактирование цеолита, полученного на стадии (b), с фторсиликатной солью в форме водного раствора; иc) contacting the zeolite obtained in step (b) with a fluorosilicate salt in the form of an aqueous solution; and d) прокаливание цеолита, полученного на стадии (с), в присутствии водяных паров.d) calcining the zeolite obtained in step (c) in the presence of water vapor. 6. Композиция по п.1, в которой Y цеолит получают посредством способа, включающего стадии:6. The composition according to claim 1, in which Y zeolite is obtained by a method comprising the steps of: a) контактирование Y цеолита с фторсиликатной солью в форме водного раствора; иa) contacting the Y zeolite with a fluorosilicate salt in the form of an aqueous solution; and b) прокаливание цеолита, полученного на стадии (а), в присутствии водяных паров.b) calcining the zeolite obtained in stage (a) in the presence of water vapor. 7. Композиция по п.1, в которой Y цеолит имеет размер элементарной ячейки от 24,26 до 24,30 Å.7. The composition according to claim 1, in which the Y zeolite has a unit cell size of from 24.26 to 24.30 Å. 8. Композиция по п.1, в которой отношение Y цеолита к бета-цеолиту по массе составляет от 2,5 до 3,0 в высушенном состоянии.8. The composition according to claim 1, in which the ratio of Y zeolite to beta zeolite by weight is from 2.5 to 3.0 in the dried state. 9. Композиция по п.1, в которой катализатор содержит от более 2 мас.% до не более 3 мас.% бета-цеолита, в расчете на объединенный вес бета-цеолита, Y-цеолита и носителя в высушенном состоянии.9. The composition according to claim 1, in which the catalyst contains from more than 2 wt.% Up to no more than 3 wt.% Beta zeolite, calculated on the combined weight of beta zeolite, Y zeolite and carrier in the dried state. 10. Способ гидрокрекинга углеводородного сырья, который включает контактирование сырья при температуре от 232 до 454°С и избыточном давлении от 5171 до 24132 кПа в присутствии водорода с катализатором по любому из предшествующих пунктов. 10. A method of hydrocracking a hydrocarbon feedstock, which comprises contacting the feedstock at a temperature of 232 to 454 ° C. and an overpressure of 5171 to 24132 kPa in the presence of hydrogen with a catalyst according to any one of the preceding paragraphs.
RU2009105256/04A 2006-07-17 2007-07-09 HYDROCRACKING CATALYST CONTAINING BETA- AND Y-ZEOLITES, AND METHOD OF ITS APPLICATION FOR OBTAINING A DISTILLATE RU2009105256A (en)

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US11/457,833 US20080011648A1 (en) 2006-07-17 2006-07-17 Hydrocracking Catalyst Containing Beta and Y Zeolites, and Process for its use to make Distillate
US11/457,833 2006-07-17

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US (1) US20080011648A1 (en)
EP (1) EP2041244A2 (en)
KR (1) KR20090025364A (en)
CN (1) CN101490217A (en)
AU (1) AU2007275504A1 (en)
CA (1) CA2657313A1 (en)
CL (1) CL2007002042A1 (en)
MX (1) MX2009000438A (en)
NO (1) NO20090743L (en)
RU (1) RU2009105256A (en)
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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
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