Combined process of hydrotreating and catalytic cracking of hydrocarbon oils

Patent metadata

Field	Value
Publication number	US-9260667-B2
Application number	US-201213618759-A
Country	US
Kind code	B2
Filing date	Sep 14, 2012
Priority date	Dec 20, 2007
Publication date	Feb 16, 2016
Grant date	Feb 16, 2016

Abstract

Disclosed is a combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils, including: contacting residual oil, catalytic cracking cycle oil, and optional distillate oil with a hydrotreating catalyst under hydrotreating conditions in the presence of hydrogen followed by separation of the reaction products to obtain hydrogenated tail oil and other products; contacting the hydrogenated tail oil and optional normal catalytic cracking feedstock oil with a cracking catalyst under catalytic cracking conditions followed by separation of the reaction products; wherein the hydrogenated tail oil and/or normal catalytic cracking feedstock oil are separated into at least two fractions prior to contacting the hydrogenated tail oil and/or normal catalytic cracking feedstock oil with the cracking catalyst.

First claim

What is claimed is:

1. An improved combined method of hydrotreating and catalytic cracking of hydrocarbon oil, comprising:
contacting residual oil, catalytic cracking cycle oil, and optional distillate oil with a hydrotreating catalyst under hydrotreating conditions in the presence of hydrogen followed by separation of the reaction products to obtain gas, hydrogenated naphtha, hydrogenated diesel oil, and hydrogenated tail oil;
contacting the hydrogenated tail oil and normal catalytic cracking feedstock oil with a catalytic cracking catalyst under catalytic cracking conditions followed by separation of the reaction products to obtain dry gas, liquefied petroleum gas, catalytically cracked gasoline, catalytically cracked diesel oil, and catalytic cracking cycle oil;
wherein
the catalytic cracking cycle oil comprises less than 30 wtppm of solid particles, and the size of the solid particles being less than 10 μm;
the contact reaction with the cracking catalyst is carried out in a reactor having at least two reaction zones I and II along the flow direction of reactants;
prior to contacting the hydrogenated tail oil and the normal catalytic cracking feedstock oil with the cracking catalyst, at least a portion of the normal catalytic cracking feedstock oil is separated into normal catalytic cracking heavy feedstock oil and normal catalytic cracking light feedstock oil, and the hydrogenated tail oil is optionally separated into at least two fractions, the light and the heavy fractions of the hydrogenated tail oil, wherein the normal catalytic cracking heavy feedstock oil and the optionally separated heavy fraction of the hydrogenated tail oil have a boiling point above 500° C., and the normal catalytic cracking light feedstock oil and the optionally separated light fraction of the hydrogenated tail oil have a distillation range of 350˜500° C.,
wherein the contact reaction with the cracking catalyst comprises:
(i) charging the reaction zone I with one of normal catalytic cracking heavy feedstock oil and normal catalytic cracking light feedstock oil, optionally with unseparated normal catalytic cracking feedstock oil; whereas charging the reaction zone II with the other of normal catalytic cracking heavy feedstock oil and normal catalytic cracking light feedstock oil, optionally with unseparated normal catalytic cracking feedstock oil, and
(ii) prior to the contact reaction, combining at least one of the normal catalytic cracking heavy feedstock oil and the normal catalytic cracking light feedstock oil with at least one feed chosen from unseparated hydrogenated tail oil, the light fraction of the hydrogenated tail, and the heavy fraction of the hydrogenated tail oil.

2. The method according to claim 1 , wherein said contact reaction with catalytic cracking catalysts is carried out by charging the reaction zone I with normal catalytic cracking heavy feedstock oil and unseparated hydrogenated tail oil, whereas charging the reaction zone II with said normal catalytic cracking light feedstock oil.

3. The method according to claim 2 , wherein the amount of hydrogenated tail oil is no more than 90% by weight, based on the mixed feedstock of normal catalytic cracking heavy feedstock oil and unseparated hydrogenated tail oil.

4. The method according to claim 2 , wherein the reaction conditions in the reaction zone I are as follows: a reaction temperature of 550-700° C., a catalyst to oil ratio of 4-20, a reaction time of 0.5-10 seconds, an amount of 2-50 wt % of atomized water steam in the feedstock, and a reaction pressure of from normal pressure to 300 kPa; the reaction conditions in the reaction zone H are as follows: a reaction temperature of 500-600° C., a catalyst to oil ratio of 7-50, a reaction time of 0.2-8 seconds, an amount of 2-20 wt % of atomized water steam in the feedstock, and a reaction pressure of from normal pressure to 300 kPa.

5. The method according to claim 2 , wherein the reaction conditions in the reaction zone I are as follows: a reaction temperature of 560-650° C., a catalyst to oil ratio of 5-16, a reaction time of 1-2 seconds, an amount of 5-10 wt % of atomized water steam in the feedstock, and a reaction pressure of 100-300 kPa; the reaction conditions in the reaction zone II are as follows: a reaction temperature of 510-560° C., a catalyst to oil ratio of 8-40, a reaction time of 0.5-1.5 seconds, an amount of 4-8 wt % of atomized water steam in the feedstock, and a reaction pressure of 100-300 kPa.

6. The method according to claim 1 , wherein said contact reaction with catalytic cracking catalysts is carried out by charging the reaction zone I with said normal catalytic cracking heavy feedstock oil and optionally with unseparated normal catalytic cracking feedstock oil, whereas charging the reaction zone II with said normal catalytic cracking light feedstock oil and unseparated hydrogenated tail oil.

7. The method according to claim 6 , wherein the amount of hydrogenated tail oil is no more than 50% by weight, based on the mixed feedstock of said normal catalytic cracking light feedstock oil and unseparated hydrogenated tail oil.

8. The method according to claim 6 , wherein the reaction conditions in the reaction zone I are as follows: a reaction temperature of 550-700° C., a catalyst to oil ratio of 4-20, a reaction time of 0.5-10 seconds, an amount of 2-50 wt % of atomized water steam in the feedstock, and a reaction pressure of from normal pressure to 300 kPa; the reaction conditions in the reaction zone II are as follows: a reaction temperature of 500-600° C., a catalyst to oil ratio of 7-50, a reaction time of 0.2-8 seconds, an amount of 2-20 wt % of atomized water steam in the feedstock, and a reaction pressure of from normal pressure to 300 kPa.

9. The method according to claim 6 , wherein the reaction conditions in the reaction zone I are as follows: a reaction temperature of 560-650° C., a catalyst to oil ratio of 5-16, a reaction time of 1-1.5 seconds, an amount of 5-10wt % of atomized water steam in the feedstock, and a reaction pressure of 100-300 kPa; the reaction conditions in the reaction zone 11 are as follows: a reaction temperature of 520-560° C., a catalyst to oil ratio of 8-40, a reaction time of 1-2 seconds, an amount of 4-8 wt % of atomized water steam in the feedstock, and a reaction pressure of 100-300 kPa.

10. The method according to claim 1 , wherein regenerated catalysts may be introduced into said reaction zone II.

11. The method according to claim 1 , wherein a delivery device for regenerated catalysts is provided between said reaction zone II and a cracking catalyst regenerator.

12. The method according to claim 11 , wherein the delivery device for regenerated catalysts is equipped at a position of the reaction zone II such that the residence time of hydrocarbon oils in the reaction zone II is not less than 0.2 second.

13. The method according to claim 12 , wherein the delivery device for regenerated catalysts is equipped at a position of the reaction zone H such that the residence time of hydrocarbon oils in the reaction zone II is not less than 1 second.

14. The method according to claim 1 , wherein the content of said solid particles in the catalytic cracking cycle oil is less than 15 wtppm, and the particle size of said solid particles is less than 5 μm.

15. The method according to claim 1 , wherein the step of removing cracking catalyst particles from catalytic cracking cycle oil is carried out by distillation and/or filtering.

16. The method according to claim 15 , wherein the operation temperature is 100˜350° C. during said filtering.

Assignees

• Gao Yongcan
• Xie Chaogang
• Niu Chuanfeng
• Zhang Jiushun
• Dai Lishun
• Nie Hong
• Li Dadong
• Long Jun
• Ma Jianguo
• Cui Yan
• China Petroleum & Chemical
• Res Inst Petroleum Processing

Inventors

• Gao Yongcan
• Xie Chaogang
• Niu Chuanfeng
• Zhang Jiushun
• Dai Lishun
• Nie Hong
• Li Dadong
• Long Jun
• Ma Jianguo
• Cui Yan

Classifications

• C10G2300/301

  Boiling range · CPC title

• C10G2300/70

  Catalyst aspects · CPC title

• C10G2300/4012

  Pressure · CPC title

• C10G2300/807

  Steam · CPC title

• C10G11/18 Primary

  according to the "fluidised-bed" technique · CPC title