Method for converting heavy hydrocarbon feedstocks with recycling of a deasphalted oil

Patent metadata

Field	Value
Publication number	US-11149217-B2
Application number	US-201816957078-A
Country	US
Kind code	B2
Filing date	Dec 7, 2018
Priority date	Dec 21, 2017
Publication date	Oct 19, 2021
Grant date	Oct 19, 2021

Abstract

The invention relates to a process for converting a heavy hydrocarbon feedstock containing a fraction of at least 50% with a boiling point of at least 300° C., and containing sulfur, Conradson carbon, metals, and nitrogen, comprising at least two successive hydroconversion steps, which may be separated by an intermediate separation step, and at least one step of deasphalting a heavy fraction of the effluent resulting from the hydroconversion, with recycling at least one portion of the deasphalted oil (DAO) during the hydroconversion, downstream of the first hydroconversion step. The DAO is either recycled at the outlet thereof from the deasphalter, or after having undergone a fractionation step that produces a heavy fraction of the DAO that then constitutes the portion of the DAO that is recycled. This process makes it possible to simultaneously improve the degree of conversion and the stability of the liquid effluents.

First claim

The invention claimed is:

1. A process for converting a heavy hydrocarbon feedstock containing a fraction of at least 50% with a boiling point of at least 300° C., and containing sulfur, Conradson carbon, metals, and nitrogen, comprising the following successive steps:
an initial step of hydroconversion (a 1 ) of at least one portion of said heavy hydrocarbon feedstock in the presence of hydrogen in an initial hydroconversion section (A 1 ), performed under conditions that make it possible to obtain a liquid effluent with a reduced content of sulfur, of Conradson carbon, of metals and of nitrogen;
(n−1) additional hydroconversion step(s) (a i ) in (n−1) additional hydroconversion section(s) (A i ), in the presence of hydrogen, of at least a portion or all of the liquid effluent resulting from the preceding hydroconversion step (a i−1 ) or optionally of a heavy fraction resulting from an optional intermediate separation step (b j ) in an intermediate separation section (B j ) between two consecutive hydroconversion steps separating a portion or all of the liquid effluent resulting from the preceding hydroconversion step (a i−1 ) in order to produce at least one heavy fraction that boils predominantly at a temperature greater than or equal to 350° C., the (n−1) additional hydroconversion step(s) (a i ) being performed so as to obtain a hydroconverted liquid effluent with a reduced content of sulfur, of Conradson carbon, of metals and of nitrogen,
n being the total number of hydroconversion steps, with n greater than or equal to 2, i being an integer ranging from 2 to n and j being an integer ranging from 1 to (n−1), and the initial (A 1 ) and additional (A i ) hydroconversion section(s) each including at least one three-phase reactor containing at least one hydroconversion catalyst;
a first step of fractionating (c) in a first fractionation section (C) a portion or all of the hydroconverted liquid effluent resulting from the last additional hydroconversion step (a n ) producing at least one heavy cut that boils predominantly at a temperature greater than or equal to 350° C., said heavy cut containing a residual fraction that boils at a temperature greater than or equal to 540° C.;
a step of deasphalting (d) in a deasphalter (D) a portion or all of said heavy cut resulting from the fractionation step (c), with at least one hydrocarbon solvent, in order to obtain a deasphalted oil DAO and a residual asphalt;
a second step of fractionating (e) in a second fractionation section (E) a portion or all of the DAO resulting from the deasphalting step (d) into at least one heavy DAO fraction and one light DAO fraction, in which the second fractionation section (E) comprises one or more flash drums arranged in series, and/or one or more steam- and/or hydrogen-stripping columns, and/or an atmospheric distillation column, and/or a vacuum distillation column;
a step of recycling (f) at least one portion of the DAO resulting from step (d) and/or at least one portion of the heavy fraction of the DAO resulting from step (e) into an additional hydroconversion step (a i ) and/or into an intermediate separation step (b j ).

2. The process as claimed in claim 1 , in which said heavy hydrocarbon feedstock has a sulfur content of at least 0.1% by weight, a Conradson carbon content of at least 0.5% by weight, a C 7 asphaltenes content of at least 1% by weight, and a metals content of at least 20 ppm by weight.

3. The process as claimed in claim 1 , in which said heavy hydrocarbon feedstock is a crude oil or consists of atmospheric residues and/or vacuum residues resulting from the atmospheric and/or vacuum distillation of crude oil.

4. The process as claimed in claim 1 , in which said three-phase reactor containing at least one hydroconversion catalyst is a three-phase reactor with ebullated-bed operation, with an upflow of liquid and of gas.

5. The process as claimed in claim 1 , in which said three-phase reactor containing at least one hydroconversion catalyst is a three-phase reactor with hybrid-bed operation, said hybrid bed including at least one catalyst maintained in said three-phase reactor and at least one catalyst entrained out of said three-phase reactor.

6. The process as claimed in claim 1 , in which the initial hydroconversion step (a 1 ) is performed under an absolute pressure of between 2 and 38 MPa, at a temperature of between 300° C. and 550° C., at an hourly space velocity HSV relative to the volume of each three-phase reactor of between 0.05 h −1 and 10 h −1 and under an amount of hydrogen mixed with the heavy hydrocarbon feedstock of between 50 and 5000 normal cubic meters (Nm 3 ) per cubic meter (m 3 ) of heavy hydrocarbon feedstock.

7. The process as claimed in claim 1 , in which the additional hydroconversion step(s) (a n ) are performed at a temperature of between 300° C. and 550° C., and above the temperature used in the initial hydroconversion step (a 1 ), under an amount of hydrogen mixed with the heavy hydrocarbon feedstock of between 50 and 5000 normal cubic meters (Nm 3 ) per cubic meter (m 3 ) of heavy hydrocarbon feedstock, and less than the amount of hydrogen used in the initial hydroconversion step (a 1 ), under an absolute pressure of between 2 and 38 MPa, and at an hourly space velocity HSV relative to the volume of each three-phase reactor of between 0.05 h −1 and 10 h −1 .

8. The process as claimed in claim 1 , in which the intermediate separation section (B j ) comprises one or more flash drums arranged in series, and/or one or more steam- and/or hydrogen-stripping columns, and/or an atmospheric distillation column, and/or a vacuum distillation column.

9. The process as claimed in claim 1 , in which the first fractionation section (C) comprises one or more flash drums arranged in series, and/or one or more steam- and/or hydrogen-stripping columns, and/or an atmospheric distillation column, and/or a vacuum distillation column.

10. The process as claimed in claim 1 , in which the second fractionation section (E) consists of a set of several flash drums in series and a vacuum distillation column.

11. The process as claimed in claim 1 , in which the deasphalting step (d) is performed in an extraction column at a temperature of between 60° C. and 250° C. with at least one hydrocarbon solvent containing from 3 to 7 carbon atoms, and a (volume/volume) solvent/feedstock ratio of between 3/1 and 16/1.

12. The process as claimed in claim 1 , in which a portion of the heavy hydrocarbon feedstock is sent to at least one additional hydroconversion section (A i ) and/or to at least one intermediate separation section (B j ) and/or to the first fractionation section (C) and/or to the deasphalter (D).

13. The process as claimed in claim 1 , in which a hydrocarbon feedstock external to the process is sent to the initial hydroconversion section (A 1 ) and/or to at least one additional hydroconversion section (A i ) and/or to at least one intermediate separation section (B j ) and/or to the first fractionation section (C) and/or to the deasphalter (D).

14. The process as claimed in claim 1 , also comprising at least one recycling step below:
the recycling (r 1 ) of a portion or all of the light fraction of the DAO resulting from step (e) into the initial hydroconversion section (A 1 ) and/or into at least one additional hydroconversion section (A i ) and/or into at least one intermediate separation section (B j ) and/or into the first fractionation section (C);
the recycling (r 2 ) of a portion of the heavy fraction of the DAO resulting from step (f) into the first fractionation section (C);
the recycling (r 3 ) of a portion of the DAO resulting fr

Assignees

• Ifp Energies Now

Inventors

• Marques Joao
• Verstraete Jan

Classifications

• C10G2300/202

  Heteroatoms content, i.e. S, N, O, P · CPC title

• C10G2300/1077

  Vacuum residues · CPC title

• C10G2300/4006

  Temperature · CPC title

• C10G2300/206

  Asphaltenes · CPC title

• C10G45/08

  in combination with chromium, molybdenum, or tungsten metals, or compounds thereof · CPC title