JP7046763B2 - Fluid cracking catalyst for hydrocarbon oil - Google Patents
Fluid cracking catalyst for hydrocarbon oil Download PDFInfo
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- JP7046763B2 JP7046763B2 JP2018160549A JP2018160549A JP7046763B2 JP 7046763 B2 JP7046763 B2 JP 7046763B2 JP 2018160549 A JP2018160549 A JP 2018160549A JP 2018160549 A JP2018160549 A JP 2018160549A JP 7046763 B2 JP7046763 B2 JP 7046763B2
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- 239000003054 catalyst Substances 0.000 title claims description 136
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 24
- 229930195733 hydrocarbon Natural products 0.000 title claims description 24
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 24
- 238000005336 cracking Methods 0.000 title claims description 12
- 239000012530 fluid Substances 0.000 title claims description 5
- 239000011148 porous material Substances 0.000 claims description 105
- 239000003921 oil Substances 0.000 claims description 56
- 239000010457 zeolite Substances 0.000 claims description 55
- 229910021536 Zeolite Inorganic materials 0.000 claims description 53
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 53
- 239000002253 acid Substances 0.000 claims description 50
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- 238000009826 distribution Methods 0.000 claims description 28
- 239000011230 binding agent Substances 0.000 claims description 25
- 238000004523 catalytic cracking Methods 0.000 claims description 24
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 23
- 238000004231 fluid catalytic cracking Methods 0.000 claims description 19
- 239000000203 mixture Substances 0.000 claims description 9
- 239000002734 clay mineral Substances 0.000 claims description 7
- 239000002841 Lewis acid Substances 0.000 claims description 6
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- ICAKDTKJOYSXGC-UHFFFAOYSA-K lanthanum(iii) chloride Chemical compound Cl[La](Cl)Cl ICAKDTKJOYSXGC-UHFFFAOYSA-K 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
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- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 2
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- WWZKQHOCKIZLMA-UHFFFAOYSA-N octanoic acid Chemical compound CCCCCCCC(O)=O WWZKQHOCKIZLMA-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 2
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- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
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- 238000010521 absorption reaction Methods 0.000 description 1
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- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- HPTYUNKZVDYXLP-UHFFFAOYSA-N aluminum;trihydroxy(trihydroxysilyloxy)silane;hydrate Chemical compound O.[Al].[Al].O[Si](O)(O)O[Si](O)(O)O HPTYUNKZVDYXLP-UHFFFAOYSA-N 0.000 description 1
- JRPBQTZRNDNNOP-UHFFFAOYSA-N barium titanate Chemical compound [Ba+2].[Ba+2].[O-][Ti]([O-])([O-])[O-] JRPBQTZRNDNNOP-UHFFFAOYSA-N 0.000 description 1
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- AOWKSNWVBZGMTJ-UHFFFAOYSA-N calcium titanate Chemical compound [Ca+2].[O-][Ti]([O-])=O AOWKSNWVBZGMTJ-UHFFFAOYSA-N 0.000 description 1
- XFWJKVMFIVXPKK-UHFFFAOYSA-N calcium;oxido(oxo)alumane Chemical compound [Ca+2].[O-][Al]=O.[O-][Al]=O XFWJKVMFIVXPKK-UHFFFAOYSA-N 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
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- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- UAMZXLIURMNTHD-UHFFFAOYSA-N dialuminum;magnesium;oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[Mg+2].[Al+3].[Al+3] UAMZXLIURMNTHD-UHFFFAOYSA-N 0.000 description 1
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Description
本発明は、ガソリンや中間留分（ＬＣＯ）の収率を高く維持しつつ、重質留分の低減に特に有効な炭化水素油の流動接触分解触媒に関する。 The present invention relates to a fluid catalytic cracking catalyst for hydrocarbon oils, which is particularly effective in reducing heavy fractions while maintaining high yields of gasoline and intermediate fractions (LCOs).
一般に、炭化水素油の接触分解に用いられる接触分解用触媒は、固体酸であるゼオライトを含んでいる。かかる接触分解用触媒としては、常圧蒸留残油などの重質炭化水素油に対する分解能力（「ボトム分解能」ともいう）が高いこと、あるいは、触媒表面に析出するコークの析出量が少ないことなど、種々の観点で高い性能を発揮できるものが求められている。一方で、この接触分解用触媒については、ボトム分解能を向上させるためにゼオライトの含有割合を増加させると、耐摩耗性が低下したり、コークの析出量が増加したりするなどの問題がある。 Generally, catalytic cracking catalysts used for catalytic cracking of hydrocarbon oils contain zeolite, which is a solid acid. Such catalytic cracking catalysts have high cracking ability (also referred to as "bottom resolution") for heavy hydrocarbon oils such as atmospheric distillation residual oil, or have a small amount of coke deposited on the catalyst surface. , Those capable of exhibiting high performance from various viewpoints are required. On the other hand, with respect to this catalytic cracking catalyst, if the content ratio of zeolite is increased in order to improve the bottom resolution, there are problems such as a decrease in wear resistance and an increase in the amount of coke precipitation.
例えば、特許文献１には、残油（ボトム）分解活性流動接触分解用触媒として、ゼオライトとケイ素系酸化物とアルミナバインダーとを含み、（ａ）マクロ孔の細孔容積に対するメソ孔の細孔容積の割合を規定し、（ｂ）細孔容積を０．２５～０．３５ｍｌ／ｇの範囲内に規定し、さらに、（ｃ）水蒸気処理した触媒について、全固体酸量および全固体酸量に対する吸着熱が特定の範囲内の固体酸量の割合を規定した残油分解活性流動接触分解用触媒が開示されている。
For example,
また、特許文献２および３には、石油原料をより低沸点の生成物に転化するための流動接触分解方法に用いられる触媒として、その触媒成分にルイス酸性を高める化合物を添加した結晶性微孔質酸化物触媒が開示されている。 Further, in Patent Documents 2 and 3, as a catalyst used in a fluid catalytic cracking method for converting a petroleum raw material into a product having a lower boiling point, crystalline micropores in which a compound for enhancing Lewis acidity is added to the catalyst component. Cracking catalysts are disclosed.
しかしながら、従来の前記流動接触分解触媒は、実際には、低重質留分を十分に達成し、かつ、ガソリンや中間留分（軽油や灯油：ＬＣＯ）を高収率で得る触媒になっていないのが実情である。 However, the conventional fluid catalytic cracking catalyst is actually a catalyst that sufficiently achieves a low heavy fraction and obtains gasoline or an intermediate fraction (light oil or kerosene: LCO) in a high yield. The reality is that there is no such thing.
そこで、本発明は、従来材が抱えている前述した事情を考慮して開発したものであって、ガソリンや中間留分（ＬＣＯ）の収率を高く維持しつつ、重質留分の低減に特に有効な炭化水素油の流動接触分解触媒を提供することを目的とする。 Therefore, the present invention has been developed in consideration of the above-mentioned circumstances of conventional materials, and is used to reduce heavy distillates while maintaining high yields of gasoline and intermediate distillates (LCO). It is an object of the present invention to provide a particularly effective flow catalytic cracking catalyst for a hydrocarbon oil.
このような技術的背景のもと、発明者らは、上記課題を解決すべく鋭意検討した結果、特定の細孔分布（細孔径―細孔容積分布）を持ち、特定の種および量の固体酸を有する流動接触分解触媒では高い重質油分解能を示すことを見出した。 Against this technical background, the inventors have diligently studied to solve the above problems, and as a result, they have a specific pore distribution (pore diameter-pore volume distribution), and a specific species and amount of solid. It has been found that a fluid catalytic cracking catalyst with an acid exhibits high heavy oil resolution.
前記課題を解決し上記の目的を実現するため開発した本発明は、下記のとおりのものである。すなわち、本発明は、ゼオライトとアルミナバインダーとを含む炭化水素油用流動接触分解触媒であって、
（ａ）擬平衡化を施した後の細孔分布において、細孔径が４ｎｍ以上５０ｎｍ以下である細孔容積（ＰＶ１）の、細孔径が５０ｎｍより大きい細孔容積（ＰＶ２）に対する割合（ＰＶ１／ＰＶ２）が０．８以上１．５以下であり、かつ
（ｂ）ルイス酸量（Ｌ酸量）が３５μｍｏｌ／ｇ以上であって、そのルイス酸量とブレンステッド酸量（Ｂ酸量）との割合（Ｂ酸量／Ｌ酸量）が０．２以上であることを特徴とする炭化水素油用流動接触分解触媒である。
The present invention developed to solve the above problems and realize the above object is as follows. That is, the present invention is a fluid catalytic cracking catalyst for hydrocarbon oils containing zeolite and an alumina binder.
(A) In the pore distribution after quasi-equilibrium, the ratio of the pore volume (PV1) having a pore diameter of 4 nm or more and 50 nm or less to the pore volume (PV2) having a pore diameter larger than 50 nm (PV1 /). PV2) is 0.8 or more and 1.5 or less, and (b) Lewis acid amount (L acid amount) is 35 μmol / g or more, and the Lewis acid amount and Bronsted acid amount (B acid amount) The fluid catalytic decomposition catalyst for hydrocarbon oil is characterized in that the ratio (Amount of B acid / amount of L acid) is 0.2 or more.
なお、本発明に係る上記流動接触分解触媒については、
（１）前記細孔分布は、さらに、細孔径が４ｎｍより大きい細孔容積（ＰＶ３）と、細孔径が３０ｎｍ以上１００ｎｍ以下の細孔容積（ＰＶ４）との割合（ＰＶ４／ＰＶ３）が０．２０以上であること、
（２）前記触媒は、触媒組成基準で、前記ゼオライトを１５～６０質量％、前記アルミナバインダーを５～３０質量％含有していること、
（３）前記アルミナバインダーは、下記（ａ）～（ｃ）から選ばれるいずれか少なくとも１種を含むこと、（ａ）塩基性塩化アルミニウム、（ｂ）重リン酸アルミニウム、（ｃ）アルミナゾル、
（４）前記ゼオライトは、ＦＡＵ型（フォージャサイト型）、ＭＦＩ型、ＣＨＡ型、およびＭＯＲ型のいずれか１種又は２種以上であること、
（５）前記ＦＡＵ型のゼオライトは、水素型Ｙ型ゼオライト（ＨＹ）、超安定化Ｙ型ゼオライト（ＵＳＹ）、レアアース交換Ｙ型ゼオライト（ＲＥＹ）、およびレアアース交換超安定化Ｙ型ゼオライト（ＲＥＵＳＹ）のいずれかであること、
（６）前記触媒は、粘土鉱物を含むこと、
などがより好ましい解決手段になり得るものと考えられる。
Regarding the above-mentioned fluidized cracking catalyst according to the present invention,
(1) In the pore distribution, the ratio (PV4 / PV3) of the pore volume (PV3) having a pore diameter larger than 4 nm and the pore volume (PV4) having a pore diameter of 30 nm or more and 100 nm or less is 0. Being 20 or more,
(2) The catalyst contains 15 to 60% by mass of the zeolite and 5 to 30% by mass of the alumina binder based on the catalyst composition.
(3) The alumina binder contains at least one selected from the following (a) to (c), (a) basic aluminum chloride, (b) heavy aluminum phosphate, (c) alumina sol, and the like.
(4) The zeolite is one or more of FAU type (Faujasite type), MFI type, CHA type, and MOR type.
(5) The FAU-type zeolite includes hydrogen-type Y-type zeolite (HY), ultra-stabilized Y-type zeolite (USY), rare earth exchange Y-type zeolite (REY), and rare earth exchange ultra-stabilized Y-type zeolite (REUSY). Being one of
(6) The catalyst contains clay minerals.
Etc. may be a more preferable solution.
以上説明したように、本発明によれば、適切な細孔分布を有すると共に、適切な固体酸量、比率を有する流動接触分解触媒とすることにより、液体であるガソリンの収率やＬＣＯの収率を高く維持しつつ、特に重質留分を低減することができるようになる。 As described above, according to the present invention, the yield of liquid gasoline and the yield of LCO can be obtained by using a fluid catalytic cracking catalyst having an appropriate pore distribution and an appropriate amount and ratio of solid acid. It will be possible to reduce the heavy fraction in particular while maintaining a high rate.
本発明は重質留分（ボトム）の分解性能に優れた炭化水素油用流動接触分解触媒（以下、「本発明触媒」という）であり、以下に本発明触媒について、説明する。 The present invention is a fluid catalytic cracking catalyst for hydrocarbon oils (hereinafter referred to as "catalyst of the present invention") having excellent cracking performance of a heavy fraction (bottom), and the catalyst of the present invention will be described below.
本発明触媒は、ゼオライトとアルミナバインダーとを含む炭化水素油用流動接触分解触媒である。 The catalyst of the present invention is a fluid catalytic cracking catalyst for hydrocarbon oils containing zeolite and an alumina binder.
＜ゼオライト＞
本発明触媒は、基本的にゼオライト（結晶性アルミナシリケート）を含有するものである。このゼオライトは、接触分解プロセス、特に流動接触分解プロセスにて炭化水素油に対する接触分解活性を持つゼオライトであれば、特段の限定はない。例えば、ＦＡＵ型（フォージャサイト型。例えば、Ｙ型ゼオライト、Ｘ型ゼオライト等）、ＭＦＩ型（例えば、ＺＳＭ－５、ＴＳ－１等）、ＣＨＡ型(例えば、チャバサイト、ＳＡＰＯ－３４等)、およびＭＯＲ型（例えば、モルデナイト、Ｃａ－Ｑ等）のいずれか１又は２以上であり、特にＦＡＵ型が好適である。なお、フォージャサイト型のゼオライトとしては、水素型Ｙ型ゼオライト（ＨＹ）、超安定化Ｙ型ゼオライト（ＵＳＹ）や、ＨＹおよびＵＳＹにそれぞれ希土類金属をイオン交換等により担持させたレアアース交換Ｙ型ゼオライト（ＲＥＹ）、あるいはレアアース交換超安定化Ｙ型ゼオライト（ＲＥＵＳＹ）が例示される。
<Zeolite>
The catalyst of the present invention basically contains zeolite (crystalline alumina silicate). This zeolite is not particularly limited as long as it is a zeolite having catalytic cracking activity against hydrocarbon oil in a catalytic cracking process, particularly a fluid cracking process. For example, FAU type (forejasite type, for example, Y-type zeolite, X-type zeolite, etc.), MFI type (for example, ZSM-5, TS-1, etc.), CHA type (for example, chabasite, SAPO-34, etc.). , And any one or more of MOR type (for example, mordenite, Ca—Q, etc.), and FAU type is particularly preferable. The Faujasite type zeolite includes hydrogen type Y type zeolite (HY), ultra-stabilized Y type zeolite (USY), and rare earth exchange Y type in which rare earth metals are supported on HY and USY by ion exchange or the like. Zeolites (REY) or rare earth exchange ultra-stabilized Y-type zeolite (REUSY) are exemplified.
＜アルミナバインダー＞
本発明触媒は、基本的にアルミナバインダーを含有するものである。このアルミナバインダーの原料としては、例えば塩基性塩化アルミニウム（［Ａｌ２（ＯＨ）ｎＣｌ６-ｎ］ｍ（但し、０＜ｎ＜６、ｍ≦１０））を用いられる。その他、重リン酸アルミニウム溶液やジブサイト、バイアライト、ベーマイト、ベントナイト、結晶性アルミナなどを酸溶液中に溶解させた粒子、ベーマイトゲル、無定形のアルミナゲルを水溶液中に分散させた粒子、あるいはアルミナゾルも使用することができる。これらは単独もしくは混合して、または複合して用いることができる。なお、塩基性塩化アルミニウムは、ゼオライトなどに含まれるアルミニウムやナトリウム、カリウムなどのカチオンの存在下で２００～４５０℃程度の比較的低温で分解する。その結果、該塩基性塩化アルミニウムの一部は分解して、水酸化アルミニウムなどの分解物が存在するサイトがゼオライトの近傍に形成されるものと考えられる。さらに分解した塩基性塩化アルミニウムというのは、３００～６００℃の範囲の温度で焼成すると、アルミナバインダー（アルミナ）を形成する。このとき、ゼオライト近傍の分解物が焼成されてアルミナバインダーになる際に、細孔径が４ｎｍ以上、５０ｎｍ以下の範囲のメソ孔が比較的多く形成され、本発明触媒の比表面積の増大に寄与すると推定される。一方で、このとき、細孔径が５０ｎｍより大きく１０００ｎｍ以下の範囲にある、耐摩耗性を低下させる要因となるマクロ孔の形成を抑えることも確認している。
<Alumina binder>
The catalyst of the present invention basically contains an alumina binder. As a raw material for this alumina binder, for example, basic aluminum chloride ([Al 2 (OH) n Cl 6-n ] m (where 0 <n <6, m ≦ 10)) is used. In addition, particles obtained by dissolving dibusite, biarite, boehmite, bentonite, crystalline alumina, etc. in an acid solution, boehmite gel, particles in which atypical alumina gel is dispersed in an aqueous solution, or alumina sol. Can also be used. These can be used alone, in admixture, or in combination. Basic aluminum chloride decomposes at a relatively low temperature of about 200 to 450 ° C. in the presence of cations such as aluminum, sodium and potassium contained in zeolite and the like. As a result, it is considered that a part of the basic aluminum chloride is decomposed to form a site in the vicinity of the zeolite in which a decomposition product such as aluminum hydroxide is present. Further decomposed basic aluminum chloride forms an alumina binder (alumina) when fired at a temperature in the range of 300 to 600 ° C. At this time, when the decomposition product in the vicinity of zeolite is calcined to form an alumina binder, a relatively large number of mesopores having a pore diameter of 4 nm or more and 50 nm or less are formed, which contributes to an increase in the specific surface area of the catalyst of the present invention. Presumed. On the other hand, at this time, it has also been confirmed that the formation of macropores having a pore diameter larger than 50 nm and 1000 nm or less, which is a factor for reducing wear resistance, is suppressed.
本発明触媒において、前記アルミナバインダーは、マトリックス成分中のアルミナとして検出される。したがって、アルミナバインダーは、マトリックス成分の一部を構成すると共に、ゼオライトとマトリックス成分を結合する目的で添加することが好ましい。 In the catalyst of the present invention, the alumina binder is detected as alumina in the matrix component. Therefore, it is preferable to add the alumina binder for the purpose of forming a part of the matrix component and binding the zeolite and the matrix component.
＜添加物＞
前述のゼオライト、アルミナバインダーに加え、本発明触媒は、マトリックス成分の原料として、種々の添加物を添加することができる。その添加物としては、活性マトリックス成分、粘土鉱物、メタルトラップ剤などを用いることができる。
<Additives>
In addition to the above-mentioned zeolite and alumina binder, the catalyst of the present invention can add various additives as raw materials for matrix components. As the additive, an active matrix component, a clay mineral, a metal trapping agent and the like can be used.
前記活性マトリックス成分としては、活性アルミナやシリカ－アルミナ、シリカ－マグネシア、アルミナ－マグネシア、シリカ－マグネシア－アルミナなどの固体酸を有する物質を含むものを用いることが好ましい。 As the activated matrix component, it is preferable to use a substance containing a substance having a solid acid such as activated alumina, silica-alumina, silica-magnesia, alumina-magnesia, and silica-magnesia-alumina.
前記粘土鉱物としては、カオリンやベントナイト、カオリナイト、ハロイサイト、モンモリロナイトなどを用いることが好ましい。さらに好ましくはカオリンが用いられる。 As the clay mineral, it is preferable to use kaolin, bentonite, kaolinite, halloysite, montmorillonite and the like. More preferably, kaolin is used.
前記メタルトラップ剤としては、アルミナ粒子やリン－アルミナ粒子、結晶性カルシウムアルミネート、セピオライト、チタン酸バリウム、スズ酸カルシウム、チタン酸ストロンチウム、酸化マンガン、マグネシア、マグネシア－アルミナなどを用いることが好ましい。また、該メタルトラップ剤の原料としては、酸化雰囲気で焼成することによりアルミナなどとなるベーマイトなどの前駆体物質を用いることができる。 As the metal trapping agent, it is preferable to use alumina particles, phosphorus-alumina particles, crystalline calcium aluminate, sepiolite, barium titanate, calcium titanate, strontium titanate, manganese oxide, magnesia, magnesia-alumina and the like. Further, as a raw material of the metal trapping agent, a precursor substance such as boehmite which becomes alumina or the like by firing in an oxidizing atmosphere can be used.
本発明触媒には、希土類金属（Ｒａｒｅ Ｅａｒｔｈ：ＲＥ）をイオン交換したものを含有させてもよい。その希土類金属としては、例えば、セリウム（Ｃｅ）やランタン（Ｌａ）、プラセオジウム（Ｐｒ）、およびネオジム（Ｎｄ）などの使用が可能である。これらは単独ないし２種以上の金属酸化物としてもよい。なおこれらは、ゼオライトをイオン交換したものでもよく、それは希土類金属を含むことで、ゼオライトの耐水熱性が向上するからである。 The catalyst of the present invention may contain a rare earth metal (Rare Earth: RE) that has been ion-exchanged. As the rare earth metal, for example, cerium (Ce), lanthanum (La), praseodymium (Pr), neodymium (Nd) and the like can be used. These may be used alone or as two or more kinds of metal oxides. It should be noted that these may be those obtained by ion-exchanged zeolite, because the inclusion of rare earth metals improves the water heat resistance of zeolite.
＜組成比＞
本発明触媒は、ゼオライト、アルミナバインダーおよび添加物由来の上述した物質を多種類含むことから、その組成を一概に特定することは困難であるが、以下に、本発明触媒の典型的な組成例を挙げる。
<Composition ratio>
Since the catalyst of the present invention contains many kinds of the above-mentioned substances derived from zeolites, alumina binders and additives, it is difficult to unconditionally specify the composition thereof, but the following are typical composition examples of the catalyst of the present invention. List.
前記ゼオライトは、１５～６０質量％が好ましい。より好ましくは２０～５０質量％である。さらに好ましくは２０～４０質量％である。その理由は、触媒に対するゼオライトの含有量が、１５％未満では接触分解活性が低くなる傾向があり、また、６０質量％を超えると接触分解活性が高くなりすぎてコークの析出量が多くなり、また、嵩密度が高くなると共に強度が低くなるためである。 The zeolite is preferably 15 to 60% by mass. More preferably, it is 20 to 50% by mass. More preferably, it is 20 to 40% by mass. The reason is that when the content of zeolite with respect to the catalyst is less than 15%, the catalytic cracking activity tends to be low, and when it exceeds 60% by mass, the catalytic cracking activity becomes too high and the amount of cork precipitated increases. This is also because the bulk density increases and the strength decreases.
前記アルミナバインダー成分は、５～３０質量％含有することが好ましい。より好ましくは１０～２５質量％である。その理由は、バインダー成分が５質量％より少ないと接触分解活性が高くなるものの、触媒のアトリッション（摩耗）強度が十分に保てない。一方、３０質量％より多いと、十分な接触分解活性が得られないおそれがある。 The alumina binder component is preferably contained in an amount of 5 to 30% by mass. More preferably, it is 10 to 25% by mass. The reason is that if the binder component is less than 5% by mass, the catalytic cracking activity becomes high, but the attrition (wear) strength of the catalyst cannot be sufficiently maintained. On the other hand, if it is more than 30% by mass, sufficient catalytic cracking activity may not be obtained.
前記希土類金属を用いる場合、ＲＥ２Ｏ３を、１０．０質量％以下、好ましくは０．５～５．０質量％となるように含有させる。ここで、触媒としては、ＲＥ２Ｏ３／ゼオライト質量比が一定となるように、ＲＥ２Ｏ３の添加量を調整する。 When the rare earth metal is used, RE 2 O 3 is contained in an amount of 10.0% by mass or less, preferably 0.5 to 5.0% by mass. Here, as the catalyst, the amount of RE 2 O 3 added is adjusted so that the RE 2 O 3 / zeolite mass ratio becomes constant.
さらに、本発明触媒には、粘土鉱物を１５～４５質量％含有させることができる。その理由は、粘土鉱物が１５質量％未満では、活性成分が多くなるため、コーク生成が過剰となり十分な性能を示さない場合があるためであり、一方、４５質量％を超えると触媒中の固体酸量が少なくなりすぎて触媒活性が低下する恐れがある。また、本発明触媒がメタルトラップ剤を含む場合、その含有量は、各組成物中に０．１～１０質量％、好ましくは０．１～５質量％の範囲内とする。 Further, the catalyst of the present invention can contain 15 to 45% by mass of clay mineral. The reason is that if the clay mineral content is less than 15% by mass, the amount of active components increases, so that coke formation may be excessive and the performance may not be sufficient. On the other hand, if the clay mineral content exceeds 45% by mass, the solid in the catalyst may not be exhibited. The amount of acid may be too small and the catalytic activity may decrease. When the catalyst of the present invention contains a metal trapping agent, the content thereof is in the range of 0.1 to 10% by mass, preferably 0.1 to 5% by mass in each composition.
＜擬平衡化処理＞
炭化水素油の流動接触分解触媒の性能を実験室の反応装置で評価する際には、前処理として擬平衡化と呼ばれる処理を行う。この擬平衡化処理は、流動接触分解触媒にＶやＮｉ等のメタルを担持してスチーム処理を行うことで、活性を平衡触媒と同等のレベルまで低下させる処理である。この擬平衡化の処理により、平衡触媒の性状を再現することは、より精度の高い活性評価を得るためには重要である。
<Pseudo-equilibrium processing>
When evaluating the performance of a hydrocracking catalytic cracking catalyst in a laboratory reactor, a process called quasi-equilibrium is performed as a pretreatment. This quasi-equilibrium treatment is a treatment in which a metal such as V or Ni is supported on a fluidized catalytic cracking catalyst and steam treatment is performed to reduce the activity to the same level as that of the equilibrium catalyst. It is important to reproduce the properties of the equilibrium catalyst by this quasi-equilibrium treatment in order to obtain a more accurate activity evaluation.
＜比表面積の測定＞
擬平衡化処理を施した触媒は、ＢＥＴ法、例えば、ＭＯＵＮＴ ＥＣＨ社製Ｍａｃｓｏｒｂ ＨＭ ｍｏｄｅｌ―１２００を用いて、比表面積を測定する。また、マトリックス成分の比表面積は、例えば、日本ベル製ベルソープｍｉｎｉ―ＩＩ型を用いて、窒素の吸着等温線を測定し、得られた吸着側の等温線からＶａ－ｔプロットにより求める。なお、全体の比表面積からマトリックス成分の比表面積を差し引くことでゼオライト成分の比表面積を求めることができる。本発明では、触媒全体の比表面積（ＳＡ）は、１００～２００ｍ２／ｇの範囲にあることが好ましい。マトリックス成分の比表面積は４５ｍ２／ｇ以上が好ましく、さらに５０ｍ２／ｇ以上であることがより好ましい。
<Measurement of specific surface area>
The quasi-equilibrium-treated catalyst is measured for specific surface area using a BET method, for example, a Macsorb HM model-1200 manufactured by MOUNT ECH. Further, the specific surface area of the matrix component is determined by measuring the adsorption isotherm of nitrogen using, for example, Bell Soap mini-II manufactured by Nippon Bell, and using the Vat plot from the obtained isotherm on the adsorption side. The specific surface area of the zeolite component can be obtained by subtracting the specific surface area of the matrix component from the total specific surface area. In the present invention, the specific surface area (SA) of the entire catalyst is preferably in the range of 100 to 200 m 2 / g. The specific surface area of the matrix component is preferably 45 m 2 / g or more, more preferably 50 m 2 / g or more.
＜細孔径－細孔容積分布の測定＞
擬平衡化処理を施した触媒は、水銀圧入法により細孔径－細孔容積分布を測定する。測定装置としては、例えば、Ｑｕａｎｔａ ｃｈｒｏｍｅ社製Ｐｏｒｅ Ｍａｓｔｅｒ－６０ＧＴを用いて、細孔径－細孔容積分布を測定する。細孔径は、水銀の表面張力４８０ｄｙｎｅ／ｃｍ、接触角１５０°を用いて計算した値である。また、各細孔径範囲の細孔容積（ＰＶｎ）は、水銀圧入法により測定した各細孔直径範囲における細孔容積の積算値である。本発明では、触媒の全細孔容積（ＰＶ）は、０．１５ｍｌ／ｇ以上、さらに好ましくは０．２０～０．４０ｍｌ／ｇの範囲にあることが好ましい。
<Measurement of pore size-pore volume distribution>
For the catalyst subjected to the quasi-equilibrium treatment, the pore diameter-pore volume distribution is measured by the mercury intrusion method. As a measuring device, for example, a Pore Master-60GT manufactured by Quanta Chrome is used to measure the pore diameter-pore volume distribution. The pore diameter is a value calculated using a surface tension of mercury of 480 dyne / cm and a contact angle of 150 °. The pore volume (PVn) in each pore diameter range is an integrated value of the pore volume in each pore diameter range measured by the mercury intrusion method. In the present invention, the total pore volume (PV) of the catalyst is preferably in the range of 0.15 ml / g or more, more preferably 0.20 to 0.40 ml / g.
上記試験により測定した触媒の細孔径－細孔容積分布の一例を図１に示す。横軸に細孔径（ｎｍ）を、縦軸にログ微分細孔容積ｄＶｐ／ｄｌｏｇｄを取っている。後述する実施例に基づき、ａおよびｂは本発明触媒の分布を、ｃは比較例の触媒の分布を表す。図１によれば、本発明触媒ａは細孔径５ｎｍ～３００ｎｍまで０．１ｍｌ／ｇ以上のログ微分細孔容積分布を持っており、比較例触媒ｃに比べ、バランスの良い細孔径－細孔容積分布を持っているといえる。 FIG. 1 shows an example of the pore diameter-pore volume distribution of the catalyst measured by the above test. The horizontal axis represents the pore diameter (nm), and the vertical axis represents the log differential pore volume dVp / dlogd. Based on the examples described later, a and b represent the distribution of the catalyst of the present invention, and c represents the distribution of the catalyst of the comparative example. According to FIG. 1, the catalyst a of the present invention has a log differential pore volume distribution of 0.1 ml / g or more from a pore diameter of 5 nm to 300 nm, and has a well-balanced pore diameter-pores as compared with the comparative example catalyst c. It can be said that it has a volume distribution.
流動接触分解触媒の比表面積が小さすぎ、全細孔容積が小さすぎる場合には、所望の分解反応活性が得られないことがある。比表面積の増大の観点からは、径の小さい細孔が多数あることが好ましい。ただし、４ｎｍ未満の細孔径では重質油の接触分解への寄与が小さいので、４ｎｍ以上の細孔径を有することが好ましい。また、炭化水素油の接触分解においては、コーク収率を低減する反応面からは、触媒の細孔は細孔直径が１０ｎｍより大きい方が反応物の拡散性がよくなるので望ましい。一方、細孔直径が１０００ｎｍより大きい細孔は、触媒の耐摩耗性を悪くすることがあるので少ない方が望ましい。 If the specific surface area of the fluid catalytic cracking catalyst is too small and the total pore volume is too small, the desired cracking reaction activity may not be obtained. From the viewpoint of increasing the specific surface area, it is preferable that there are many pores having a small diameter. However, if the pore diameter is less than 4 nm, the contribution of heavy oil to catalytic cracking is small, so it is preferable to have a pore diameter of 4 nm or more. Further, in the catalytic cracking of hydrocarbon oil, from the reaction surface for reducing the cork yield, it is desirable that the pores of the catalyst have a pore diameter larger than 10 nm because the diffusivity of the reactant is improved. On the other hand, it is desirable that the number of pores having a pore diameter larger than 1000 nm is smaller because it may deteriorate the wear resistance of the catalyst.
本発明触媒は、擬平衡化が施された後の細孔径－細孔容積分布について、細孔径が４ｎｍ以上５０ｎｍ以下の範囲のメソ細孔容積（ＰＶ１）の、細孔径が５０ｎｍより大きい範囲のマクロ細孔容積（ＰＶ２）に対する割合（ＰＶ１／ＰＶ２）が０．８以上１．５以下であり、このような細孔構造をとることによって、高い重質留分の分解能をもつことになる。
その理由は前記（ＰＶ１／ＰＶ２）が０．８未満では重質留分の分解能が十分ではなく、（ＰＶ１／ＰＶ２）が高すぎるとコーク生成が増加する恐れがあるので１．５以下とする。好ましくは、（ＰＶ１／ＰＶ２）が１．０～１．３の範囲である。
In the catalyst of the present invention, regarding the pore diameter-pore volume distribution after quasi-equilibrium, the mesopore volume (PV1) having a pore diameter in the range of 4 nm or more and 50 nm or less has a pore diameter larger than 50 nm. The ratio (PV1 / PV2) to the macropore volume (PV2) is 0.8 or more and 1.5 or less, and by adopting such a pore structure, a high resolution of the heavy fraction is obtained.
The reason is that if (PV1 / PV2) is less than 0.8, the resolution of the heavy fraction is not sufficient, and if (PV1 / PV2) is too high, cork formation may increase, so the resolution should be 1.5 or less. .. Preferably, (PV1 / PV2) is in the range of 1.0 to 1.3.
さらに、細孔径が４ｎｍより大きい範囲の細孔容積（ＰＶ３）に対する、細孔径が３０ｎｍ以上１００ｎｍ以下の範囲の細孔容積（ＰＶ４）割合（ＰＶ４／ＰＶ３）が０．２０以上であることが好ましい。（ＰＶ４／ＰＶ３）が０．２０以上とすることで、ガソリンやＬＣＯの収率向上が望める。
（ＰＶ４／ＰＶ３）の上限は特に定めないが、触媒に含まれる構成成分のサイズに起因するため０．５０を上回ることは難しい。さらに好ましくは、（ＰＶ４／ＰＶ３）が０．２０～０．３０の範囲である。
Further, it is preferable that the ratio of the pore volume (PV4) in the range of the pore diameter of 30 nm or more and 100 nm or less (PV4 / PV3) to the pore volume (PV3) in the range of the pore diameter larger than 4 nm is 0.20 or more. .. By setting (PV4 / PV3) to 0.20 or more, the yield of gasoline or LCO can be expected to be improved.
The upper limit of (PV4 / PV3) is not particularly set, but it is difficult to exceed 0.50 because of the size of the constituents contained in the catalyst. More preferably, (PV4 / PV3) is in the range of 0.20 to 0.30.
＜固体酸量、Ｌ酸量、Ｂ酸量＞
固体酸とは、触媒が使用される温度領域において固体酸性を示すものであり、固体酸性の確認は、アンモニアを用いた昇温脱離法や、アンモニア又はピリジンを用いる in situ ＦＴＩＲ（フーリエ変換赤外線吸収スペクトル）法によりなされる。固体酸は、電子対受容体であるルイス酸（Ｌ酸）とプロトン供与体であるブレンステッド酸（Ｂ酸）に分類される。以下の説明におけるＬ酸量およびＢ酸量の測定は、ピリジンを用いる in situ ＦＴＩＲ法で実施した。
<Amount of solid acid, amount of L acid, amount of B acid>
The solid acid indicates solid acidity in the temperature range in which the catalyst is used, and confirmation of solid acidity can be performed by a thermal desorption method using ammonia or in situ FTIR (Fourier transform infrared) using ammonia or pyridine. Absorption spectrum) method. Solid acids are classified into Lewis acid (L acid), which is an electron pair acceptor, and Bronsted acid (B acid), which is a proton donor. The measurement of the amount of L acid and the amount of B acid in the following description was carried out by the in situ FTIR method using pyridine.
試料粉末４０ｍｇを２０ｍｍφのディスクに成型した後、真空ラインに接続されたＩＲセル（赤外分光分析用セル）に設置して、５００℃で一時間真空排気処理を行った。前処理後、１５０℃に降温して、ピリジン蒸気の導入前後の試料ディスクのＩＲ（赤外吸収）スペクトルを日本分光社製ＦＴ／ＩＲ－４６００で測定した。ブレンステッド酸点とルイス酸点の定量はC.A.Emeis,J.Catal.,141,347-354(1993)に基づいて行った。 After molding 40 mg of the sample powder into a disk having a diameter of 20 mm, the sample powder was placed in an IR cell (infrared spectroscopic analysis cell) connected to a vacuum line and subjected to vacuum exhaust treatment at 500 ° C. for 1 hour. After the pretreatment, the temperature was lowered to 150 ° C., and the IR (infrared absorption) spectrum of the sample disk before and after the introduction of the pyridine vapor was measured by FT / IR-4600 manufactured by JASCO Corporation. The quantification of Bronsted acid and Lewis acid points was performed based on C.A.Emeis, J.Catal., 141,347-354 (1993).
本発明触媒は、Ｌ酸量を３５μｍｏｌ／ｇ以上とする。Ｌ酸量が３５μｍｏｌ／ｇ未満では、良好な重質留分分解性能が得られない。好ましくはＬ酸量の上限を６０μｍｏｌ／ｇとする。これ以上増やすと活性が高くなりすぎて、水素等ガス成分が増加してしまうのでガソリン等の収率が下がってしまう。より好ましくは、Ｌ酸量：４０～５５μｍｏｌ／ｇの範囲である。 The catalyst of the present invention has an L acid content of 35 μmol / g or more. If the amount of L acid is less than 35 μmol / g, good heavy fraction decomposition performance cannot be obtained. Preferably, the upper limit of the amount of L acid is 60 μmol / g. If it is increased more than this, the activity becomes too high and the gas component such as hydrogen increases, so that the yield of gasoline or the like decreases. More preferably, the amount of L acid is in the range of 40 to 55 μmol / g.
また、本発明触媒は、Ｂ酸量／Ｌ酸量を０．２以上とする。Ｂ酸量／Ｌ酸量が０．２未満では、ガソリンやＬＣＯの収率が十分ではない。好ましくは、Ｂ酸量／Ｌ酸量：０．２５～０．６０、さらに好ましくは０．３０～０．５０の範囲である。 Further, the catalyst of the present invention has a B acid amount / L acid amount of 0.2 or more. If the amount of B acid / L acid is less than 0.2, the yield of gasoline or LCO is not sufficient. The amount of B acid / amount of L acid is preferably in the range of 0.25 to 0.60, more preferably 0.30 to 0.50.
［接触分解用触媒の製造方法］
次に、本発明触媒の好適な製造方法について説明する。
１．調整工程
前記した塩基性塩化アルミニウム水溶液（アルミナバインダー原料の一例）を純水で希釈し、超安定化Ｙ型ゼオライトおよび添加剤として、カオリン、活性アルミナを加えて、よく撹拌した後、塩化ランタン溶液を添加し、調合スラリーを調整する。添加物の組成は、予め、上記細孔分布、Ｌ酸量およびＢ酸量割合となるように把握したものを用いる。
[Manufacturing method of catalytic cracking catalyst]
Next, a suitable manufacturing method of the catalyst of the present invention will be described.
1. 1. Adjustment step The above-mentioned basic aluminum chloride aqueous solution (an example of an alumina binder raw material) is diluted with pure water, kaolin and activated alumina are added as ultra-stabilized Y-type zeolite and an additive, and the mixture is well stirred and then a lanthanum chloride solution. To prepare the compounded slurry. As the composition of the additive, the one that has been grasped in advance so as to have the pore distribution, the amount of L acid, and the ratio of the amount of B acid is used.
２．噴霧乾燥工程
上記の調合したスラリーを噴霧乾燥機の原料貯槽に充填し、２００～４５０℃の範囲の例えば２３０℃に調整された気流（例えば空気）が流れる乾燥チャンバー内に原料スラリーを噴霧することにより、噴霧乾燥粒子が得られる。原料スラリーの噴霧乾燥によって前記気流の温度は低下するが、乾燥チャンバーの出口の温度は、ヒーターなどを用いて１１０～３５０℃の範囲の例えば１３０℃に維持される。このとき、原料スラリー中のゼオライトに含まれる骨格外アルミナ中のアルミニウム及び当該ゼオライトから遊離したナトリウムとの反応により、アルミナバインダー原料である塩基性塩化アルミニウムの分解反応が進行する。
2. 2. Spray drying step Filling the raw material storage tank of the spray dryer with the prepared slurry, and spraying the raw material slurry into a drying chamber through which an air flow (for example, air) adjusted to, for example, 230 ° C. in the range of 200 to 450 ° C. flows. To obtain spray-dried particles. Although the temperature of the air flow is lowered by spray drying of the raw material slurry, the temperature at the outlet of the drying chamber is maintained in the range of 110 to 350 ° C., for example, 130 ° C. by using a heater or the like. At this time, the decomposition reaction of the basic aluminum chloride, which is the raw material of the alumina binder, proceeds by the reaction between the aluminum in the extraskeletal alumina contained in the zeolite in the raw material slurry and the sodium liberated from the zeolite.
３．焼成工程
３００～６００℃の範囲の例えば４００℃に調整された空気雰囲気下で前記噴霧乾燥粒子の焼成を行う。その結果、前記分解反応により分解した塩基性塩化アルミニウムの分解物がアルミナバインダーに変化する。このとき、先行する噴霧乾燥工程では、ゼオライトの表面で塩基性塩化アルミニウムの分解反応を進行させているので、ゼオライトの表面には分解反応で発生した分解物が付着する。このゼオライト表面の分解物を焼成してアルミナバインダーに変化させると、既知のメカニズムにより、接触分解用触媒となる焼成粒子の表面にメソ孔が多く形成される。また焼成粒子は、ゼオライトの表面に、接触分解活性を持つアルミナバインダーが積層された構造となる。
3. 3. Firing step The spray-dried particles are calcined in an air atmosphere adjusted to, for example, 400 ° C. in the range of 300 to 600 ° C. As a result, the decomposition product of basic aluminum chloride decomposed by the decomposition reaction is changed to an alumina binder. At this time, in the preceding spray drying step, the decomposition reaction of basic aluminum chloride is promoted on the surface of the zeolite, so that the decomposition products generated in the decomposition reaction adhere to the surface of the zeolite. When the cracked product on the surface of the zeolite is calcined and changed into an alumina binder, many mesopores are formed on the surface of the calcined particles serving as a catalyst for catalytic cracking by a known mechanism. Further, the calcined particles have a structure in which an alumina binder having catalytic cracking activity is laminated on the surface of zeolite.
４．洗浄・乾燥工程
前記焼成粒子を例えば純水中に分散させて焼成粒子スラリー液を形成し、次いで焼成粒子スラリーから水分を濾別して洗浄粒子ケーキを得る。さらに、当該洗浄粒子ケーキに純水を供給して再度の洗浄を行う。得られたケーキを１２０～６００℃の温度範囲例えば１４０℃に加熱された空気中で乾燥することにより本発明触媒が得られる。得られた触媒粒子の平均粒子径は、５０～１００μｍ程度である。
4. Cleaning / Drying Step The calcined particles are dispersed in, for example, pure water to form a calcined particle slurry liquid, and then water is filtered off from the calcined particle slurry to obtain a washed particle cake. Further, pure water is supplied to the cleaning particle cake to perform cleaning again. The catalyst of the present invention can be obtained by drying the obtained cake in air heated to a temperature range of 120 to 600 ° C., for example, 140 ° C. The average particle size of the obtained catalyst particles is about 50 to 100 μm.
本発明に係る流動接触分解触媒によれば、重質炭化水素油の分解能力が高く、ガソリンやＬＣＯの収率を高めることができる。 According to the fluid catalytic cracking catalyst according to the present invention, the cracking ability of heavy hydrocarbon oil is high, and the yield of gasoline or LCO can be increased.
＜流動接触分解方法＞
本発明に係る流動接触分解触媒を用いる流動接触分解については、通常の炭化水素油の流動接触分解条件を採用することができ、例えば、以下に述べる条件が好適である。
<Flow contact cracking method>
For the fluid catalytic cracking using the fluid catalytic cracking catalyst according to the present invention, ordinary fluid catalytic cracking conditions of hydrocarbon oil can be adopted, and for example, the conditions described below are suitable.
接触分解に使用される原料油としては、通常の炭化水素原料油、例えば、水素化脱硫減圧蒸留軽油（ＤＳＶＧＯ）や、減圧蒸留軽油（ＶＧＯ）を用いることができる他、常圧蒸留残渣油（ＡＲ）、減圧蒸留残渣油（ＶＲ）、脱硫常圧蒸留残渣油（ＤＳＡＲ）、脱硫減圧蒸留残渣油（ＤＳＶＲ）、脱アスファルテン油（ＤＡＯ）等の残渣油も使用することができ、これらの単独又は混合したものも使用できる。なお、本発明に係る流動接触分解触媒においては、ニッケルおよびバナジウムがそれぞれ０．５ｐｐｍ以上含まれている残渣油も処理可能であり、原料油として残渣油を単独で用いる残渣油接触分解装置（Ｒｅｓｉｄ ＦＣＣ。ＲＦＣＣ）にも使用できる。ここで、従来の流動接触分解触媒をＲＦＣＣで使用した場合には、残渣油中のニッケルおよびバナジウムが触媒に付着して活性が低下するが、本発明の流動接触分解触媒では、バナジウムおよびニッケルがそれぞれ０．５ｐｐｍ以上含有している残渣油を処理しても、優れた触媒性能を保持できる。また、本発明の流動接触分解触媒は、バナジウムおよびニッケルがそれぞれ３００ｐｐｍ以上含有されていても触媒性能を保持できる。本発明の流動接触分解触媒に含有されるバナジウムおよびニッケルの上限は、それぞれ１００００ｐｐｍ程度である。 As the raw material oil used for catalytic decomposition, ordinary hydrocarbon raw material oil, for example, hydrodesulfurized vacuum distillation light oil (DSVGO), vacuum distillation light oil (VGO) can be used, and atmospheric distillation residual oil (atmospheric distillation residue oil). Residual oils such as AR), hydrodesulfurized distillation residue oil (VR), hydrodesulfurized atmospheric distillation residue oil (DSAR), hydrodesulfurized vacuum distillation residue oil (DSVR), hydrodesulfurized oil (DAO), etc. can also be used, and these alone can be used. Alternatively, a mixture can also be used. In the fluid catalytic cracking catalyst according to the present invention, residual oil containing 0.5 ppm or more of nickel and vanadium can be treated, and the residual oil catalytic cracking apparatus (Resid) using the residual oil alone as a raw material oil can be processed. It can also be used for FCC (RFCC). Here, when a conventional flow catalytic cracking catalyst is used in RFCC, nickel and vanadium in the residual oil adhere to the catalyst and the activity decreases, but in the fluid cracking catalyst of the present invention, vanadium and nickel are used. Excellent catalytic performance can be maintained even when the residual oil containing 0.5 ppm or more of each is treated. Further, the fluid catalytic cracking catalyst of the present invention can maintain the catalytic performance even if vanadium and nickel each contain 300 ppm or more. The upper limits of vanadium and nickel contained in the fluid catalytic cracking catalyst of the present invention are each about 10,000 ppm.
また、前述の炭化水素原料油を接触分解する際の反応温度は４７０～５５０℃の範囲が好適に採用され、反応圧力は一般的にはおよそ１～３ｋｇ／ｃｍ2の範囲が好適であり、触媒／油の質量比（触媒／油比）は２．５～９．０の範囲が好ましく、更に接触時間は１０～６０ｈｒ-1の範囲が好ましい。 Further, the reaction temperature at the time of catalytic cracking of the above-mentioned hydrocarbon raw material oil is preferably in the range of 470 to 550 ° C., and the reaction pressure is generally preferably in the range of about 1 to 3 kg / cm 2 . The catalyst / oil mass ratio (catalyst / oil ratio) is preferably in the range of 2.5 to 9.0, and the contact time is preferably in the range of 10 to 60 hr -1 .
以下、本発明を実施例によりさらに詳細に説明するが、本発明はこれらの実施例に何ら制限されるものではない。
（実施例）
＜触媒ａ＞
ａ．調合工程
２３．５質量％の塩基性塩化アルミニウム水溶液５３１．９ｇと純水２９９．３ｇを混合した。次いで、この混合溶液をよく攪拌しながら、カオリン（固形分濃度：８４％質量）４５２．４ｇ、活性アルミナ粉末（固形分濃度：８１％質量）６１．７ｇ、事前に硫酸を用いてｐＨを３．１に調整した活性アルミナスラリー（ベーマイトゲルスラリー。固形分濃度：１０質量％）１５００ｇおよび超安定化Ｙ型ゼオライト粉末（固形分濃度：７５質量％）３３３．３ｇを順次添加した。その後、塩化ランタン溶液（Ｌａ２Ｏ３濃度：２９．１質量％）を１５４．６ｇ添加し、よく撹拌し、調合スラリーを得た。得られた調合スラリーは、ホモジナイザーを用いて分散処理を行い、固形分濃度が３０質量％、ｐＨが３．４であった。
Hereinafter, the present invention will be described in more detail with reference to Examples, but the present invention is not limited to these Examples.
(Example)
<Catalyst a>
a. Preparation step 531.9 g of a basic aluminum chloride aqueous solution of 23.5% by mass and 299.3 g of pure water were mixed. Then, while stirring this mixed solution well, the pH was adjusted to 32.4 g of kaolin (solid content concentration: 84% mass), 61.7 g of activated alumina powder (solid content concentration: 81% mass), and sulfuric acid in advance. 1500 g of activated alumina slurry (boehmite gel slurry. Solid content concentration: 10% by mass) adjusted to .1 and 333.3 g of ultra-stabilized Y-type zeolite powder (solid content concentration: 75% by mass) were sequentially added. Then, 154.6 g of a lanthanum chloride solution (La 2 O 3 concentration: 29.1% by mass) was added and stirred well to obtain a prepared slurry. The obtained prepared slurry was subjected to a dispersion treatment using a homogenizer, and had a solid content concentration of 30% by mass and a pH of 3.4.
ｂ．噴霧乾燥、焼成、洗浄、乾燥工程
調合スラリーを液滴として、入口温度が２３０℃、出口温度が１３０℃の噴霧乾燥機で噴霧乾燥を行い、平均粒子径が６８μｍの球状粒子を得た。この乾燥粉末は電気炉にて空気雰囲気下、４００℃で１時間焼成した後、焼成品に対して質量にて１０倍量の温水（６０℃）に懸濁させ、脱水濾過を施した。さらに、質量で１０倍量の温水（６０℃）を掛水した後、ケーキを回収し、雰囲気温度１４０℃に保持した乾燥機にて１０時間乾燥させ、触媒ａを得た。
b. Spray-drying, firing, washing, and drying steps Using the prepared slurry as droplets, spray-drying was performed with a spray-dryer having an inlet temperature of 230 ° C. and an outlet temperature of 130 ° C. to obtain spherical particles having an average particle diameter of 68 μm. This dry powder was fired in an electric furnace in an air atmosphere at 400 ° C. for 1 hour, then suspended in warm water (60 ° C.) 10 times by mass with respect to the fired product, and dehydrated and filtered. Further, after sprinkling 10 times the amount of warm water (60 ° C.) by mass, the cake was recovered and dried in a dryer maintained at an atmospheric temperature of 140 ° C. for 10 hours to obtain a catalyst a.
ｃ．擬平衡化工程
前記のようにして得られた触媒ａを予め雰囲気温度６００℃にて２時間焼成した。その後、ニッケルオクチル酸塩およびバナジウムオクチル酸塩をそれぞれ金属換算で１０００ｐｐｍ（ニッケルの質量を触媒の質量で除算している）および２０００ｐｐｍ（バナジウムの質量を触媒の質量で除算している）の量で、焼成した触媒粒子に沈着させた。次いで、触媒ａを雰囲気温度１１０℃で乾燥した後、雰囲気温度６００℃で１．５時間焼成し、その後、触媒ａに雰囲気温度７８０℃で１３時間のスチーム処理を施し、触媒ａの擬平衡化処理品を得た。
c. Pseudo-equilibrium step The catalyst a obtained as described above was calcined in advance at an atmospheric temperature of 600 ° C. for 2 hours. Then, nickel octylate and vanadium octylate are added in metal equivalents of 1000 ppm (mass of nickel divided by mass of catalyst) and 2000 ppm (mass of vanadium divided by mass of catalyst), respectively. , Deposited on the calcined catalyst particles. Next, the catalyst a is dried at an atmospheric temperature of 110 ° C., then fired at an atmospheric temperature of 600 ° C. for 1.5 hours, and then the catalyst a is steamed at an atmospheric temperature of 780 ° C. for 13 hours to quasi-equilibrium the catalyst a. Obtained a processed product.
ｄ．細孔径－細孔容積分布の測定
擬平衡化を施した触媒ａについて、前述の水銀圧入法による細孔径－細孔容積分布測定を行った。擬平衡化を施した触媒ａは測定前に空気雰囲気下、６００℃で１時間焼成した。全細孔容積は０．３１ｍｌ／ｇであり、細孔径が４ｎｍ以上５０ｎｍ以下の範囲のメソ細孔容積（ＰＶ１）の、細孔径が５０ｎｍより大きい範囲のマクロ細孔容積（ＰＶ２）に対する割合はＰＶ１／ＰＶ２＝１．１４であった。また、細孔径が４ｎｍより大きい範囲の細孔容積（ＰＶ３）に対する、細孔径が５０ｎｍ以上１００ｎｍ以下の範囲の細孔容積（ＰＶ４）割合は、ＰＶ４／ＰＶ３＝０．２５であった。擬平衡化を施した触媒ａの細孔径［ｎｍ］に対するログ微分細孔容積ｄＶ／ｄｌｏｇｄの分布を図１に示す。
d. Measurement of Pore Diameter-Pore Volume Distribution For the quasi-equilibrium catalyst a, the pore size-pore volume distribution was measured by the above-mentioned mercury intrusion method. The quasi-equilibriumized catalyst a was calcined at 600 ° C. for 1 hour in an air atmosphere before the measurement. The total pore volume is 0.31 ml / g, and the ratio of the mesopore volume (PV1) having a pore diameter of 4 nm or more and 50 nm or less to the macropore volume (PV2) having a pore diameter larger than 50 nm is PV1 / PV2 = 1.14. The ratio of the pore volume (PV4) in the range of 50 nm or more and 100 nm or less to the pore volume (PV3) in the range of the pore diameter larger than 4 nm was PV4 / PV3 = 0.25. FIG. 1 shows the distribution of the log differential pore volume dV / dlogd with respect to the pore diameter [nm] of the quasi-equilibrium-applied catalyst a.
ｅ．比表面積
擬平衡化した触媒ａについて、前述の比表面積測定を行ったところ１６０ｍ２／ｇであった。マトリックス成分の表面積は８７ｍ２／ｇであり、計算されるゼオライト成分の比表面積は７３ｍ２／ｇであった。
e. Specific surface area The pseudo-equilibrium catalyst a was found to be 160 m 2 / g when the above-mentioned specific surface area measurement was performed. The surface area of the matrix component was 87 m 2 / g, and the calculated specific surface area of the zeolite component was 73 m 2 / g.
ｆ．Ｌ酸量、Ｂ酸量［測定は擬平衡化した触媒でしょうか、それとも擬平衡化しない触媒でしょうか］
触媒ａについて、前述のピリジンを用いる in situ ＦＴＩＲ法によりＬ酸量およびＢ酸量割合を求めた。Ｌ酸量が４９μｍｏｌ／ｇ、Ｂ酸量／Ｌ酸量が０．３２であった。
f. Amount of L acid, amount of B acid [Is the measurement a quasi-equilibrium catalyst or a non-quasi-equilibrium catalyst?]
For the catalyst a, the amount of L acid and the ratio of the amount of B acid were determined by the above-mentioned in situ FTIR method using pyridine. The amount of L acid was 49 μmol / g, and the amount of B acid / L acid was 0.32.
＜触媒ｂ＞
ａ．調合工程
２３．５質量％の塩基性塩化アルミニウム水溶液５３１．９ｇと純水１１３８．０ｇを混合した。次いで、この混合溶液をよく攪拌しながら、カオリン（固形分濃度：８４％質量）４５２．４ｇ、活性アルミナ粉末（固形分濃度：８１％質量）２４６．９ｇおよび超安定化Ｙ型ゼオライト粉末（固形分濃度：７５質量％）３３３．３ｇを順次添加した。その後、塩化ランタン溶液（Ｌａ２Ｏ３濃度：２９．１質量％）を１５４．６ｇ添加し、よく撹拌し、調合スラリーを得た。得られた調合スラリーは、ホモジナイザーを用いて分散処理した結果、固形分濃度は３５質量％、ｐＨは３．８であった。
<Catalyst b>
a. Preparation Step 531.9 g of a 23.5 mass% basic aluminum chloride aqueous solution and 1138.0 g of pure water were mixed. Then, while stirring this mixed solution well, kaolin (solid content concentration: 84% mass) 452.4 g, activated alumina powder (solid content concentration: 81% mass) 246.9 g and ultra-stabilized Y-type zeolite powder (solid). Mineral concentration: 75% by mass) 333.3 g was sequentially added. Then, 154.6 g of a lanthanum chloride solution (La 2 O 3 concentration: 29.1% by mass) was added and stirred well to obtain a prepared slurry. As a result of dispersion treatment using a homogenizer, the obtained prepared slurry had a solid content concentration of 35% by mass and a pH of 3.8.
ｂ．噴霧乾燥、焼成、洗浄、乾燥工程
前記のようにして得られた調合スラリーを液滴として、入口温度が２３０℃、出口温度が１３０℃の噴霧乾燥機で噴霧乾燥を行い、平均粒子径が７０μｍの球状粒子を得た。この乾燥粉末は電気炉にて空気雰囲気下、４００℃で1時間焼成した後、焼成品に対して質量にて１０倍量の温水（６０℃）に懸濁させ、脱水濾過を施した。さらに、質量で１０倍量の温水（６０℃）を掛水した後、ケーキを回収し、雰囲気温度１４０℃に保持した乾燥機にて１０時間乾燥させて、触媒ｂを得た。
b. Spray drying, baking, washing, and drying steps Using the prepared slurry obtained as described above as droplets, spray drying is performed with a spray dryer having an inlet temperature of 230 ° C and an outlet temperature of 130 ° C, and the average particle size is 70 μm. Spherical particles were obtained. This dry powder was fired in an electric furnace in an air atmosphere at 400 ° C. for 1 hour, then suspended in warm water (60 ° C.) 10 times by mass with respect to the fired product, and dehydrated and filtered. Further, after sprinkling 10 times the amount of warm water (60 ° C.) by mass, the cake was recovered and dried in a dryer maintained at an atmospheric temperature of 140 ° C. for 10 hours to obtain a catalyst b.
ｃ．擬平衡化工程
得られた触媒ｂは、触媒ａと同様の条件で擬平衡化処理を施した。
c. Pseudo-equilibrium step The obtained catalyst b was subjected to a pseudo-equilibrium treatment under the same conditions as that of the catalyst a.
ｄ．細孔径－細孔容積分布の測定
擬平衡化を施した触媒ｂについて、触媒ａと同様に、前述の水銀圧入法による細孔径－細孔容積分布測定を行った。全細孔容積は０．３９ｍｌ／ｇであり、細孔径が４ｎｍ以上５０ｎｍ以下の範囲のメソ細孔容積（ＰＶ１）の、細孔径が５０ｎｍより大きい範囲のマクロ細孔容積（ＰＶ２）に対する割合はＰＶ１／ＰＶ２＝１．５３であった。また、細孔径が４ｎｍより大きい範囲の細孔容積（ＰＶ３）に対する、細孔径が３０ｎｍ以上１００ｎｍ以下の範囲の細孔容積（ＰＶ４）割合は、ＰＶ４／ＰＶ３＝０．１１であった。擬平衡化を施した触媒ｂの細孔径［ｎｍ］に対するログ微分細孔容積ｄＶ／ｄｌｏｇｄの分布を図１に示す。
d. Measurement of Pore Diameter-Pore Volume Distribution For the quasi-equilibrium catalyst b, the pore size-pore volume distribution was measured by the above-mentioned mercury intrusion method in the same manner as in the catalyst a. The total pore volume is 0.39 ml / g, and the ratio of the mesopore volume (PV1) having a pore diameter of 4 nm or more and 50 nm or less to the macropore volume (PV2) having a pore diameter larger than 50 nm is PV1 / PV2 = 1.53. The ratio of the pore volume (PV4) in the range of 30 nm or more and 100 nm or less to the pore volume (PV3) in the range of the pore diameter larger than 4 nm was PV4 / PV3 = 0.11. FIG. 1 shows the distribution of the log differential pore volume dV / dlogd with respect to the pore diameter [nm] of the quasi-equilibrium-applied catalyst b.
ｅ．比表面積
擬平衡化した触媒ｂについて、前述の比表面積測定を行ったところ１６６ｍ２／ｇであった。マトリックス成分の表面積は９０ｍ２／ｇであり、計算されるゼオライト成分の比表面積は７６ｍ２／ｇであった。
e. Specific surface area The pseudo-equilibrium catalyst b was found to be 166 m 2 / g when the above-mentioned specific surface area measurement was performed. The surface area of the matrix component was 90 m 2 / g, and the calculated specific surface area of the zeolite component was 76 m 2 / g.
ｆ．Ｌ酸量、Ｂ酸量
触媒ｂについて、前述のピリジンを用いる in situ ＦＴＩＲ法によりＬ酸量およびＢ酸量割合を求めた。Ｌ酸量が４８μｍｏｌ／ｇ、Ｂ酸量／Ｌ酸量が０．２９であった。
f. Amount of L acid and amount of B acid For the catalyst b, the amount of L acid and the ratio of the amount of B acid were determined by the above-mentioned in situ FTIR method using pyridine. The amount of L acid was 48 μmol / g, and the amount of B acid / L acid was 0.29.
（比較例）
＜触媒ｃ＞
ａ．調合工程
水ガラス（ＳｉＯ２濃度：１７質量％）２９４１ｇと硫酸（硫酸濃度：２５質量％）１０５９ｇを同時に連続的に加えて、ＳｉＯ２濃度が１２．５質量％のシリカゾル（シリカ系バインダーの一例）４０００ｇを調整した。このシリカゾルにカオリン（固形分濃度：８４％質量）８９３ｇ、活性アルミナ粉末（固形分：８１％質量）５５６ｇを加え、さらに、硫酸にてｐＨを３．９に調整した超安定化Ｙ型ゼオライトスラリー（固形分濃度：３３％質量）を２４２４ｇ加えて混合スラリーを調整した。
(Comparative example)
<Catalyst c>
a. Mixing process An example of a silica sol (silica binder) having a SiO 2 concentration of 12.5% by mass by continuously adding 2941 g of water glass (SiO 2 concentration: 17% by mass) and 1059 g of sulfuric acid (sulfuric acid concentration: 25% by mass) at the same time. ) 4000 g was adjusted. 893 g of kaolin (solid content concentration: 84% mass) and 556 g of activated alumina powder (solid content: 81% mass) were added to this silica sol, and the pH was adjusted to 3.9 with sulfuric acid. (Solid content concentration: 33% mass) was added in an amount of 2424 g to prepare a mixed slurry.
ｂ．噴霧乾燥、洗浄、乾燥工程
前記混合スラリーを液滴として、入口温度が２３０℃、出口温度が１３０℃の噴霧乾燥機で噴霧乾燥し、平均粒径が７０μｍの球状粒子を得た。得られた噴霧乾燥粒子を質量で１０倍量の温水（６０℃）に懸濁し、脱水濾過した。次いで、質量で１０倍量の温水（６０℃）を掛水した後、さらに懸濁し、希土類金属（ＲＥ）塩化物の水溶液（セリウムおよびランタンの塩化物を含む）と接触させて、ＲＥ２Ｏ３として２．１質量％となるようにイオン交換処理した。その後、触媒粒子を雰囲気１３５℃の乾燥機で乾燥して、触媒ｃを得た。
b. Spray drying, washing, and drying steps The mixed slurry was spray-dried with a spray dryer having an inlet temperature of 230 ° C. and an outlet temperature of 130 ° C. to obtain spherical particles having an average particle size of 70 μm. The obtained spray-dried particles were suspended in 10 times the mass of warm water (60 ° C.) and dehydrated and filtered. Then, after sprinkling 10 times the amount of warm water (60 ° C.) by mass, it is further suspended and contacted with an aqueous solution of rare earth metal (RE) chloride (including cerium and lanthanum chloride) to RE 2 O. Ion exchange treatment was performed so that the value of 3 was 2.1% by mass. Then, the catalyst particles were dried in a dryer having an atmosphere of 135 ° C. to obtain a catalyst c.
ｃ．擬平衡化工程
得られた触媒ｃは、触媒ａと同様の条件で擬平衡化処理を施した。
c. Pseudo-equilibrium step The obtained catalyst c was subjected to a pseudo-equilibrium treatment under the same conditions as that of the catalyst a.
ｄ．細孔径－細孔容積分布の測定
擬平衡化を施した触媒ｃについて、触媒ａと同様に、前述の水銀圧入法による細孔径－細孔容積分布測定を行った。全細孔容積は０．２８ｍｌ／ｇであった。細孔径が４ｎｍ以上５０ｎｍ以下の範囲のメソ細孔容積（ＰＶ１）の、細孔径が５０ｎｍより大きい範囲のマクロ細孔容積（ＰＶ２）に対する割合はＰＶ１／ＰＶ２＝０．５６であった。擬平衡化を施した触媒ｃの細孔径［ｎｍ］に対するログ微分細孔容積ｄＶ／ｄｌｏｇｄの分布を図１に示す。
d. Measurement of Pore Diameter-Pore Volume Distribution For the quasi-equilibrium catalyst c, the pore size-pore volume distribution was measured by the above-mentioned mercury intrusion method in the same manner as in the catalyst a. The total pore volume was 0.28 ml / g. The ratio of the mesopore volume (PV1) in the range of pore diameter of 4 nm or more and 50 nm or less to the macropore volume (PV2) in the range of pore diameter larger than 50 nm was PV1 / PV2 = 0.56. FIG. 1 shows the distribution of the log differential pore volume dV / dlogd with respect to the pore diameter [nm] of the quasi-equilibrium-applied catalyst c.
ｅ．比表面積
擬平衡化した触媒ｃについて、前述の比表面積測定を行ったところ１６９ｍ２／ｇであった。また、マトリックス成分の表面積は４８ｍ２／ｇであり、ゼオライト成分の比表面積は１２１ｍ２／ｇであった。
e. Specific surface area The pseudo-equilibrium catalyst c was found to be 169 m 2 / g when the above-mentioned specific surface area measurement was performed. The surface area of the matrix component was 48 m 2 / g, and the specific surface area of the zeolite component was 121 m 2 / g.
ｆ．Ｌ酸量、Ｂ酸量
触媒ｃについて、前述のピリジンを用いる in situ ＦＴＩＲ法によりＬ酸量およびＢ酸量割合を求めた。Ｌ酸量が２２μｍｏｌ／ｇ、Ｂ酸量／Ｌ酸量が０．４５であった。
f. Amount of L acid and amount of B acid With respect to the catalyst c, the amount of L acid and the ratio of the amount of B acid were determined by the above-mentioned in situ FTIR method using pyridine. The amount of L acid was 22 μmol / g, and the amount of B acid / L acid was 0.45.
［触媒活性評価試験］
＜性能評価試験＞
前記した実施例、比較例に係る各触媒について、ＡＣＥ－ＭＡＴ（Advanced Cracking Evaluation-Micro Activity Test）を用い、同一原油、同一反応条件下で触媒の性能評価試験を行った。ただし、評価にあたって、すべて、前記の擬平衡化処理を施したものを用いた。
性能評価試験における運転条件は以下の通りである。
反応温度：５２０℃
再生温度：７００℃
原料油：脱硫常圧残渣油（ＤＳＡＲ）５０％：水素化脱硫減圧蒸留軽油（ＤＳＶＧＯ）５０％
触媒／油比：３．７５，５．０
但し、
・転化率（質量％）＝（Ａ－Ｂ）／Ａ×１００
Ａ：原料油の重量
Ｂ：生成油中の２１６℃以上の留分の重量
・水素（質量％）＝Ｃ／Ａ×１００
Ｃ：生成ガス中の水素の重量
・Ｃ１＋Ｃ２（質量％）＝Ｄ／Ａ×１００
Ｄ：生成ガス中のＣ１（メタン）、Ｃ２（エタン、エチレン）の重量
・ＬＰＧ（液化石油ガス、質量％）＝Ｅ／Ａ×１００
Ｅ：生成ガス中のプロパン、プロピレン、ブタン、ブチレンの重量
・ガソリン（質量％）＝Ｆ／Ａ×１００
Ｆ：生成油中のガソリン（沸点範囲：Ｃ５～２１６℃）の重量
・ＬＣＯ（質量％）＝Ｇ／Ａ×１００
Ｇ：生成油中のライトサイクルオイル（沸点範囲：２１６～３４３℃）の重量
・ＨＣＯ（質量％）＝Ｈ／Ａ×１００
Ｈ：生成油中のヘビーサイクルオイル（沸点範囲：３４３℃以上）の重量
・コーク（質量％）＝Ｉ／Ａ×１００
Ｉ：触媒上に析出したコーク重量
[Catalytic activity evaluation test]
<Performance evaluation test>
Each catalyst according to the above-mentioned Examples and Comparative Examples was subjected to a catalyst performance evaluation test under the same crude oil and the same reaction conditions using ACE-MAT (Advanced Cracking Evaluation-Micro Activity Test). However, in all the evaluations, those subjected to the above-mentioned pseudo-equilibrium treatment were used.
The operating conditions in the performance evaluation test are as follows.
Reaction temperature: 520 ° C
Regeneration temperature: 700 ° C
Raw material oil: Desulfurization normal pressure residual oil (DSAR) 50%: Hydrodesulfurization vacuum distillation light oil (DSVGO) 50%
Catalyst / oil ratio: 3.75, 5.0
However,
・ Conversion rate (mass%) = (AB) / A × 100
A: Weight of raw material oil
B: Weight of fraction above 216 ° C in produced oil-Hydrogen (% by mass) = C / A x 100
C: Weight of hydrogen in the produced gas ・ C1 + C2 (mass%) = D / A × 100
D: Weight of C1 (methane) and C2 (ethane, ethylene) in the produced gas ・ LPG (liquefied petroleum gas, mass%) = E / A × 100
E: Weight of propane, propylene, butane, and butylene in the produced gas ・ Gasoline (mass%) = F / A × 100
F: Weight of gasoline (boiling point range: C5 to 216 ° C.) in produced oil ・ LCO (mass%) = G / A × 100
G: Weight of light cycle oil (boiling point range: 216 to 343 ° C.) in produced oil ・ HCO (mass%) = H / A × 100
H: Weight of heavy cycle oil (boiling point range: 343 ° C or higher) in the produced oil ・ Cork (mass%) = I / A × 100
I: Weight of cork deposited on the catalyst
上記で調整した本発明触媒ａおよびｂならびに比較触媒ｃについて、触媒活性評価試験の結果を表１に示す。 Table 1 shows the results of the catalytic activity evaluation test for the catalysts a and b of the present invention and the comparative catalyst c prepared above.
触媒ａは、重質油の分解性能が同等の触媒ｂと比較し、ガソリン収率およびＬＣＯ収率がやや優れていることがわかる。 It can be seen that the catalyst a is slightly superior in gasoline yield and LCO yield as compared with the catalyst b having the same decomposition performance of heavy oil.
以上説明したように、本発明によれば、軽質液体油であるガソリンの収率やＬＣＯの収率を高く維持しつつ、特に重質留分を低減することができる。
As described above, according to the present invention, it is possible to maintain high yields of gasoline, which is a light liquid oil, and yields of LCO, and in particular, reduce heavy fractions.
Claims (7)
（ａ）擬平衡化を施した後の細孔分布において、細孔径が４ｎｍ以上５０ｎｍ以下である細孔容積（ＰＶ１）の、細孔径が５０ｎｍより大きい細孔容積（ＰＶ２）に対する割合（ＰＶ１／ＰＶ２）が０．８以上１．５以下であり、かつ
（ｂ）ルイス酸量（Ｌ酸量）が３５μｍｏｌ／ｇ以上であって、そのルイス酸量とブレンステッド酸量（Ｂ酸量）との割合（Ｂ酸量／Ｌ酸量）が０．２以上であることを特徴とする炭化水素油用流動接触分解触媒。 A fluid catalytic cracking catalyst for hydrocarbon oils containing zeolite and an alumina binder.
(A) In the pore distribution after quasi-equilibrium, the ratio of the pore volume (PV1) having a pore diameter of 4 nm or more and 50 nm or less to the pore volume (PV2) having a pore diameter larger than 50 nm (PV1 /). PV2) is 0.8 or more and 1.5 or less, and (b) Lewis acid amount (L acid amount) is 35 μmol / g or more, and the Lewis acid amount and Bronsted acid amount (B acid amount) A fluid catalytic decomposition catalyst for hydrocarbon oil, wherein the ratio (Amount of B acid / amount of L acid) is 0.2 or more.
（ａ）塩基性塩化アルミニウム。
（ｂ）重リン酸アルミニウム。
（ｃ）アルミナゾル。 The flow catalytic cracking catalyst for a hydrocarbon oil according to claim 3, wherein the alumina binder contains at least one selected from the following (a) to (c).
(A) Basic aluminum chloride.
(B) Heavy aluminum phosphate.
(C) Alumina sol.
The fluid catalytic cracking catalyst for hydrocarbon oil according to any one of claims 1 to 6, wherein the catalyst contains a clay mineral.
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