# US 4,395,330 A · Process for solvent deasphalting of residual hydrocarbon oils

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- Number: US 4,395,330 A
- Document ID: US4395330A
- Status: Granted
- Kind: A
- Application number: 06/325,254
- Filed: 1981-11-27
- Granted: 1983-07-26
- Earliest claimed: 1980-11-28
- Assignees: Institut Francais du Petrole
- Inventors: Pierre Auboir; Pierre Bonnefond; Larry Mank
- Web page: https://patentgrep.com/patent/US4395330A

## CPC

- C10G 21/28: Recovery of used solvent
- C10G 21/003: {Solvent de-asphalting}
- 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

An asphaltene-containing residual hydrocarbon oil is deasphalted by means of a light hydrocarbon solvent. Heating of the resultant asphaltic phase for solvent removal is effected by heat exchange with the deasphalted oil previously subjected to sufficient heating in a furnace heated by flame. Fouling of the plant is thus avoided.

## Claims

### Claim 1

In a process for solvent deasphalting an asphaltene-containing residual hydrocarbon oil, wherein the residual oil is contacted with a light hydrocarbon solvent, in an extraction zone, deasphalting conditions are maintained to allow the formation of a liquid solvent-deasphalted oil phase and a fluid solvent-asphalt phase, the two resultant phases are separated and the solvent is separately vaporized from each of the two phases, so as to separately obtain a deasphalted oil and an asphaltic residue, the improvement comprising:
a. passing a portion of the deasphalted oil, substantially freed of solvent, through a zone of indirect heating by flame, so as to raise its temperature;
b. contacting the reheated deasphalted oil from step (a), in indirect heat exchange relation, with the fluid solvent-asphalt phase, so as to deliver to said phase at least a part of the heat necessaary to vaporize the solvent therein; and
c. admixing the deasphalted oil, after the heat exchanger of step (b), with the liquid solvent-deasphalted oil phase recovered from the extraction zone.

### Claim 2 (depends on 1)

A process according to claim 1, wherein a portion of the reheated deasphalted oil from step (a) is contacted, in indirect heat exchange relation, with the asphaltic residue, so as to reheat said residue and make it more fluid.

### Claim 3 (depends on 1)

A process according to claim 1, wherein the temperature of the deasphalted oil is raised to 250.degree.-420.degree. C. in step (a).

### Claim 4 (depends on 1)

A process according to claim 1, wherein the temperature of the deasphalted oil is raised to 350.degree.-400.degree. C. in step (a).

### Claim 5 (depends on 1)

A process according to claim 1, wherein the solvent vapor separated from the deasphalted oil is contacted, in heat exchange portion, with the liquid solvent-deasphalted oil phase before subjecting the latter to the mixing of step (c).

### Claim 6 (depends on 1)

A process according to claim 1, wherein the solvent is selected from the aliphatic hydrocarbons with 4 to 7 carbon atoms.

### Claim 7 (depends on 1)

A process according to claim 1, wherein the solvent is selected from the aliphatic hydrocarbons with 5 to 7 carbon atoms.

### Claim 8 (depends on 1)

A process according to claim 1, wherein the feed rate of the deasphalted oil supplied to step (a) is controlled according to the heat amount to be delivered to the fluid solvent-asphaltic oil phase.