Process for the intense conversion of residues, maximizing the gasoline yield

Patent metadata

Field	Value
Publication number	US-9745527-B2
Application number	US-201514974968-A
Country	US
Kind code	B2
Filing date	Dec 18, 2015
Priority date	Dec 18, 2014
Publication date	Aug 29, 2017
Grant date	Aug 29, 2017

Abstract

A process for the intense conversion of a heavy hydrocarbon feed, comprising a) ebullated bed hydroconversion of the feed; b) separating at least a portion of hydroconverted liquid effluent obtained from a); c)i) either hydrotreatment of at least a portion of the gas oil fraction and of the vacuum gas oil fraction obtained from b), ii) or hydrocracking at least a portion of gas oil fraction and vacuum gas oil fraction obtained from b); d) fractionation of at least a portion of the effluent obtained from c)i) or c)ii); e) recycling at least a portion of unconverted vacuum gas oil fraction obtained from the fractionation d) to said first hydroconversion a); f) hydrocracking at least a portion of gas oil fraction obtained from fractionation d); g) recycling all or a portion of effluent obtained from f) to the fractionation d).

First claim

The invention claimed is:

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 the hydroconverted liquid effluent obtained from step a) into a gasoline fraction, a gas oil fraction, a vacuum gas oil fraction and an unconverted residual fraction;
c) i) either a step for hydrotreatment of at least a portion of the gas oil fraction and the vacuum gas oil fraction obtained from step b) in a reactor comprising at least one fixed bed hydrotreatment catalyst;
ii) or a first step for hydrocracking at least a portion of the gas oil fraction and 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 the effluent obtained from step c)i) or step c)ii) 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 fractionation step d) to said first hydroconversion step a);
f) a second step for hydrocracking at least a portion of the gas oil fraction obtained from fractionation step d);
g) a step for recycling all or a portion of the effluent obtained from step f) to the fractionation step d).

2. The process according to claim 1 , in which at least a portion of the residual unconverted fraction obtained from step b) is sent to a deasphalting section in which it is treated in an extraction step using a solvent under conditions for obtaining a deasphalted hydrocarbon cut and pitch.

3. The process according to claim 2 , in which at least a portion of the deasphalted hydrocarbon cut obtained from the deasphalting step is sent to the hydrotreatment step c)i) or the hydrocracking step c)ii) as a mixture with the gas oil fraction and the vacuum gas oil fraction obtained from step b) and optionally with a straight run gas oil fraction and/or a straight run vacuum gas oil fraction.

4. The process according to claim 2 , in which at least a portion of the deasphalted hydrocarbon cut obtained from the deasphalting step is sent to a second step for hydroconversion in the presence of hydrogen, said step being carried out in fixed bed or ebullated bed mode.

5. The process according to claim 4 , in which the effluent obtained from the second hydroconversion step undergoes a separation step h) in order to produce at least a gasoline fraction, a gas oil fraction, a vacuum gas oil fraction and a residual unconverted fraction.

6. The process according to claim 5 , in which at least a portion of the gas oil and vacuum gas oil fractions obtained from the separation step h) is sent to the hydrotreatment step c)i) or the hydrocracking step c)ii) as a mixture with the gas oil fraction and the vacuum gas oil fraction obtained from step b) and optionally with a straight run gas oil fraction and/or a straight run vacuum gas oil fraction.

7. The process according to claim 2 , in which at least a portion of the vacuum gas oil fraction obtained from the fractionation step d) is recycled to the inlet of the deasphalting step and/or to the inlet of the first hydroconversion step.

8. 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 .

9. The process according to claim 1 , in which the operating conditions used in the hydrotreatment step c)i) are a pressure in the range 5 to 35 MPa, a temperature in the range 320° C. to 460° C. and a liquid hourly space velocity in the range 0.1 to 10 h −1 .

10. The process according to claim 1 , in which the operating conditions used in the first hydrocracking step c)ii) are a weighted average catalytic bed temperature 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 20 h −1 .

11. The process according to claim 1 , in which the second hydrocracking step is carried out at a temperature at least 10° C. below that employed during the hydrotreatment step c)i) or the first hydrocracking step c)ii), and at a liquid hourly space velocity (feed flow rate/volume of catalyst) which is at least 30% higher, preferably at least 45% higher, more preferably at least 60% higher than that employed during the hydrotreatment step c)i) or the first hydrocracking step c)ii).

12. The process according to claim 2 in which, in the deasphalting step, the typical temperature at the head of the 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.

13. The process according to claim 1 , in which the feed is selected from heavy hydrocarbon feeds of the atmospheric residue or vacuum residue type obtained, for example, by straight run oil cut distillation or by vacuum distillation of crude oil, distillate type feeds such as vacuum gas oils or deasphalted oils, asphalts obtained from oil residue solvent deasphalting, coal in suspension in a hydrocarbon fraction such as, for example, gas oil obtained by vacuum distillation of crude oil or a distillate obtained from the liquefaction of coal, used alone or as a mixture.

Assignees

• Axens

Inventors

• Morel Frederic
• Frecon Jacinthe

Classifications

• C10G65/10

  including only cracking steps · CPC title

• C10G65/12

  including cracking steps and other hydrotreatment steps · CPC title

• C10G67/049 Primary

  The hydrotreatment being a hydrocracking · CPC title

• C10G67/00

  Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only · CPC title

• C10G47/12

  Inorganic carriers · CPC title