Fluid catalytic cracking catalyst for hydrocarbon oil

Patent metadata

Field	Value
Publication number	US-11731114-B2
Application number	US-201917267976-A
Country	US
Kind code	B2
Filing date	Jul 22, 2019
Priority date	Aug 29, 2018
Publication date	Aug 22, 2023
Grant date	Aug 22, 2023

Abstract

A fluid catalytic cracking catalyst for hydrocarbon oil that is a blend of two types of fluid catalytic cracking catalysts each of which has a different hydrogen transfer reaction activity or has a pore distribution within a specific range after being pseudo-equilibrated. One catalyst is a catalyst containing a zeolite and matrix components, and the other catalyst is a catalyst containing a zeolite and matrix components. This catalyst is composed of the one catalyst and the other catalyst blended at a mass ratio within a range of 10:90 to 90:10.

First claim

The invention claimed is:

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 RE 2 O 3 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 RE 2 O 3 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.

2. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 1 , wherein in the blend (I), the hydrogen transfer reaction activity of each catalyst is determined by a ratio of i-C4 over C4= in a test, where i-C4 and C4= represent masses of isobutane and butene respectively deposited on each of the first catalyst component and the second catalyst component, and
wherein a difference between the ratio of the first catalyst component and the second catalyst component is within a range of 0.10 to 0.85,
wherein the test is performed using advanced cracking evaluation-micro activity test (ACE-MAT) under the following conditions:
(i) a reaction temperature: 520° C.,
(ii) regeneration temperature: 700° C.,
(iii) raw oil: Desulfurized atmospheric residual oil (DSAR) 50%: hydrodesulfurized vacuum gas oil (DSVGO) 50%,
(iv) catalyst/oil ratio: 7 mass %/mass %.

3. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 1 , wherein
the catalyst (1) contains 15 to 60 mass % of the faujasite-type zeolite (A) based on the catalyst (1) composition, and the catalyst (2) contains 15 to 60 mass % of the faujasite-type zeolite (B) based on the catalyst (2) composition.

4. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 1 , wherein:
the catalyst (3) contains a zeolite and a silica-based binder as a binding agent, and contains 15 to 60 mass % of the zeolite and 5 to 30 mass % of the silica-based binder based on the catalyst (3) composition; and
the catalyst (4) contains a zeolite and an aluminum compound binder as a binding agent, and contains 15 to 60 mass % of the zeolite and 5 to 30 mass % of the aluminum compound binder based on the catalyst (4) composition.

5. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 4 , wherein
the silica-based binder is one or more than one of silica sol, water glass, and an acidic silicate solution.

6. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 4 , wherein the aluminum compound binder contains one type selected from the following (a) to (c):
(a) basic aluminum chloride;
(b) aluminum biphosphate; and
(c) alumina sol.

7. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 1 , wherein the zeolites contained in the catalyst (3) and the catalyst (4) are of one or more than one of the following types: FAU (faujasite), MFI, CHA, and MOR.

8. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 7 , wherein the FAU-type zeolite is one of a hydrogen Y-type zeolite (HY), an ultra-stable Y-type zeolite (USY), a rare-earth-exchanged Y-type zeolite (REY), and a rare-earth-exchanged ultra-stable Y-type zeolite (REUSY).

9. The fluid catalytic cracking catalyst for hydrocarbon oil according to claim 4 , wherein the catalyst (3) and the catalyst (4) contain clay mineral other than the zeolite and the binding agent.

10. A fluid catalytic cracking catalyst for hydrocarbon oil comprising a blend of a catalyst component with another catalyst, the catalyst component being characterized by having, 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 catalyst component contains a zeolite and an aluminum compound binder as a binding agent; and
wherein the pore distribution is determined on a portion of the catalyst component, for testing and evaluation, by first performing pseudo-equilibration, prior to said testing and evaluation; and
wherein the pseudo-equilibration is performed by baking the catalyst component 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 component particles, respectively, such that nickel metal is present in an amount of 1000 ppm and vanadium metal in an

Assignees

• Jgc Catalysts & Chemicals Ltd

Inventors

• Mizuno Takaki
• TANAKA Chisuzu
• Mitsui Tomohiro

Classifications

• B01J35/19

  Catalysts containing parts with different compositions · CPC title

• B01J35/613

  10-100 m2/g · CPC title

• B01J35/615

  100-500 m2/g · CPC title

• B01J35/633

  less than 0.5 ml/g · CPC title

• B01J35/647

  2-50 nm · CPC title