Conversion of a crude oil in a fluidized bed comprising zones with different contact times

Patent metadata

Field	Value
Publication number	US-11839872-B2
Application number	US-201917415920-A
Country	US
Kind code	B2
Filing date	Dec 13, 2019
Priority date	Dec 19, 2018
Publication date	Dec 12, 2023
Grant date	Dec 12, 2023

Abstract

The present invention relates to a device and to a process for the fluidized bed catalytic cracking of a hydrocarbon feedstock, in which: a first feedstock ( 2 ) is cracked in a dense fluidized bed reactor ( 1 ) in the presence of a catalyst ( 3 ) to produce a first effluent; and at least one second feedstock ( 10 ) is cracked in a transport fluidized bed reactor ( 4 ) in the presence of the catalyst ( 3 ) supplied by the dense fluidized bed reactor ( 1 ) to produce a second effluent, the second feedstock ( 10 ) being a heavier feedstock than the first feedstock ( 2 ).

First claim

The invention claimed is:

1. A device capable of fluidized bed catalytic cracking of a hydrocarbon feedstock, said device comprising: a dense fluidized bed reactor ( 1 ) suitable for at least partially cracking a first hydrocarbon feedstock ( 2 ) in the presence of a catalyst ( 3 ) to produce a first effluent, reactor ( 1 ) being adapted to operate with a gas velocity between minimum fluidization velocity and transportation velocity, reactor ( 1 ) and at least partially feeding with catalyst ( 3 ) a transport fluidized bed reactor ( 4 ); and
the transport fluidized bed reactor ( 4 ) suitable for at least partially cracking at least one second hydrocarbon feedstock ( 10 ) in the presence of the catalyst ( 3 ) to produce a second effluent, reactor ( 4 ) being adapted to operate with a gas velocity greater than the transportation velocity, the second hydrocarbon feedstock ( 10 ) being a heavier feedstock than the first hydrocarbon feedstock ( 2 ).

2. The device as claimed in claim 1 , wherein the dense fluidized bed reactor ( 1 ) is directly connected to the transport fluidized bed reactor ( 4 ) in order to directly feed the transport fluidized bed reactor ( 4 ) with catalyst ( 3 ).

3. The device as claimed in claim 1 , wherein the dense fluidized bed reactor ( 1 ) is an ebullating or turbulent fluidized bed reactor.

4. The device as claimed in claim 1 , wherein the transport fluidized bed reactor ( 4 ) is an upward or downward gas-solid cocurrentwise fluidized bed reactor.

5. The device as claimed in claim 1 , wherein the transport fluidized bed reactor ( 4 ) is an upward gas-solid cocurrentwise fluidized bed reactor.

6. The device as claimed in claim 1 , wherein the dense fluidized bed reactor ( 1 ) is connected to an intermediate feedstock inlet of the transport fluidized bed reactor ( 4 ).

7. The device as claimed in claim 1 , wherein the dense fluidized bed reactor ( 1 ) comprises at least two compartments ( 14 A, 14 B; 17 A, 17 B) for treating the first hydrocarbon feedstock ( 2 ) in the form of at least one first lighter feedstock ( 2 A) and one first less light feedstock ( 2 B), and in which: either a first compartment ( 17 A) is fed with a first catalyst ( 3 A) and a second compartment ( 17 B) fed with a second catalyst ( 3 B); or a first compartment ( 14 A) is fed with the catalyst resulting directly from a regenerator and a second compartment ( 14 B) is fed with catalyst by movement between the first compartment ( 14 A) and the second compartment ( 14 B).

8. A process for the fluidized bed catalytic cracking of a hydrocarbon feedstock, comprising:
at least partially cracking a first hydrocarbon feedstock ( 2 ) in a dense fluidized bed reactor ( 1 ) in the presence of a catalyst ( 3 ) to produce a first effluent;
feeding with catalyst ( 3 ) a transport fluidized bed reactor ( 4 ) at least partially from the dense fluidized bed reactor ( 1 ); and
at least partially cracking at least one second hydrocarbon feedstock ( 10 ) in the transport fluidized bed reactor ( 4 ) in the presence of the catalyst ( 3 ) to produce a second effluent;
the second hydrocarbon feedstock ( 10 ) being a heavier feedstock than the first hydrocarbon feedstock ( 2 ), said reactor ( 1 ) being adapted to operate with a gas velocity between minimum fluidization velocity and transportation velocity, reactor ( 1 ) and at least partially feeding with catalyst ( 3 ) a transport fluidized bed reactor ( 4 ); and the transport fluidized bed reactor ( 4 ) being adapted to operate with a gas velocity greater than the transportation velocity, the second hydrocarbon feedstock ( 10 ) being a heavier feedstock than the first hydrocarbon feedstock ( 2 ).

9. The process as claimed in claim 8 , in which the dense fluidized bed reactor ( 1 ) is directly connected to the transport fluidized bed reactor ( 4 ) in order to directly feed the transport fluidized bed reactor ( 4 ) with catalyst ( 3 ).

10. The process as claimed in claim 8 , in which the effluent from the dense fluidized bed reactor ( 1 ) is an ebullating or turbulent fluidized bed reactor.

11. The process as claimed in claim 8 , in which the transport fluidized bed reactor ( 4 ) is an upward or downward gas-solid cocurrentwise fluidized bed reactor.

12. The process as claimed in claim 8 , in which the transport fluidized bed reactor ( 4 ) is an upward gas-solid cocurrentwise fluidized bed reactor.

13. The process as claimed in claim 8 , in which the dense fluidized bed reactor ( 1 ) is connected to an intermediate feedstock inlet of the transport fluidized bed reactor ( 4 ).

14. The process as claimed in claim 8 , in which the dense fluidized bed reactor ( 1 ) comprises at least two compartments ( 14 A, 14 B; 17 A, 17 B) for treating the first hydrocarbon feedstock ( 2 ) in the form of at least one first lighter feedstock ( 2 A) and one first less light feedstock ( 2 B), and in which: either a first compartment ( 17 A) is fed with a first catalyst ( 3 A) and a second compartment ( 17 B) fed with a second catalyst ( 3 B); or a first compartment ( 14 A) is fed with the catalyst resulting directly from a regenerator and a second compartment ( 14 B) is fed with catalyst by movement between the first compartment ( 14 A) and the second compartment ( 14 B).

15. The process as claimed in claim 8 , in which the operating conditions of the dense fluidized bed reactor ( 1 ) are as follows:
superficial gas velocity: between 0.2 and 2 m/s;
temperature: between 500 and 800° C. and preferably less than 750° C.;
pressure: between 0.1 and 0.6 MPaa; and
contact time of greater than 1 second, and/or

the operating conditions of the transport fluidized bed reactor ( 4 ) are as follows:
superficial gas velocity: between 3 and 30 m/s;
temperature: between 500 and 700° C. and preferably less than 650° C.;
pressure: between 0.1 and 0.6 MPaa;
contact time of less than 1 second; and
C/O: between 3 and 50.

Assignees

• Ifp Energies Now

Inventors

• Cloupet Ann
• Raynal Ludovic

Classifications

• B01J8/1863 Primary

  followed by a downward movement outside the reactor and subsequently re-entering it · CPC title

• B01J8/1872

  Details of the fluidised bed reactor (B01J8/1836 takes precedence) · CPC title

• B01J8/28

  the one above the other · CPC title

• B01J8/388

  externally, i.e. the particles leaving the vessel and subsequently re-entering it · CPC title

• C10G11/16

  according to the "moving bed" method · CPC title