Process and system for upgrading low-quality oils

Patent metadata

Field	Value
Publication number	US-11078434-B2
Application number	US-201716646070-A
Country	US
Kind code	B2
Filing date	Sep 11, 2017
Priority date	Sep 11, 2017
Publication date	Aug 3, 2021
Grant date	Aug 3, 2021

Abstract

Disclosed is a process and system for upgrading low-quality oils. The upgrading process comprises: (1) subjecting a low-quality oil to a conversion reaction in the presence of hydrogen and optionally in the presence of a conversion catalyst to obtain a conversion product, (2) processing the conversion product to obtain a first processed product, wherein the first processed product comprises a specific amount of a special component, and (3) subjecting the first processed product to extraction separation to obtain an upgraded oil and a pitch. The upgrading process and the upgrading system have the advantages of stable operation, high upgrading efficiency, environmental friendliness, low coke yield or high yield of upgraded oil.

First claim

The invention claimed is:

1. An upgrading process, comprising:
(1) subjecting a low-quality oil used as an upgrading feedstock to a conversion reaction in the presence of hydrogen to obtain a conversion product,
(2) processing the conversion product to obtain a first processed product, wherein the first processed product comprises from 20 wt % to 60 wt % of a component having a boiling point or boiling range between 350° C. and 524° C., and
(3) subjecting the first processed product to extraction separation to obtain an upgraded oil and a pitch.

2. The upgrading process according to claim 1 , wherein the step (2) further comprises:
(2-1) subjecting the conversion product to a first separation at a first pressure and a first temperature to obtain a gas component and a liquid component, and
(2-2) subjecting the liquid component to a second separation at a second pressure and a second temperature to obtain a second separated product and a first separated product, wherein the first separated product is the first processed product, and the second separated product or any component thereof has a final boiling point of less than or equal to 350° C.,
wherein the first pressure is 4-24 MPa greater than the second pressure.

3. The upgrading process according to claim 2 , wherein the first pressure is in a range from 10.0 MPa to 25.0 Mpa and the first temperature is in a range from 380° C. to 470° C.; or the second pressure is in a range from 0.1 MPa to 5.0 Mpa, and the second temperature is in a range from 150° C. to 390° C.

4. The upgrading process according to claim 2 , wherein the step (2) further comprises:
(2-3) separating the second separated product to obtain naphtha and atmospheric gas oil, and
(2-4) subjecting the gas component to step (1), and
wherein the first pressure is 7-19 MPa greater than the second pressure.

5. The upgrading process according to claim 1 , wherein the step (3) further comprises:
(3-1) contacting the first processed product with a solvent at a third pressure and a third temperature to obtain the upgraded oil and the pitch.

6. The upgrading process according to claim 5 , wherein the solvent is one or more of C 3-7 hydrocarbons, and a weight ratio of the solvent to the first processed product is 1-7:1.

7. The upgrading process according to claim 5 , wherein the third pressure is in a range from 3 MPa to 12 Mpa, and the third temperature is in a range from 55° C. to 300° C.

8. The upgrading process according to claim 5 , wherein the step (3) further comprises one or more of the following steps:
(3-2) subjecting the upgraded oil to hydrogenation to obtain a hydrotreated upgraded oil,
(3-3) subjecting the upgraded oil to hydrocracking to obtain a hydrocracked product, and then separating the hydrocracked product into dry gas, liquefied gas, aviation kerosene, diesel oil, and hydrogenated tail oil,
(3-4) subjecting the hydrotreated upgraded oil to catalytic cracking to obtain a first catalytic cracked product, and then separating the first catalytic cracked product into dry gas, liquefied gas, gasoline, cycle oil and slurry oil,
(3-5) catalytically cracking a mixture comprising the hydrotreated upgraded oil and the atmospheric gas oil to obtain a second catalytic cracked product, and then separating the second catalytic cracked product into dry gas, liquefied gas, gasoline, cycle oil and slurry oil,
(3-6) catalytically cracking a mixture comprising the hydrotreated upgraded oil and the second separated product to obtain a third catalytic cracked product, and then separating the third catalytic cracked product into dry gas, liquefied gas, gasoline, cycle oil and slurry oil,
(3-7) subjecting the atmospheric gas oil to a hydrogenation reactor to obtain diesel oil,
(3-8) subjecting the cycle oil obtained in any step of the upgrading process to a hydrogenation reactor alone or together with the upgraded oil to obtain a hydrotreated oil,
(3-9) catalytically cracking a mixture comprising the hydrotreated oil and the second separated product to obtain a fourth catalytic cracked product, and then separating the fourth catalytic cracked product into dry gas, liquefied gas, gasoline, cycle oil and slurry oil,
(3-10) subjecting the slurry oil obtained in any step of the upgrading process and/or an externally supplied slurry oil to the step (1), step (2), and/or step (3), or
(3-11) subjecting the liquefied gas obtained in any step of the upgrading process to the step (3) or step (3-1).

9. The upgrading process according to claim 8 , wherein the step (3-2) or step (3-8) is carried out in the presence of a hydrogenation catalyst under the following conditions: a hydrogen partial pressure between 5.0 MPa and 20.0 MPa, a reaction temperature between 330° C. and 450° C., a volumetric space velocity of the feedstock oil between 0.1 h −1 and 3.0 h −1 , and a volume ratio of hydrogen to feedstock oil between 300 and 3000;
or alternatively, the step (3-3) is carried out in the presence of a hydrocracking catalyst under the following conditions: a hydrogen partial pressure between 10.0 MPa and 20.0 MPa, a reaction temperature between 310° C. and 420° C., a volumetric space velocity of the upgraded oil between 0.3 h −1 and 1.2 h −1 , and a volume ratio of hydrogen to the upgraded oil between 600 and 1500;
or alternatively, the step (3-4), step (3-5), step (3-6) or step (3-9) is carried out in the presence of a cracking catalyst under the following conditions: a reaction temperature between 450° C. and 650° C., a reaction pressure between 0.15 MPa and 0.4 MPa, a reaction time between 0.1 seconds and 10 seconds, a weight ratio of cracking catalyst to feedstock oil between 3 and 30, and a weight ratio of steam to feedstock oil between 0.05 and 0.6;
or alternatively, the step (3-7) is carried out in the presence of a hydrogenation catalyst under the following conditions: a hydrogen partial pressure between 7.0 MPa and 15.0 MPa, a reaction pressure between 8 MPa and 12 MPa, a reaction temperature between 340° C. and 400° C.; a volumetric space velocity of the atmospheric gas oil between 0.6 h −1 and 1.5 h −1 , and a volume ratio of hydrogen to the atmospheric gas oil between 500 and 800.

10. The upgrading process according to claim 1 , wherein the conversion reaction is carried out in the presence of a conversion catalyst under the following conditions: a hydrogen partial pressure between 10.0 MPa and 25.0 MPa, a reaction temperature between 380° C. and 470° C., a volumetric space velocity of the upgrading feedstock between 0.01 h −1 and 2.0 h −1 , and a volume ratio of hydrogen to the upgrading feedstock between 500 and 5000.

11. The upgrading process according to claim 1 , wherein the pitch has a softening point of less than 150° C.

12. The upgrading process according to claim 1 , wherein the low-quality oil is one or more selected from the group consisting of inferior oils, deoiled asphalt, heavy oil, extra heavy oil, coal-derived oil, shale oil, and petrochemical waste oil, and wherein the heavy oil is one or more selected from the group consisting of topped crude oil, heavy oil derived from oil sands bitumen, and heavy oil having an initial boiling point of greater than 350° C., the coal-derived oil is one or more selected from the group consisting of coal liquefied oil produced by coal liquefaction and coal tar produced by coal pyrolysis, or the petrochemical waste oil is one or more selected from the group consisting of petrochemical waste oil sludge, petrochemical oil residue, and refined products thereof.

13. The upgrading process according to claim 1 , wherein the first processed product has an initial boiling point of greater than or

Assignees

• China Petroleum & Chem Corp
• Sinopec Res Inst Petroleum

Inventors

• Long Jun
• Hou Huandi
• Wang Zijun
• Shen Haiping
• Dong Ming
• Dai Lishun
• Gong Jianhong
• Li Jiguang
• Zhang Shuhong
• Wang Cuihong
• She Yucheng
• Wang Yuzhang
• Tao Mengying

Classifications

• C10G67/02 Primary

  plural serial stages only · CPC title

• C10G67/00

  Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only · CPC title

• C10G21/00

  Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents (C10G17/00, C10G19/00 take precedence) · CPC title

• B01D11/04

  of solutions which are liquid · CPC title

• B01D3/06

  Flash distillation · CPC title