Methods and systems for increasing production of middle distillate hydrocarbons from heavy hydrocarbon feed during fluid catalytic cracking

Patent metadata

Field	Value
Publication number	US-9816037-B2
Application number	US-201414493207-A
Country	US
Kind code	B2
Filing date	Sep 22, 2014
Priority date	Sep 22, 2014
Publication date	Nov 14, 2017
Grant date	Nov 14, 2017

Abstract

A method is provided for increasing production of middle distillate hydrocarbons from conversion of a heavy hydrocarbon feed in a fluid catalytic cracking system having a primary riser and a secondary riser, wherein the method comprises providing regenerated catalyst to the primary riser and operating the primary riser under severe conditions and providing spent catalyst to the secondary riser and operating the secondary riser under moderate conditions.

First claim

What is claimed is:

1. A method for fluid catalytic cracking, said method comprising the steps of:
contacting at least a portion of a heavy hydrocarbon feed with a fluidized regenerated catalyst in a primary riser to produce a primary cracked product that comprises primary spent catalyst;
separating the primary cracked product into the primary spent catalyst and a substantially catalyst-free primary cracked product;
contacting an intermediate hydrocarbon feed with a fluidized spent catalyst in a secondary riser to produce a secondary cracked product comprising secondary spent catalyst, wherein the intermediate hydrocarbon feed comprises: at least a portion of the substantially catalyst-free primary cracked product, at least a portion of the heavy hydrocarbon feed, at least a portion of a different heavy hydrocarbon feed than is used in the primary riser, or combinations thereof;
separating the secondary cracked product into the secondary spent catalyst and a substantially catalyst-free secondary product comprising middle distillates;
providing regenerated catalyst to the primary riser; and
providing spent catalyst to the secondary riser, wherein the spent catalyst comprises both the secondary spent catalyst and the primary spent catalyst.

2. The method of claim 1 , further comprising:
contacting at least a portion of the primary spent catalyst with an oxygen-containing gas to produce primary regenerated catalyst; and
contacting at least a portion of the secondary spent catalyst with an oxygen containing gas to produce secondary regenerated catalyst,
wherein the regenerated catalyst provided to the primary riser comprises at least a portion of the primary regenerated catalyst, or at least a portion of the secondary regenerated catalyst, or both; and
wherein the spent catalyst provided to the secondary riser comprises at least a portion of the primary spent catalyst, or at least a portion of the secondary spent catalyst, or both.

3. The method of claim 2 , wherein the steps of contacting at least a portion of the primary and secondary spent catalysts, respectively, with an oxygen-containing gas are performed concurrently in the same apparatus.

4. The method of claim 1 , wherein the heavy hydrocarbon feed has a boiling point of about 500° F. (260° C.) or greater, and comprises primarily C18 and higher hydrocarbons.

5. The method of claim 4 , wherein the heavy hydrocarbon feed comprises: vacuum gas oil, or heavy cycle oil, or both.

6. The method of claim 1 , wherein the regenerated catalyst, primary spent catalyst and secondary spent catalyst each, independently, comprise a large pore molecular sieve having pore openings of greater than about 0.7 nm in effective diameter.

7. The method of claim 6 , wherein the large pore molecular sieve comprises a synthetic X-type or Y-type material chosen from: zeolite, mordenite, faujasite and combinations thereof.

8. The method of claim 1 , wherein only spent catalyst is provided to the secondary riser for contacting the intermediate hydrocarbon feed therein.

9. The method of claim 1 , wherein the contacting steps are performed to achieve a conversion rate in a range of from about 10% to no more than about 60%.

10. The method of claim 1 , wherein the intermediate hydrocarbon feed further comprises at least a portion of the substantially catalyst-free secondary cracked product.

11. The method of claim 1 , wherein the steps of separating the primary and secondary cracked product are performed concurrently in the same apparatus to provide a spent catalyst comprising at least portions of each of the primary and secondary spent catalysts;
and a substantially catalyst-free product comprising at least a portion of each of the primary and secondary cracked product and comprising middle distillates in an amount of from about 14 to about 26 percent, by volume (vol %), based on the total volume of the combined substantially catalyst-free product gas.

12. The method of claim 1 , further comprising the step of fractionating at least a portion of the substantially catalyst-free primary cracked product, at least a portion of the substantially catalyst-free secondary cracked product, or both, to produce the middle distillates.

13. The method of claim 1 , further comprising fractionating a cracked product feed stream to produce the middle distillates, wherein the cracked product feed stream comprises: at least a portion of the substantially catalyst-free primary cracked primary product, at least a portion of the substantially catalyst-free secondary cracked product, or both.

14. The method of claim 13 , wherein the middle distillates comprise primarily C8-C23 hydrocarbons having a boiling point of from about 149 to about 371° C. (about 300 to about 700° F.).

15. The method of claim 1 , wherein the step of contacting at least a portion of a heavy hydrocarbon feed with a fluidized regenerated catalyst in the primary riser is performed under severe operating conditions comprising a cracking temperature of from about 482 to about 593° C. (about 900 to about 1100° F.).

16. The method of claim 1 , wherein the step of contacting an intermediate hydrocarbon feed with a fluidized spent catalyst in the secondary riser is performed under moderate operating conditions comprising a cracking temperature of from about 482 to about 593° C. (about 900 to about 1100° F.).

17. The method of claim 1 , wherein each of the primary and secondary spent catalysts provided by the separation steps has adsorbed hydrocarbons thereon, said method further comprising removing at least a portion of the adsorbed hydrocarbons from the primary spent catalyst, or from the secondary spent catalyst, or from both.

18. The method of claim 17 , wherein the step of removing at least a portion of the adsorbed hydrocarbons comprises removing at least a portion of the adsorbed hydrocarbons from the primary spent catalyst and from the secondary spent catalyst concurrently in the same apparatus.

19. A method for fluid catalytic cracking, said method comprising the steps of:
contacting at least a portion of a heavy hydrocarbon feed with a fluidized regenerated catalyst in a primary riser to produce a primary cracked product comprising primary spent catalyst;
contacting an intermediate hydrocarbon feed with a fluidized spent catalyst in a secondary riser to produce a secondary cracked product comprising secondary spent catalyst;
combining said primary cracked product and said secondary cracked product to form a combined cracked product comprising spent catalyst;
separating the combined cracked product into spent catalyst and a substantially catalyst-free cracked product comprising middle distillates;
providing a portion of the spent catalyst to the secondary riser;
contacting a different portion of the spent catalyst with an oxygen-containing gas to produce regenerated catalyst; and
providing regenerated catalyst to the primary riser.

Assignees

• Uop Llc

Inventors

• Avais Fariha

Classifications

• C10G51/026 Primary

  only catalytic cracking steps · CPC title

• B01J8/28

  the one above the other · CPC title

• C10G11/182

  Regeneration · CPC title

• C10G11/187

  Controlling or regulating · CPC title

• B01J2208/00796

  Details of the reactor or of the particulate material · CPC title