# US 2022/0033723 A1 · Feed Flexible Hydrocracking Operations

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- Number: US 2022/0033723 A1
- Document ID: US20220033723A1
- Status: Published application
- Kind: A1
- Application number: 17/385,782
- Filed: 2021-07-26
- Published: 2022-02-03
- Earliest claimed: 2020-07-29
- Assignees: Chevron U.S.A. Inc.
- Applicants: Chevron U.S.A. Inc.
- Inventors: Varut KOMALARAJUN; Theodorus Ludovicus Michael MAESEN
- Web page: https://patentgrep.com/patent/US20220033723A1

## CPC

- C10G 67/02: plural serial stages only
- B01D 3/14: Fractional distillation {or use of a fractionation or rectification column}
- B01J 23/002: {Mixed oxides other than spinels, e.g. perovskite}
- B01J 23/8885: {containing also molybdenum}
- B01J 27/0515: {with iron group metals or platinum group metals}
- B01J 35/615: {100-500 m2/g}
- B01J 35/633: {less than 0.5 ml/g}
- B01J 35/647: {2-50 nm}
- B01J 37/0236: {Drying, e.g. preparing a suspension, adding a soluble salt and drying}
- B01J 37/033: {Using Hydrolysis}
- B01J 37/20: Sulfiding
- C10G 45/04: characterised by the catalyst used
- C10G 47/00: Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06)
- C10G 65/12: including cracking steps and other hydrotreatment steps
- B01J 2523/00: Constitutive chemical elements of heterogeneous catalysts
- C10G 2300/1074: Vacuum distillates
- C10G 2300/202: Heteroatoms content, i.e. S, N, O, P
- C10G 2300/4018: Spatial velocity, e.g. LHSV, WHSV
- C10G 2300/70: Catalyst aspects
- C10G 2400/04: Diesel oil
- C10G 2400/08: Jet fuel
- 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
- B01D: SEPARATION (separating solids from solids by wet methods B03B, B03D; by pneumatic jigs or tables B03B; by other dry methods B07; magnetic or electrostatic separation of solid materials from solid materials or fluids, separation by high-voltage electric fields B03C; centrifuges, vortex apparatus B04; presses per se for squeezing-out liquid from liquid-containing material B30B9/02; treatment of water C02F, e.g. softening by ion-exchange C02F1/42; {arrangements of air intake cleaners in gas turbine plants F02C7/05} ; arrangements or mounting of filters in air-conditioning, air-humidification or ventilation F24F13/28)
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

## Abstract

A hydrocracking process for converting a petroleum feed to lower boiling products. The process comprises hydrotreating a petroleum feed in a pre-treating zone in the presence of hydrogen to produce a hydrotreated effluent stream comprising a liquid product. At least a portion of the hydrotreated effluent stream is then passed to an MMS catalyst zone, and then to a hydrocracking zone. In one embodiment, the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form. The percentage work of the hydrotreating in the pre-treating zone is maintained at a level of at least 56%.

## Claims

### Claim 1

A hydrocracking process for converting a petroleum feed to lower boiling products,
which process comprises:
(i) hydrotreating a petroleum feed in the presence of hydrogen in a pre-treating zone to produce a hydrotreated effluent stream comprising a liquid product;
(ii) passing the hydrotreated effluent stream to an MMS catalyst zone comprising an MMS catalyst for reaction to create a resulting effluent; and
(iii) passing at least a portion of the resulting effluent from (ii) to a hydrocracking zone having a reaction zone to produce a hydrocracked effluent stream;
with a work percentage for the pre-treating zone (i) maintained at a level of at least 56%.

### Claim 2 (depends on 1)

The process of claim 1, wherein the MMS catalyst in the MMS catalyst zone in (ii) comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form.

### Claim 3 (depends on 2)

The process of claim 2, wherein the MMS catalyst in the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the hydroxide form.

### Claim 4 (depends on 2)

The process of claim 2, wherein the hydrocracked effluent is passed to a distillation column.

### Claim 5 (depends on 2)

The process of claim 2, wherein the hydrocracking zone comprises up to three reaction zones.

### Claim 6 (depends on 5)

The process of claim 5, wherein effluent from a bottom reaction zone is passed to a distillation column.

### Claim 7 (depends on 2)

The process of claim 2, wherein the hydrocracking zone comprises at least one reaction zone which is a hydrodesulfurization zone.

### Claim 8 (depends on 6)

The process of claim 6, wherein the bottom reaction zone is a hydrodesulfurization zone.

### Claim 9 (depends on 8)

The process of claim 8, wherein the hydrodesulfurization zone comprises a bulk multimetallic catalyst comprised of one Group VIII noble metal and two Group VI B metals.

### Claim 10 (depends on 4)

The process of claim 4, wherein a portion of bottoms from the distillation column is passed to an FCC unit.

### Claim 11 (depends on 4)

The process of claim 4, wherein cuts of light naphtha, heavy naphtha, kerosene and diesel are recovered from the distillation column.

### Claim 12 (depends on 3)

The process of claim 3, wherein the self-supported multi-metallic catalyst is prepared by sulfiding a precursor catalyst in the hydroxide form of the general formula: Av[(MP)(OH)x(L)ny]z(MVIBO4), wherein:
A is one monovalent cationic species;
MP is a promoter metal with an oxidation state of +2 or +4 selected from one or more of Group IIA, Group IIB, Group IVA, and Group VIII metals;
L is an organic oxygen-containing ligand; and
MVIB is Group VIB metal.

### Claim 13 (depends on 12)

The process of claim 12, wherein the catalyst precursor MP:MVIB has an atomic ratio between 100:1 and 1:100.

### Claim 14 (depends on 12)

The process of claim 12, wherein MP is nickel (Ni), MVIB is selected from molybdenum (Mo), tungsten (W) or a combination thereof.

### Claim 15 (depends on 14)

The process of claim 14, wherein the catalyst precursor comprises Ni—Mo—W.

### Claim 16 (depends on 15)

The process of claim 15, wherein Ni:(Mo+W) has a molar ratio of 10:1 to 1:10.

### Claim 17 (depends on 12)

The process of claim 12, wherein L is a maleate ligand.

### Claim 18 (depends on 2)

The process of claim 2, wherein the pre-treating zone, MMS catalyst zone and the hydrocracking zone are in the same reactor.

### Claim 19 (depends on 1)

The process of claim 1, wherein the pre-treating zone is in a first reactor and the MMS catalyst zone and the hydrocracking zone are in a second reactor.

### Claim 20 (depends on 19)

The process of claim 19, wherein the MMS catalyst zone is in the top half of the second reactor and comprises a catalyst prepared from a precursor in the hydroxide form.

### Claim 21 (depends on 1)

The process of claim 1, wherein the pre-treating zone in (i) comprises a plurality of hydrotreating reaction beds prior to the MMS catalyst zone and the hydrocracking zone.