# US 10,864,504 B2 · Hydrocracking catalyst

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- Number: US 10,864,504 B2
- Document ID: US10864504B2
- Status: Granted
- Kind: B2
- Application number: 16/796,223
- Filed: 2020-02-20
- Published: 2020-06-18
- Granted: 2020-12-15
- Earliest claimed: 2009-04-29
- Assignees: Shell Oil Company
- Applicants: Shell Oil Company
- Inventors: László Domokos; Cornelis Ouwehand
- Web page: https://patentgrep.com/patent/US10864504B2

## CPC

- B01J 29/166: {Y-type faujasite}
- B01J 29/084: {Y-type faujasite}
- B01J 29/106: {Y-type faujasite}
- B01J 29/146: {Y-type faujasite}
- B01J 29/80: Mixtures of different zeolites
- B01J 35/647: {2-50 nm}
- B01J 37/0009: {Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst}
- B01J 37/0201: {Impregnation}
- B01J 37/20: Sulfiding
- C10G 47/16: Crystalline alumino-silicate carriers
- C10G 47/18: the catalyst containing platinum group metals or compounds thereof
- C10G 47/20: the catalyst containing other metals or compounds thereof
- B01J 29/7007: {Zeolite Beta}
- B01J 29/7815: {Zeolite Beta}
- B01J 35/633: {less than 0.5 ml/g}
- B01J 35/67: monomodal
- B01J 2229/16: to increase the Si/Al ratio; Dealumination
- B01J 2229/18: to introduce other elements into or onto the molecular sieve itself
- B01J 2229/186: not in framework positions
- B01J 2229/20: to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
- B01J 2229/40: Special temperature treatment, i.e. other than just for template removal
- B01J 2229/42: Addition of matrix or binder particles
- C10G 2300/301: Boiling range
- C10G 2300/70: Catalyst aspects
- C10G 2400/06: Gasoil
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES

## Abstract

Process for preparing a hydrocracking catalyst carrier which process comprises subjecting a carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10 to calcination at a temperature of from 700 to 900° C., hydrocracking catalyst carrier comprising amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, the infrared spectrum of which catalyst has a peak at 3690 cm−1, substantially reduced peaks at 3630 cm−1 and 3565 cm−1 and no peak at 3600 cm−1, hydrocracking catalyst carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, which catalyst has an acidity as measured by exchange with perdeuterated benzene of at most 20 micromole/gram, hydrocracking catalyst derived from such carrier and hydrocracking process with the help of such catalyst.

## Claims

### Claim 1

A hydrocracking process for converting a hydrocarbon feedstock into lower boiling materials, wherein said process comprises:
contacting said hydrocarbon feedstock and hydrogen at an elevated temperature in the range of from 250 to 500° C. and an elevated pressure in the range of from 3×106 to 3×107 Pa with a hydrocracking catalyst within a hydrocracking reaction vessel having a reactor inlet and a reactor outlet, wherein said hydrocracking catalyst comprises, a Group VIII metal; a Group VIB metal; and a carrier, wherein said carrier comprises an amorphous binder in an amount in the range of from 30% wt to 98% wt based on the total weight of said carrier, a zeolite Y, having a silica-to-alumina molar ratio of at least 10, in an amount in the range of from 2% to 70% wt based on the total weight of said carrier, and a second zeolite component that is either zeolite beta or ZSM-5 in an amount up to 20% wt based on the total weight of said carrier, and wherein the infrared spectrum of said carrier has peaks at 3690 cm−1, 3630 cm−1, and 3565 cm−1, and no peak at 3600 cm−1.

### Claim 2 (depends on 1)

A process as recited in claim 1, wherein said hydrocracking catalyst contains from 2 to 40 parts by weight of the Group VIB metal and from 0.05 to 10 parts by weight of the Group VIII metal, calculated as metal per 100 parts by weight of the hydrocracking catalyst.

### Claim 3 (depends on 1)

A process as recited in claim 1, wherein said amorphous binder is selected from the group consisting of alumina, silica, silica-alumina and mixtures thereof.

### Claim 4 (depends on 1)

A process as recited in claim 1, wherein said amorphous binder is silica-alumina containing silica in an amount in the range of from 25% to 95% by weight as calculated on the total carrier.

### Claim 5 (depends on 1)

A process as recited in claim 1, wherein said Group VIII metal is either nickel or cobalt, and said Group VIB metal is either molybdenum or tungsten.

### Claim 6 (depends on 1)

A process as recited in claim 1, wherein said hydrocracking catalyst contains from 2 to 40 parts by weight of the Group VIB metal and from 0.05 to 10 parts by weight of the Group VIII metal, calculated as metal per 100 parts by weight of the hydrocracking catalyst.

### Claim 7 (depends on 1)

A process as recited in claim 1, wherein said second zeolite component is zeolite beta present in said carrier in an amount in the range of from 0.5 to 10% wt, based on the total carrier.

### Claim 8 (depends on 1)

A process as recited in claim 1, wherein said hydrocarbon feedstock comprises hydrocarbons having a boiling point of at least 330° C.

### Claim 9 (depends on 1)

A process as recited in claim 1, wherein the hydrocarbon feedstock and hydrogen at the reactor inlet are such that there is a hydrogen partial pressure at said reactor inlet is in the range of from 3×106 to 2.9×107 Pa.

### Claim 10 (depends on 1)

A process as recited in claim 1, wherein said hydrocarbon feedstock and hydrogen are such that there is a space velocity is in the range of from 0.1 to 10 kg of said hydrocarbon feedstock per liter of said hydrocracking catalyst per hour.