# US 10,501,695 B2 · Process for the intense conversion of residues, maximizing the gas oil yield

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- Number: US 10,501,695 B2
- Document ID: US10501695B2
- Status: Granted
- Kind: B2
- Application number: 14/974,313
- Filed: 2015-12-18
- Published: 2016-06-23
- Granted: 2019-12-10
- Earliest claimed: 2014-12-18
- Assignees: Axens
- Applicants: Axens
- Inventors: Frederic Morel; Jacinthe Frecon
- Web page: https://patentgrep.com/patent/US10501695B2

## CPC

- C10G 67/049: {The hydrotreatment being a hydrocracking}
- C10G 65/10: including only cracking steps
- C10G 65/12: including cracking steps and other hydrotreatment steps
- C10G 67/00: Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- 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

The invention concerns a process for the intense conversion of a heavy hydrocarbon feed, comprising the following steps: a) a first step for ebullated bed hydroconversion; b) a step for separating at least a portion of the hydroconverted liquid effluent obtained from step a); c) a step for hydrocracking at least a portion of the vacuum gas oil fraction obtained from step b); d) a step for fractionating at least a portion of the effluent obtained from step c); e) a step for recycling at least a portion of the unconverted vacuum gas oil fraction obtained from step d) to said first hydroconversion step a).

## Claims

### Claim 1

A process for the intense conversion of a heavy hydrocarbon feed, comprising the following steps:
a) a first step for ebullated bed hydroconversion of the feed in the presence of hydrogen, comprising at least one three-phase reactor containing at least one ebullated bed hydroconversion catalyst;
b) a step for separating at least a portion of a hydroconverted liquid effluent obtained from step a) into a fraction comprising a gasoline cut and a gas oil cut, a vacuum gas oil fraction and an unconverted residual fraction;
c) a step for hydrocracking at least a portion of the vacuum gas oil fraction obtained from step b) in a reactor comprising at least one fixed bed hydrocracking catalyst;
d) a step for fractionating at least a portion of an effluent obtained from step c) into a gasoline fraction, a gas oil fraction and an unconverted vacuum gas oil fraction;
e) a step for recycling at least a portion of the unconverted vacuum gas oil fraction obtained from step d) to said first hydroconversion step a)
wherein at least a portion of the unconverted residual fraction obtained from step b) is sent to a deasphalting section where it is treated in an extraction step using a solvent under conditions for obtaining a deasphalted hydrocarbon cut and pitch;
wherein said deasphalted hydrocarbon cut is sent to a second hydroconversion step in the presence of hydrogen and at least one ebullated bed hydroconversion catalyst,
wherein the effluent obtained from the second hydroconversion step undergoes a separation step f) in order to produce at least one fraction comprising a gasoline cut and a gas oil cut, a vacuum gas oil fraction and a unconverted residual fraction, and
wherein the vacuum gas oil fraction obtained from the separation step f) is sent to the hydrocracking step c) as a mixture with the vacuum gas oil fraction obtained from step b) and optionally with a straight run vacuum gas oil fraction.

### Claim 2 (depends on 1)

The process according to claim 1, in which at least a portion of the deasphalted hydrocarbon cut is sent to the hydrocracking step c) as a mixture with the vacuum gas oil fraction separated in step b) and optionally with a straight run vacuum gas oil fraction.

### Claim 3 (depends on 1)

The process according to claim 1, in which at least a portion of the vacuum gas oil fraction obtained from the fractionation step d) is recycled to an inlet of the deasphalting section.

### Claim 4 (depends on 1)

The process according to claim 1, in which the hydroconversion step a) is operated under an absolute pressure in the range 5 to 35 MPa, at a temperature of 260° C. to 600° C. and at an hourly space velocity of 0.05 h−1 to 10 h−1.

### Claim 5 (depends on 1)

The process according to claim 1, in which the hydrocracking step c) is operated at an average bed temperature of the catalytic bed in the range 300° C. to 550° C., a pressure in the range 5 to 35 MPa and a liquid hourly space velocity in the range 0.1 to 10h−1.

### Claim 6 (depends on 1)

The process according to claim 1, in which in the deasphalting section, the typical temperature at the head of an extractor is in the range 60° C. to 220° C. and the temperature at the bottom of the extractor is in the range 50° C. to 190° C.

### Claim 7 (depends on 1)

The process according to claim 1, in which the feed is selected from heavy hydrocarbon feeds of the atmospheric residue or vacuum residue type distillate type feeds, asphalts obtained from oil residue solvent deasphalting, coal in suspension in a hydrocarbon fraction.

### Claim 8 (depends on 7)

The process according to claim 7, wherein the vacuum residue type is obtained by straight run oil cut distillation or by vacuum distillation of crude oil, the distillate type feeds are vacuum gas oils or deasphalted oils and the hydrocarbon fraction is gas oil obtained by vacuum distillation of crude oil or a distillate obtained from the liquefaction of coal used alone or as a mixture.