Process and system for processing aromatics-rich fraction oil

Patent metadata

Field	Value
Publication number	US-12331256-B2
Application number	US-202017772317-A
Country	US
Kind code	B2
Filing date	Oct 30, 2020
Priority date	Oct 31, 2019
Publication date	Jun 17, 2025
Grant date	Jun 17, 2025

Abstract

Described are a process and a system for processing aromatics-rich fraction oil. The process includes: (1) introducing an aromatics-rich fraction oil into a fifth reaction unit for hydrosaturation, followed by fractionation, to provide a first light component and a first heavy component; (2) introducing a deoiled asphalt and an aromatics-comprising stream including the first heavy component into a hydrogen dissolving unit to be mixed with hydrogen, and introducing the mixed material into a first reaction unit for a hydrogenation reaction; (3) fractionating a liquid-phase product from the first reaction unit to provide a second light component and a second heavy component; (41) introducing the second light component into a second reaction unit for reaction; and (42) introducing the second heavy component into a delayed coking unit for reaction; or using the second heavy component as a component of low sulfur ship fuel oil.

First claim

What is claimed is:

1. A process for processing an aromatics-rich fraction oil, comprising:
(11) introducing a heavy raw oil into a solvent deasphalting unit for solvent deasphalting treatment, to provide a deoiled asphalt and a deasphalted oil;
(12) introducing the deasphalted oil into a fourth reaction unit for hydrogenation reaction, introducing a liquid phase effluent obtained in the fourth reaction unit into a DCC unit for reaction, to provide propylene, LCO, HCO and slurry oil;
(1) introducing an aromatics-rich fraction oil comprising the LCO and/or HCO from the DCC unit into a third reaction unit for hydrosaturation, followed by fractionation, to provide a first light component and a first heavy component, wherein the first light component and the first heavy component has a cutting point of 100-250° C., and the aromatic content in the first heavy component is more than or equal to 20 wt %;
(2) introducing the deoiled asphalt and an aromatics-comprising stream comprising the first heavy component from step (1) into a hydrogen dissolving unit to be mixed with hydrogen to form a mixed material, and introducing the mixed material into a first reaction unit for a hydrogenation reaction, wherein the deoiled asphalt and the aromatics-containing stream are used in such an amount ratio that a mixed feedstock formed by the deoiled asphalt and the aromatics-containing stream is in liquid state at a temperature of not higher than 400° C.;
(3) fractionating a liquid-phase product from the first reaction unit to provide a second light component and a second heavy component, wherein the cutting point for the second light component and the second heavy component is at 240-450° C.;
(41) introducing the second light component into a second reaction unit for reaction, to provide at least one product selected from 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
(42) introducing the second 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 second heavy component as a component of low sulfur ship fuel oil.

2. The process according to claim 1 , wherein in step (2), the deoiled asphalt and the aromatics-containing stream are used in a ratio such that the viscosity at 100° C. of the mixed feedstock formed from the deoiled asphalt and the aromatics-containing stream is not greater than 400 mm 2 /s, and/or
wherein in step (2), the first reaction unit comprises a mineral-rich precursor material and a hydrogenation catalyst, the first reaction unit is a liquid-phase hydrogenation reaction unit, the mineral-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca and Mg.

3. The process according to claim 1 , wherein in step (2), the mineral-rich precursor material has a loss on ignition of not less than 3 wt %, a specific surface area of not less than 80 m 2 /g, and a water absorption of not less than 0.9 g/g.

4. The process according to claim 3 , wherein in step (2), the mineral-rich precursor material comprises a support and an active component element loaded on the support, wherein the support is at least one selected from the group consisting of aluminum hydroxide, alumina and silica, and the active component element is at least one metal element selected from the group consisting of Group VIB and Group VIII.

5. The process according to claim 4 , wherein in step (2), according to the flowing direction of reactants, the first reaction unit is sequentially loaded with a first mineral-rich precursor material and a second mineral-rich precursor material, and the second mineral-rich precursor material has a loss on ignition equal to or greater than that of the first mineral-rich precursor material;
wherein the first mineral-rich precursor material has a loss on ignition of 3-15% by weight, and the second mineral-rich precursor material has a loss on ignition of not less than 15% by weight; and/or
the first mineral-rich precursor material and the second mineral-rich precursor material are loaded at a ratio by volume of from 5:95 to 95:5.

6. The process according to claim 1 , wherein in step (2), the aromatics-containing stream further comprises an aromatic hydrocarbon and/or an aromatic oil,
wherein the aromatic oil is at least one selected from the group consisting of LCO, HCO, FGO, ethylene tar, coal tar, coker diesel, and coker wax oil; and/or
the aromatic hydrocarbon 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, and tricyclic or higher aromatic hydrocarbons.

7. The process according to claim 1 , wherein the aromatics-rich fraction oil has an aromatic content of more than or equal to 20 wt %.

8. The process according to claim 1 , wherein
in the solvent deasphalting unit, the yield of the deoiled asphalt is not more than 50% by weight.

9. The process according to claim 1 , wherein in step (2), the weight ratio of the amount of the deoiled asphalt to the amount of the aromatics-containing stream is from 1:10 to 50:10.

10. The process according to claim 1 , further comprising: recycling the coker diesel and/or coker wax oil obtained in step (42) to the third reaction unit in step (1) for hydrosaturation.

11. The process according to claim 10 , wherein in step (2), the first reaction unit is operated under conditions of: a reaction temperature of 260-500° C., a reaction pressure of 2.0-20.0 MPa, and a liquid hourly space velocity of 0.1-1.5 h −1 .

12. The process according to claim 1 , wherein in step (1), the third reaction unit is at least one of a fixed bed reactor, a moving bed reactor and a boiling bed reactor; and/or
wherein the third reaction unit is operated under conditions of: a reaction temperature of 200-420° C., a reaction pressure of 2-18 MPa, a liquid hourly space velocity of 0.3-10 h −1 , and a volume ratio of hydrogen to oil of 50-5000.

13. The process according to claim 1 , wherein in step (41), the second reaction unit is a hydrocracking unit, operated under conditions of: a reaction temperature of 360-420° C., a reaction pressure of 10.0-18.0 MPa, a volume ratio of hydrogen to oil of 600-2000, and a liquid hourly volume space velocity of 1.0-3.0 h −1 ; and/or
wherein the hydrocracking unit is loaded with at least one hydrotreating catalyst and at least one hydrocracking catalyst.

14. The process according to claim 1 , wherein in step (41), the second reaction unit is a catalytic cracking unit, and the catalytic cracking unit is a fluid catalytic cracking unit;
wherein the fluid 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 0.6-6 s.

15. The process according to claim 1 , wherein in step (41), the second reaction unit is a diesel hydrogenation upgrading unit,
wherein the diesel hydrogenation 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 hydrogenation upgrading unit is loaded with at least one diesel hydrogenation upgrading catalyst.

16. The process according to claim 1 , whe

Assignees

• China Petroleum & Chem Corp
• Sinopec Res Inst Petroleum

Inventors

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

Classifications

• C10G69/06

  including at least one step of thermal cracking in the absence of hydrogen · CPC title

• C10G69/04 Primary

  including at least one step of catalytic cracking in the absence of hydrogen · CPC title

• C10G2400/30

  Aromatics · CPC title

• C10G2400/08

  Jet fuel · CPC title

• C10G2400/04

  Diesel oil · CPC title