Wax oil hydrocracking method and system

Patent metadata

Field	Value
Publication number	US-10639618-B2
Application number	US-201816235932-A
Country	US
Kind code	B2
Filing date	Dec 28, 2018
Priority date	Dec 29, 2017
Publication date	May 5, 2020
Grant date	May 5, 2020

Abstract

A method of wax oil hydrocracking includes the steps of pre-hydrotreating wax oil to obtain a pre-hydrotreated material flow; controlling the pre-hydrotreated material flow and a hydrogen-containing material flow to contact with a first hydrocracking catalyst to obtain a first hydrocracked material flow, and dividing the first hydrocracked material flow into a first hydrocracked material flow A and a first hydrocracked material flow B; controlling the flow B and a hydrogen-containing material flow to contact with a second hydrocracking catalyst to obtain a second hydrocracked material flow, and then separating and fractionating the second hydrocracked material flow to obtain a hydrocracked tail oil product; controlling the flow A, at least a part of the hydrocracked tail oil product, and a hydrogen-containing material flow to contact with a hydrogenation isocracking catalyst to obtain a hydrogenation isocracked material flow, and then separating and fractionating the obtained hydrogenation isocracked material flow.

First claim

The invention claimed is:

1. A wax oil hydrocracking method, comprising:
(1) contacting wax oil and a hydrogen-containing material flow with a pre-hydrotreating catalyst under pre-hydrotreating conditions to obtain a pre-hydrotreated material flow;
(2) contacting the pre-hydrotreated material flow and a hydrogen-containing material flow with a first hydrocracking catalyst to perform a first hydrocracking reaction under first hydrocracking conditions to obtain a first hydrocracked material flow, and dividing the first hydrocracked material flow into flow A and flow B;
(3) contacting flow B and a hydrogen-containing material flow with a second hydrocracking catalyst to perform a second hydrocracking reaction under second hydrocracking conditions to obtain a second hydrocracked material flow, and then separating and fractionating the second hydrocracked material flow to obtain a hydrocracked tail oil product; and
(4) contacting flow A, at least a part of the hydrocracked tail oil product, and a hydrogen-containing material flow with a hydrogenation isocracking catalyst to perform a hydrogenation isocracking reaction under hydrogenation isocracking conditions to obtain a hydrogenation isocracked material flow, and then separating and fractionating the hydrogenation isocracked material flow.

2. The method according to claim 1 , wherein flow A accounts for 5-95 wt % of the wax oil.

3. The method according to claim 2 , wherein flow A accounts for 10-80 wt % of the wax oil.

4. The method according to claim 1 , wherein the method further comprising: separating flow A by gas-liquid separation to obtain a first hydrocracked gas-phase material flow and a first hydrocracked liquid-phase material flow; introducing the first hydrocracked gas-phase material flow into the step (3) to carry out the second hydrocracking reaction; contacting the first hydrocracked liquid-phase material flow, at least a part of the hydrocracked tail oil product and the hydrogen-containing material flow with the hydrogenation isocracking catalyst in the step (4) to carry out the hydrogenation isocracking reaction;
the first hydrocracked liquid-phase material flow accounts for 5-95 wt % of the wax oil.

5. The method according to claim 4 , wherein the first hydrocracked liquid-phase material flow accounts for 10-80 wt % of the wax oil.

6. The method according to claim 1 , wherein a hydrocracked hydrogen-rich gas, a hydrocracked gas product, a hydrocracked naphtha product, a hydrocracked jet fuel product, a hydrocracked diesel oil product, and the hydrocracked tail oil product are obtained through the separation and fractionation in the step (3);
a hydrogenation isocracked hydrogen-rich gas, a hydrogenation isocracked gas product, a hydrogenation isocracked naphtha product, a hydrogenation isocracked jet fuel product, a hydrogenation isocracked diesel oil product, and a hydrogenation isocracked tail oil product are obtained through the separation and fractionation in the step (4).

7. The method according to claim 6 , wherein the separation in the step (3) comprises high-pressure separation and low-pressure separation, the second hydrocracked material flow is separated by high-pressure separation to obtain a hydrocracked hydrogen-rich gas and a hydrocracked high-pressure separated liquid-phase material flow, then the hydrocracked high-pressure separated liquid-phase material flow is separated by low-pressure separation to obtain a hydrocracked gas product and a hydrocracked liquid-phase material flow, the hydrocracked liquid-phase material flow is fractionated to obtain a hydrocracked naphtha product, a hydrocracked jet fuel product, a hydrocracked diesel oil product, and the hydrocracked tail oil product;
the separation in the step (4) comprises high-pressure separation and low-pressure separation, the hydrogenation isocracked material flow is separated by high-pressure separation to obtain a hydrogenation isocracked hydrogen-rich gas and a hydrogenation isocracked high-pressure separated liquid-phase material flow, and then the hydrogenation isocracked high-pressure separated liquid-phase material flow is separated by low-pressure separation to obtain a hydrogenation isocracked gas product and a hydrogenation isocracked liquid-phase material flow, the hydrogenation isocracked liquid-phase material flow is fractionated to obtain a hydrogenation isocracked naphtha product, a hydrogenation isocracked jet fuel product, a hydrogenation isocracked diesel oil product, and a hydrogenation isocracked tail oil product;
the method further comprises: recycling the hydrocracked hydrogen-rich gas and the hydrogenation isocracked hydrogen-rich gas to provide required hydrogen-containing material flow.

8. The method according to claim 1 , wherein an initial boiling point of the wax oil is 100-400° C., and a final boiling point of the wax oil is 405-650° C.;
the wax oil is selected from at least one of vacuum gas oil (VGO), coker gas oil (CGO), deasphalted oil (DAO), catalytic cycle oil, coal tar, direct coal liquefaction distillate (DCLD), indirect coal liquefaction distillate (ICLD), synthetic oil, and shale oil;
wherein an initial boiling point of the hydrocracked tail oil product is 300-375° C.

9. The method according to claim 1 , wherein the pre-hydrotreating catalyst contains a carrier and an active component, wherein, the active component is one or more VIB metal, one or more VIII metal, or mixtures thereof, and the carrier is alumina, silicon-containing alumina, or a mixture thereof;
wherein, based on the total weight of the pre-hydrotreating catalyst and measured in oxide, a content of the VIB metal element is 10-35 wt %, and a content of the VIII metal element is 3-15 wt %;
a specific surface area of the pre-hydrotreating catalyst is 100-650 m 2 /g, and a pore volume of the pre-hydrotreating catalyst is 0.15-0.6 mL/g.

10. The method according to claim 1 , wherein the pre-hydrotreating conditions include: reaction pressure: 3-19 MPa, reaction temperature: 300-450° C., liquid hourly space velocity: 0.2-6 h −1 , and volume ratio of hydrogen to oil: 100-2,000:1.

11. The method according to claim 1 , wherein the first hydrocracking catalyst and the second hydrocracking catalyst respectively and independently contain a carrier and an active constituent, wherein, the active constituent is one or more VIB metal, one or more VIII metal, or mixtures thereof, and the carrier contains a Y zeolite;
based on a total weight of the first hydrocracking catalyst and measured in oxide, a content of the VIB metal is 10-35 wt %, and a content of the VIII metal is 3-15 wt %;
the content of the Y zeolite is 5-80 wt %;
based on a total weight of the second hydrocracking catalyst and measured in oxide, a content of the VIB metal is 10-35 wt %, and a content of the VIII metal is 3-15 wt %; and a content of the Y zeolite is 5-80 wt %.

12. The method according to claim 1 , wherein the first hydrocracking conditions and the second hydrocracking conditions respectively and independently include: reaction pressure: a pressure of 3-19 MPa, a reaction temperature of 300-450° C., a liquid hourly space velocity of 0.2-6 h −1 , and a volume ratio of hydrogen to oil is 100to 2,000.

13. The method according to claim 1 , wherein the hydrocracked tail oil product in the step (4) accounts for 10-100 wt % of the hydrocracked tail oil product obtained in the step (3).

14. The method according to claim 1 , wherein the hydrogenation isocracking catalyst contains a carrier and an active constituent, wherein, the active constituent is one or more of VIB metal, one or more of VIII metal, or mixtures thereof, and the carrier

Assignees

• China Petroleum & Chem Corp
• Dalian Res Institute Of Petroleum And Petrochemicals Sinopec Corp

Inventors

• Liu Tao
• Li Baozhong
• Zeng Ronghui
• Zhao Yuzhuo
• Bai Zhenmin
• Fang Xiangchen
• Wang Yan
• Zhang Xuehui
• Liu Chang

Classifications

• C10G45/58

  to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins (C10G32/00 takes precedence; improving or increasing the octane number or aromatic content of naphtha C10G35/00) · CPC title

• C10G65/14

  plural parallel stages only · CPC title

• B01J29/80

  Mixtures of different zeolites · CPC title

• B01J2229/36

  Steaming · CPC title

• C10G65/12

  including cracking steps and other hydrotreatment steps · CPC title