# US 10,246,652 B2 · Process for the dearomatization of petroleum cuts

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- Number: US 10,246,652 B2
- Document ID: US10246652B2
- Status: Granted
- Kind: B2
- Application number: 15/107,360
- Filed: 2014-12-15
- Published: 2016-12-22
- Granted: 2019-04-02
- Earliest claimed: 2013-12-23
- Assignees: Total Marketing Services
- Applicants: Total Marketing Services
- Inventors: Xavier Chouan; Patrick Vedrine
- Web page: https://patentgrep.com/patent/US10246652B2

## CPC

- C10G 65/08: at least one step being a hydrogenation of the aromatic hydrocarbons
- C10G 45/44: Hydrogenation of the aromatic hydrocarbons
- C10G 2300/4031: Start up or shut down operations
- C10G 2300/70: Catalyst aspects
- 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

A process for the continuous dearomatization of a petroleum cut to produce a hydrocarbon-containing fluid with a very low sulphur content and very low aromatic compounds content, includes at least one stage of catalytic hydrogenation at a temperature between 80 and 180° C. and at a pressure between 50 and 160 bar. The stage of catalytic hydrogenation of the dearomatization process comprises several interchangeable reactors linked in series.

## Claims

### Claim 1

A process for continuous dearomatization of a petroleum cut, comprising:
(a) producing a hydrocarbon-containing fluid with a very low sulphur content and very low aromatic compounds content, at least one stage of catalytic hydrogenation at a temperature comprised between 80 and 180° C. and at a pressure comprised between 50 and 160 bar, and the stage of catalytic hydrogenation is made up of several interchangeable reactors linked in series;
(b) isolating one of the reactors;
(c) feeding a first one of two non-isolated reactors with the petroleum cut and feeding a second non-isolated reactor with effluent from the first non-isolated reactor;
(d) regenerating the isolated reactor by replacement of the catalyst;
(e) interrupting the feeding the second non-isolated reactor with effluent from the first non-isolated reactor; and
(f) feeding the regenerated reactor with the effluent from the first non-isolated reactors of stage (c) and feeding the second non-isolated reactor of stage (c) with the effluent from the regenerated reactor.

### Claim 2 (depends on 1)

The process according to claim 1, wherein the several interchangeable reactors of the stage of catalytic hydrogenation comprises three interchangeable reactors linked in series, each comprising at least one catalyst.

### Claim 3 (depends on 1)

The process according to claim 1, wherein first and second reactors, of the several interchangeable reactors, can be isolated in turn.

### Claim 4 (depends on 1)

The process according to claim 1, further comprising catalysts of the first and second reactors, of the several interchangeable reactors, being changed without prolonged interruption of the production of the hydrocarbon-containing fluids.

### Claim 5 (depends on 1)

The process according to claim 1, wherein the reactors in series are linked by fixed additional connections making it possible to isolate one of the reactors.

### Claim 6 (depends on 1)

The process according to claim 1, wherein the reactors in series are linked by removable additional connections making it possible to isolate one of the reactors.

### Claim 7 (depends on 1)

The process according to claim 1, wherein the reactors comprise catalysts, the catalysts of the reactors being changed at 100% saturation.

### Claim 8 (depends on 1)

The process according to claim 1, wherein a rate of hydrogenation is comprised between 50 and 300 Nm3/tonne of petroleum cut.

### Claim 9 (depends on 2)

The process according to claim 2, wherein a quantity by weight of catalyst in each of the reactors is 0.05-0.5/0.10-0.70/0.25-0.85.

### Claim 10 (depends on 9)

The process according to claim 9, wherein the quantity by weight of catalyst in each of the reactors is 0.07-0.25/0.15-0.35/0.4-0.78.

### Claim 11 (depends on 1)

The process according to claim 1, comprising the stages of:
(b) isolating the first reactor in series;
(c) feeding the second reactor in series with the petroleum cut and feeding a third reactor in series with the effluent from the second reactor;
(d) replacing the catalyst of the first reactor;
(e) interrupting the feeding the third reactor in series with the effluent from the second reactor; and
(f) feeding the first reactor with the effluent from the second reactor and feeding the third reactor with the effluent from the first reactor.

### Claim 12 (depends on 1)

The process according to claim 1, comprising the stages of:
(b) isolating the second reactor in series;
(c) feeding the first reactor in series with the petroleum cut and feeding a third reactor in series with the effluent from the first reactor;
(d) replacing the catalyst of the second reactor;
(e) interrupting the feeding the third reactor in series with the effluent from the first reactor; and
(f) feeding the second reactor with the effluent from the first reactor and feeding the third reactor with the effluent from the second reactor.