Process and system for hydrotreating deoiled asphalt

Patent metadata

Field	Value
Publication number	US-12467004-B2
Application number	US-202017772799-A
Country	US
Kind code	B2
Filing date	Oct 30, 2020
Priority date	Oct 31, 2019
Publication date	Nov 11, 2025
Grant date	Nov 11, 2025

Abstract

Described are a process and a system for hydrotreating a deoiled asphalt. The process includes: (2) introducing a deoiled asphalt and an aromatics-containing stream into a first reaction unit for hydrogenation reaction, wherein the first reaction unit comprises a mineral-rich precursor material and/or a hydrogenation catalyst, and the first reaction unit is a fixed bed hydrogenation unit; (21) fractionating the liquid-phase product from the first reaction unit to provide a first light component and a first heavy component; (31) introducing the first light component into a second reaction unit for reaction, to provide a gasoline component, a diesel component and/or a BTX feedstock component; and (32) introducing the first heavy component to a delayed coking unit for reaction; or using the first heavy component as a low sulfur ship fuel oil component.

First claim

What is claimed is:

1 . A process for hydrotreating deoiled asphalt, comprising:
(1) introducing a heavy oil feedstock into a solvent deasphalting unit for solvent deasphalting treatment, to provide a deoiled asphalt and a deasphalted oil; (2) introducing a mixed feedstock obtained by mixing the deoiled asphalt and an aromatics-containing stream into a first reaction unit for hydrogenation reaction, wherein the composition and the ratio of the deoiled asphalt and the aromatics-containing stream are that the mixed feedstock is in a liquid state at a temperature of not higher than 400° C., and the deoiled asphalt and the aromatics-containing stream are used at weight ratio of 1:10 to 50:10; (11) introducing the deasphalted oil into a third hydrogenation unit for hydrogenation reaction to obtain a liquid phase effluent, and introducing the liquid phase effluent obtained in the third hydrogenation unit into a DCC unit for reaction, to provide propylene, LCO, HCO and a slurry oil; (13) introducing the slurry oil obtained in the DCC unit into a fourth hydrogenation unit for demetallization reaction, to provide demetallized slurry oil; and incorporating the LCO, the HCO, and/or the slurry oil obtained in the DCC unit and/or the demetallized slurry oil obtained in the fourth hydrogenation unit into the aromatics-containing stream in step (2) or using the LCO, the HCO, and/or the slurry oil obtained in the DCC unit and/or the demetallized slurry oil obtained in the fourth hydrogenation unit as the aromatics-containing stream in step (2); (21) separating a liquid phase product from the first reaction unit into a first light component and a first heavy component, wherein the first light component and the first heavy component have a cutting point of 240-450° C., and wherein the separation is optionally carried out by fractional distillation; (31) introducing the first light component into a second reaction unit for reaction, to provide at least one product selected from the group consisting of a gasoline component, a diesel component and a BTX feedstock component, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit and a diesel hydro-upgrading unit; and (32) introducing the first heavy component into a delayed coking unit for reaction, to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil and low sulfur petroleum coke; or using the first heavy component as a low sulfur ship fuel oil component.

2 . The process according to claim 1 , wherein in step (2), the deoiled asphalt and the aromatics-containing stream are used in such a ratio that the mixed feedstock formed from the deoiled asphalt and the aromatics-containing stream has a viscosity at 100° C. of not more than 400 mm 2 /s.

3 . The process according to claim 1 , wherein in step (2), the aromatics-containing stream is an aromatics-rich fraction oil and/or aromatic compounds.

4 . The process according to claim 3 , wherein the aromatic compound is at least one selected from the group consisting of benzene, toluene, xylene, naphthalene, naphthalene substituted with at least one C 1-6 alkyl group, tricyclic or higher aromatic hydrocarbon.

5 . The process according to claim 3 , wherein the aromatics-rich fraction oil has a distillation end point of 200-540° C., an aromatic hydrocarbon content of more than or equal to 20 wt %; and the aromatics-rich fraction oil is at least one selected from the group consisting of LCO, HCO, FGO, ethylene tar, coal tar, coker diesel and coker wax oil.

6 . The process according to claim 1 , wherein in step (2), the deoiled asphalt and the aromatics-containing stream are used at weight ratio of 3:10 to 30:10.

7 . The process according to claim 1 , wherein in step (2), the deoiled asphalt is a deoiled asphalt obtained by subjecting a heavy oil feedstock to a solvent deasphalting treatment in a solvent deasphalting unit;
in the solvent deasphalting unit, the deoiled asphalt is obtained at a yield of not more than 50%.

8 . The process according to claim 1 , wherein the process further comprises: recycling the coker diesel and/or coker wax oil obtained in step (32) back to step (2) for as at least part of the aromatics-containing stream.

9 . The process according to claim 1 , wherein in step (2), the first reaction unit is operated under conditions of: a reaction temperature of 280-450° C., a reaction pressure of 8.0-20.0 MPa, a volume ratio of hydrogen to oil of 400-2000, and a liquid hourly volume space velocity of 0.05-1.2 h −1 .

10 . The process according to claim 1 , wherein in step (31), the second reaction unit is a hydrocracking unit,
wherein the hydrocracking unit is operated under conditions of: a reaction temperature of 330-420° C., a reaction pressure of 5.0-18.0 MPa, a volume ratio of hydrogen to oil of 500-2000, and a liquid hourly volume space velocity of 0.3-3.0 h −1 ; and/or the hydrocracking unit is loaded with at least one hydrotreating catalyst and at least one hydrocracking catalyst.

11 . The process according to claim 1 , wherein in step (31), the second reaction unit is a catalytic cracking unit, and the catalytic cracking unit is a fluidized catalytic cracking unit;
wherein the fluidized catalytic cracking unit is operated under conditions of: a reaction temperature of 500-600° C., a catalyst-to-oil ratio of 3-12, and a retention time of 1-10 s.

12 . The process according to claim 1 , wherein in step (31), the second reaction unit is a diesel hydro-upgrading unit,
wherein the diesel hydro-upgrading unit is operated under conditions of: a reaction temperature of 330-420° C., a reaction pressure of 5.0-18.0 MPa, a volume ratio of hydrogen to oil of 500-2000, and a liquid hourly volume space velocity of 0.3-3.0 h −1 ; and/or the diesel hydro-upgrading unit is loaded with at least one diesel hydro-upgrading catalyst.

13 . The process according to claim 1 , wherein in step (32), the first heavy component is fed into a delayed coking unit for reaction to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low sulfur petroleum coke, and the delayed coking unit is operated under conditions of: a reaction temperature of 440-520° C., and a retention time of 0.1-4 h.

14 . The process according to claim 13 , wherein in step (32), the first heavy component has a sulfur content of not greater than 1.8 wt %, and the first heavy component is fed into a delayed coking unit for reaction, to provide a low-sulfur petroleum coke having a sulfur content of not greater than 3 wt %.

15 . The process according to claim 1 , wherein in step (32), the first heavy component is useful as a low-sulfur ship fuel oil component and the low-sulfur ship fuel oil component has a sulfur content of not greater than 0.5 wt %.

16 . The process according to claim 1 , wherein the first reaction unit is a fixed bed hydrogenation unit, a moving bed-fixed bed hydrogenation combined unit, or a moving bed hydrogenation unit.

17 . The process according to claim 1 , wherein,
the first reaction unit comprises a mineral-rich precursor material and/or a hydrogenation catalyst, the hydrogenation catalyst can catalyze at least one reaction selected from hydrodemetallization reaction, hydrodesulfurization reaction, hydrodeasphalting reaction and hydrodecarbonization reaction, and the mineral-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca and Mg.

Assignees

• China Petroleum & Chem Corp
• Sinopec Res Inst Petroleum

Inventors

• Yang Qinghe
• Sun Shuling
• Hu Dawei
• Niu Chuanfeng
• Jia yanzi
• Dai Lishun
• Wang Zhen
• Hu Anpeng
• Ren Liang
• Li Dadong

Classifications

• C10G2400/30

  Aromatics · CPC title

• C10G2400/04

  Diesel oil · CPC title

• C10G2400/02

  Gasoline · CPC title

• C10G2300/4018

  Spatial velocity, e.g. LHSV, WHSV · CPC title

• C10G2300/4012

  Pressure · CPC title