Ultra-short contact time fluidized catalytic cracking process

• US 4,985,136 A
• Filed: 11/05/1987
• Issued: 01/15/1991
• Est. Priority Date: 11/05/1987
• Status: Expired due to Term

• Current Assignee: David B. Bartholic
• Original Assignee: David B. Bartholic
• Inventors: Bartholic, David B.
• Primary Examiner(s): MYERS, HELANE ELEANORA
• Application Number:
  US07/116,910
• Time in Patent Office: 1,167 Days
• Field of Search: 208/113, 208/118, 208/120, 208/153, 208/154, 208/157, 208/161, 208/163, 208/176, 208/146, 208/160, 208/168, 422/145, 422/147, 422/139
• US Class Current: 208/153
• CPC Class Codes: B01J 8/085 Feeding reactive fluids for solid material, see B01J8/0015
• CPC Class Codes: B01J 8/12 moved by gravity in a downward flow
• CPC Class Codes: C10G 11/16 according to the "moving bed" method
• CPC Class Codes: C10G 11/18 according to the "fluidised-bed" technique

Abstract

A fluid catalytic cracking process wherein a hydrocarbon charge-stock is atomized and injected, in a contactor/reactor, into a vertical curtain of hot regenerated catalyst to vaporize and crack hydrocarbons in the charge-stock, wherein the catalyst preferably contains at least 40% by weight of a zeolitic cracking component and the contact time of the hydrocarbon vapors and the catalyst in the contactor/reactor is ultra-short, preferably not greater than 0.5 second.

Claims

1. A fluidized process for the conversion of a hydrocarbon oil charge stock to lower molecular weight liquid product comprising:

(a) atomizing a primary charge-stock to provide a stream of liquid particles of a preselected size;

(b) introducing said atomized primary charge-stock substantially horizontally into a primary reaction zone;

(c) introducing a stream of hot fluidized cracking catalyst particles mixed with gaseous dispersion media downwardly into said reaction zone at a velocity greater than 10 feet per second to intimately contact said atomized primary charge-stock therein, the temperature, pressure and contact time with said atomized primary charge-stock being sufficient to vaporize hydrocarbons in said charge-stock and to crack the hydrocarbons to lower molecular weight product;

(d) vaporizing a substantial portion of said hydrocarbons to form a mixture of said catalyst particles in the resulting vaporized hydrocarbons and cracking said vaporized hydrocarbons in said reaction zone to form cracked product vapors and spent catalyst;

(e) rapidly passing a mixture of the resulting cracked product vapors, said media and a majority of said spent catalyst particles substantially horizontally through said reaction zone and into a reactor separation zone to provided a hydrocarbon/catalyst contact time prior to passage into said separation zone of not greater than 0.5 second and separating spent catalyst particles from said cracked product, said spent catalyst particles containing deposit of carbonaceous material thereon which reduce the cracking activity of said catalyst;

(f) passing said spent catalyst particles to a combustion zone;

(g) contacting said spent catalyst with an oxygen-containing gas in said combustion zone to burn said carbonaceous deposits and to provide a regenerated catalyst and a flue gas;

(h) recycling the resulting hot, regenerated catalyst to said reaction zone to contact fresh atomized charge-stock; and

(i) recovering a hydrocarbon product having a molecular weight lower than said charge stock.

2. The process of claim 1, wherein said catalyst is fresh catalyst containing at least 40% by weight of a zeolitic component having substantial cracking activity.

3. The process of claim 1, wherein said primary charge-stock is selected from the group consisting of residual oil, gas oil and tar sand bitumen.

4. The process of claim 1, wherein said flue gas is mixed with an oxygen-containing gas to provide a fluidizing media, said fluidizing media is introduced into the said combustion zone near the bottom thereof to fluidize the catalyst particles therein and oxidize said carbonaceous deposits, and wherein the flow rate and oxygen content of said fluidizing media supplied to said combustion zone are controlled in response to a signal representative of the amount of oxygen in said flue gas to obtain the desired amount of burning in said combustion zone.

5. The process of claim 4, wherein said combustion zone has an upper section and a lower section, the diameter of said lower section being greater than that of said upper section, and the velocity of said fluidizing media and spent catalyst particles in said lower section is less than the velocity thereof in said upper section.

6. The process of claim 1, wherein said cracked product is passed to a product fractionation zone, hydrocarbon gas from said fractionation zone is mixed with said hot, regenerated catalyst, the resulting mixture is introduced into said primary reaction zone and wherein the flow rate of said hydrocarbon gas is adjusted to control the contact time of said catalyst with said hydrocarbons in said primary reaction zone.

7. The process of claim 6, wherein the temperature and flow rate of said mixture of hydrocarbon gas and regenerated catalyst introduced into said primary reaction zone are measured, the flow rate of said charge-stock introduced into said primary reaction zone is measured, the amount of heat required to vaporize and crack hydrocarbons in said charge-stock is determined relative to the amount of heat in said mixture and the flow rate of said charge-stock is adjusted in response to said determined amount of heat.

8. The process of claim 1, wherein said spent catalyst is passed to a stripping zone and hydrocarbons are stripped therefrom prior to passing the spent catalyst to said combustion zone.

9. The process of claim 8, wherein a portion of said hot, regenerated catalyst is passed to said stripping zone to increase the temperature therein.

10. The process of claim 1, wherein said mixture of cracked product vapors and entrained spent catalyst particles are separated in at least a primary reactor separation zone and a secondary reactor separation zone, and a portion of said hot, regenerated catalyst is added to the cracked product vapors between said primary and secondary separation zones to increase the temperature of said cracked product vapors prior to entry into said secondary separation zone.

11. The process of claim 10, wherein the increase in the temperature of said cracked product vapors is at least 5°

F.

12. The process of claim 1, further including contacting at least a secondary charge stock requiring a different severity of operation than said primary charge-stock to produce the desired product with said catalyst.

13. The process of claim 12, wherein said primary charge stock is a gas-oil and said secondary charge-stock is a residual oil, said spent catalyst is passed to a stripping zone for stripping hydrocarbons therefrom, a catalyst bed level being maintained in said stripping zone, and said residual oil is atomized and injected onto the top of said bed level and into a stream of hot, regenerated catalyst particles introduced substantially vertically into a secondary reaction zone located apart from said primary reaction zone.

14. The process of claim 8, wherein said hot fluidized cracking catalyst particles are introduced downwardly into said reaction zone, said stripping zone is positioned below said reaction zone, a portion of said spent catalyst particles drop from said reaction zone into said stripping zone, and spent catalyst particles are passed from said stripping zone into said combustion zone.

15. A fluidized process for the conversion of a hydrocarbon oil charge-stock to lower molecular weight liquid product comprising:

(a) introducing a hydrocarbon oil charge-stock into a reaction zone;

(b) introducing a mixture of hot fluidized particles of a cracking catalyst containing at least 40% by weight of a zeolitic component having a substantial cracking activity mixed with a gaseous dispersion media into said reaction zone in a first downward direction and at a velocity greater than 10 feet per second to intimately contact said charge-stock therein, the temperature, pressure and contact time with said primary charge-stock in said reaction zone being sufficient to vaporize hydrocarbons in said charge-stock and to crack the hydrocarbons to lower molecular weight cracked product;

(c) vaporizing a substantial portion of said hydrocarbons to form a mixture of said catalyst particles in the resulting vaporized hydrocarbons and cracking said vaporized hydrocarbons in said reaction zone to form cracked product vapors and spent catalyst;

(d) rapidly passing a mixture of the resulting cracked product vapors, said media and a majority of said spent catalyst particles through said reaction zone in a second direction substantially transverse to said first direction and into a reactor separation zone and separating spent catalyst particles from said cracked product, the hydrocarbon/catalyst contact time in said reaction zone prior to passage into said separation zone being not greater than 0.5 second, while a portion of said spent catalyst particles settles into a catalyst stripping zone positioned below said reaction zone; and

(e) recovering a hydrocarbon product having a molecular weight lower than said charge stock.

16. The process of claim 15, wherein said catalyst is fresh catalyst.

17. The process of claim 15, wherein said charge stock is introduced substantially horizontally into said reaction zone.

18. The process of claim 15, wherein said charge stock is atomized to provide a stream of liquid particles of a preselected size and the atomized charge stock is introduced into said reaction zone.