| CPC B01J 29/088 (2013.01) [B01J 29/80 (2013.01); B01J 35/0006 (2013.01); B01J 35/1014 (2013.01); B01J 35/1019 (2013.01); B01J 35/1038 (2013.01); B01J 35/1061 (2013.01); B01J 37/009 (2013.01); B01J 37/0009 (2013.01); B01J 37/0045 (2013.01); B01J 37/06 (2013.01); B01J 37/08 (2013.01); B01J 37/30 (2013.01); C10G 11/05 (2013.01); C10G 11/18 (2013.01); C10G 2300/1059 (2013.01); C10G 2300/70 (2013.01); C10G 2400/02 (2013.01); C10G 2400/26 (2013.01)] | 15 Claims |
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1. A fluid catalytic cracking catalyst for hydrocarbon oil comprising a blend of two fluid catalytic cracking catalyst components each of which has a different hydrogen transfer reaction activity or has a pore distribution within a specific range, wherein these catalyst components are not pseudo-equilibrated, wherein
a first catalyst component contains a zeolite and matrix components,
a second catalyst component contains a zeolite and matrix components, and
the fluid catalytic cracking catalyst is composed of the first catalyst component and the second catalyst component blended at a mass ratio within a range of 10:90 to 90:10,
the fluid catalytic cracking catalyst being selected from one of blends I and II:
I) the first catalyst component comprises a catalyst (1) containing a faujasite-type zeolite (A) having a lattice constant within a range of 2.435 to 2.459 nm, matrix components, and 0.5 to 2.0 mass % of a rare earth as RE2O3 based on the catalyst (1) composition;
the second catalyst component comprises a catalyst (2) containing a faujasite-type zeolite (B) having a lattice constant within a range of 2.440 to 2.478 nm, matrix components, and 2.5 to 12 mass % of a rare earth as RE2O3 based on the catalyst (2) composition; and
the hydrogen transfer reaction activity of the catalyst (1) is lower than the hydrogen transfer reaction activity of the catalyst (2);
II) the first catalyst component comprises a catalyst (3) that has a pore distribution in which a ratio (PV1/PV2) of a volume (PV1) of pores having a pore size not smaller than 4 nm nor larger than 50 nm to a volume (PV2) of pores having a pore size larger than 50 nm is lower than 0.8;
the second catalyst component comprises a catalyst (4) that has a pore distribution in which: (a) a ratio (PV1/PV2) of a volume (PV1) of pores having a pore size not smaller than 4 nm nor larger than 50 nm to a volume (PV2) of pores having a pore size larger than 50 nm is not lower than 0.8; and (b) a ratio (PV4/PV3) of a volume (PV4) of pores having a pore size not smaller than 30 nm nor larger than 100 nm to a volume (PV3) of pores having a pore size larger than 4 nm is lower than 0.2;
wherein the hydrogen transfer reaction activity is determined on test portions of the catalyst (1) and the catalyst (2), for testing and evaluation, by first performing pseudo-equilibration I, prior to said testing and evaluation;
wherein the pseudo-equilibration I is performed by being held at 790° C. for 13 hours under a 100% water vapor condition;
wherein the pore distribution is determined on test portions of the catalyst (3) and the catalyst (4), for testing and evaluation, by first performing pseudo-equilibration II, prior to said testing and evaluation; and
wherein the pseudo-equilibration II is performed by baking each of the catalyst (3) and the catalyst (4) at an atmospheric temperature of 600° C. for two hours, followed by depositing nickel octyl acid salt and vanadium octyl acid salt on the baked catalyst particles, respectively, such that nickel metal is present in an amount of 1000 ppm and vanadium metal in an amount of 2000 ppm, obtained by the mass of nickel or vanadium divided by the mass of the catalyst, followed by drying the catalyst at an atmospheric temperature of 110° C. and baking at an atmospheric temperature of 600° C. for 1.5 hours, and lastly subjecting each of the catalyst (3) and the catalyst (4) to a steaming treatment for 13 hours at an atmospheric temperature of 780° C.
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