Integrated process for the treatment of oil feeds for the production of fuel oils with a low sulphur and sediment content

Patent metadata

Field	Value
Publication number	US-9650580-B2
Application number	US-201415105314-A
Country	US
Kind code	B2
Filing date	Dec 5, 2014
Priority date	Dec 17, 2013
Publication date	May 16, 2017
Grant date	May 16, 2017

Abstract

Treating a hydrocarbon feed having a sulphur content of at least 0.5% by weight, an asphaltenes content of at least 1% by weight, an initial boiling point of at least 340° C. and a final boiling point of at least 480° C., in order to obtain at least one deasphalted oil fraction with a sulphur content of 0.5% by weight or less and a sediment content of 0.1% by weight or less.

First claim

The invention claimed is:

1. A process for the treatment of a hydrocarbon feed having a sulphur content of at least 0.5% by weight, an asphaltenes content of at least 1% by weight, an initial boiling point of at least 340° C., and a final boiling point of at least 480° C., in order to obtain at least one deasphalted oil fraction with a sulphur content of 0.5% by weight or less and a sediment content of 0.1% by weight or less, comprising, in succession:
a) fixed bed hydrotreatment, in which the hydrocarbon feed and hydrogen are brought into contact over at least one hydrotreatment catalyst,
b) optionally, separating effluent obtained from the hydrotreatment a) into at least one light fraction and at least one heavy fraction,
c) hydroconversion of at least a portion of effluent obtained from a) or at least a portion of the heavy fraction obtained from b) and optionally at least a portion of the light fraction obtained from b) in at least one reactor containing at least one supported ebullated bed catalyst,
d) separating effluent obtained from c) in order to obtain at least one gaseous fraction and a liquid hydrocarbon fraction, by an atmospheric distillation, in which the effluent obtained at the end of c) is fractionated by atmospheric distillation into at least one atmospheric distillate fraction and at least one atmospheric residue fraction, then a vacuum distillation in which at least a portion of the atmospheric residue fraction obtained after atmospheric distillation is fractionated by vacuum distillation into at least one vacuum distillate fraction and at least one vacuum residue fraction; and at least a portion of the vacuum residue fraction is recycled to the hydrotreatment a),
e) at least one selective deasphalting in order to separate at least one asphalt fraction and at least one deasphalted oil fraction, the deasphalting being carried out at least by bringing at least a portion of the liquid hydrocarbon fraction obtained from d), comprising at least a portion of said vacuum residue fraction and optionally a portion of said vacuum distillate fraction, into contact with a mixture of at least one polar solvent and at least one apolar solvent under subcritical conditions for the mixture of solvents used,
f) recycling at least a portion of said deasphalted oil fraction obtained from e) upstream of the hydrotreatment a) and/or to the inlet for the hydroconversion c).

2. The process according to claim 1 , in which the deasphalting e) comprises at least two deasphaltings in series in order to separate at least one asphalt fraction, at least one deasphalted oil fraction termed heavy DAO and at least one light deasphalted oil fraction termed light DAO, at least one of said deasphaltings being carried out by bringing at least a portion of the liquid hydrocarbon fraction obtained from d) into contact with a mixture of at least one polar solvent and at least one apolar solvent under subcritical conditions for the mixture of solvents used.

3. The process according to claim 2 , in which in f), at least a portion of the deasphalted oil fraction termed heavy DAO obtained from e) is recycled upstream of the hydrotreatment a) and/or to the inlet for the hydroconversion c).

4. The process according to claim 1 , in which e) is carried out at an extraction temperature in the range 50° C., to 350° C., and at a pressure in the range 0.1 to 6 MPa.

5. The process according to claim 1 , in which the fixed bed hydrotreatment is carried out at a temperature in the range 300° C., to 500° C., at an absolute pressure in the range 2 MPa to 35 MPa, with an hourly space velocity of the hydrocarbon feed in the range from 0.1 h −1 to 5 h −1 , and the quantity of hydrogen is in the range 100Nm 3 /m 3 to 5000 Nm 3 /m 3 .

6. The process according to claim 1 , in which the polar solvent used is (i) a pure aromatic solvent, a naphtheno-aromatic solvent, a polar solvent comprising hetero-elements, or a mixture thereof, or (ii) a cut rich in aromatics, a cut obtained from FCC (Fluid Catalytic Cracking), a cut derived from coal, a cut derived from biomass or a cut derived from a biomass/coal mixture.

7. The process according to claim 1 , in which the apolar solvent used comprises a solvent composed of a saturated hydrocarbon containing 2 or more carbon atoms.

8. The process according to claim 1 , in which the hydroconversion c) is carried out at an absolute pressure in the range 2.5 MPa to 35 MPa, at a temperature in the range 330° C., to 550° C., with a space velocity in the range from 0.1 h −1 to 5 h −1 , and with a quantity of hydrogen of 50 Nm 3 /m 3 to 5000 Nm 3 /m 3 .

9. The process according to claim 1 , in which least a portion of the atmospheric residue fraction is sent to the hydroconversion c).

10. The process according to claim 1 , in which the hydrocarbon feed is an atmospheric residue, straight run vacuum residue, crude oil, topped crude oil, deasphalting resin, asphalt or deasphalted pitch, a residue obtained from a conversion process, an aromatic extract obtained from production lines for lubricant bases, bituminous sand or a derivative, oil shale or a derivative, or source rock oil or a derivative, used alone or as a mixture.

11. The process according to claim 10 , in which the hydrocarbon feed is diluted with a co-feed that is a hydrocarbon fraction or a mixture of lighter hydrocarbon fractions which may be products obtained from a fluidized bed catalytic cracking process, a light oil cut LCO, a heavy oil cut HCO, a decanted oil, a FCC residue, a diesel fraction; one or more cuts obtained from a coal liquefaction process or from biomass, aromatic extracts, or non-oilfield feeds.

12. The process according to claim 1 , in which the deasphalted oil fraction obtained is mixed with one or more cutter stocks that are light oil cuts (LCO) from catalytic cracking, heavy oil cuts (HCO) from catalytic cracking, a catalytic cracking residue, kerosene, diesel, vacuum distillate and/or a decanted oil.

13. The process according to claim 12 , in which the cutter stock is a portion of kerosene and/or diesel or vacuum diesel type light hydrocarbon fraction obtained from the separation b).

14. The process according to claim 1 , in which the apolar solvent used comprises a solvent composed of a saturated hydrocarbon containing 2 to 9 carbon atoms.

Assignees

• Ifp Energies Now

Inventors

• Merdrignac Isabelle
• Weiss Wilfried
• Majcher Jerome

Classifications

• C10G45/02 Primary

  to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing · CPC title

• C10G21/06

  characterised by the solvent used · CPC title

• C10G2400/06

  Gasoil · CPC title

• C10L2200/0446

  Diesel · CPC title

• C10G65/12

  including cracking steps and other hydrotreatment steps · CPC title