Direct dry gas recovery from FCC reactor

• US 5,360,533 A
• Filed: 06/08/1993
• Issued: 11/01/1994
• Est. Priority Date: 06/08/1993
• Status: Expired due to Fees

• Current Assignee: UOP Llc (Honeywell International Inc.)
• Original Assignee: UOP Llc (Honeywell International Inc.)
• Inventors: Lomas, David A., Zimmermann, Joseph E., Tagamolila, Constante P., Haun, Edward C.
• Primary Examiner(s): Pal, Asok
• Assistant Examiner(s): Yildirim, Bekir L.
• Application Number:
  US08/073,396
• Time in Patent Office: 511 Days
• Field of Search: 208/48 Q, 208/78, 208/100, 208/101, 208/103, 208/104, 208/105, 208/113, 208/74, 208/50, 208/59, 208/96, 208/99, 208/146, 208/147, 208/155, 208/157, 208/83, 208/108, 422/190, 585/519
• US Class Current: 208/101
• CPC Class Codes: C10G 11/18 according to the "fluidised-bed" technique
• CPC Class Codes: C10G 7/02 Stabilising gasoline by removing gases by fractioning

Abstract

A FCC product recovery section operates at greater efficiency by recovering separate riser product streams and reactor product streams and quenching and absorbing lighter, more valuable hydrocarbon products from the reactor product stream in separate quench and absorption vessels. The quench and absorbtion vessels are intergrated with a main fractionator and gas concentration section of a typical FCC product recovery section. Heavy hydrocarbons, clarified oil and/or cycle oil absorb hydrocarbons from the reactor product stream in the quench and absorption vessels and return the absorbed products to the main fractionator while net gasoline product from the reactor product stream enter the primary absorber of the gas concentration section. This arrangement is particularly useful in increasing the product recovery capacity of an existing FCC product separation section.

Claims

1. A process for the fluidized catalytic cracking (FCC) of an FCC feedstock and the recovery of a riser effluent stream and a reactor effluent stream, said process comprising:

a) passing an FCC feedstock and regenerated catalyst particles to a reactor riser and transporting said catalyst and feedstock through said riser to convert said feedstock;

b) discharging a mixture comprising catalyst particles and gaseous hydrocarbons from a discharge end of said riser directly into a separation zone, separating gaseous hydrocarbons from catalyst containing adsorbed hydrocarbons and recovering a riser effluent stream from said separation zone;

c) passing said catalyst containing adsorbed hydrocarbons from said separation zone into a reaction vessel and withdrawing a reactor effluent stream from said reactor vessel;

d) separating said riser effluent stream in a primary fractionation zone and recovering fractions comprising a heavy hydrocarbon stream, a light cycle oil stream and a gasoline stream;

e) passing said reactor effluent stream to a reactor quench zone and contacting said reactor effluent stream with at least a portion of at least one of said fractions in said quench zone to absorb C₃ and higher hydrocarbons from said reactor effluent stream and produce a quenched overhead stream and a primary recycle stream;

f) returning at least a portion of said primary recycle stream to said primary fractionation zone;

g) passing at least a portion of said quenched overhead stream to a reactor absorber and contacting said at least a portion of said quenched overhead stream with at least a portion of said light cycle oil stream in said reactor absorber to absorb C₃ and higher hydrocarbons from said quenched overhead stream and produce a reactor gas stream comprising C₂ hydrocarbons and lower boiling gases and a C₃ rich light cycle oil stream; and

,

h) returning said C₃ rich light cycle oil stream to said primary fractionation zone.

2. The process of claim 1 wherein at least one of said fractions of step e) comprises a heavy hydrocarbon stream having a boiling point greater than said light cycle oil stream.

3. The process of claim 1 wherein a gas fraction of said gasoline stream is contacted with an absorber liquid in a primary absorber and at least a fraction of said quenched overhead vapor is compressed, condensed and passed to said primary absorber.

4. The process of claim 3 wherein a condensed fraction of said gasoline fraction is stripped and debutanized to provide a debutanized gasoline product and a portion of said absorber liquid comprises a portion of said debutanized gasoline product.

5. The process of claim 1 wherein said reactor gas stream is separated to reject hydrocarbons and recover a hydrogen-rich stream.

6. The process of claim 1 wherein a secondary feed stream is passed to said reactor zone and recovered from said reactor with said reactor effluent stream.

7. The process of claim 6 wherein said secondary feed stream comprises at least one of hydrotreated heavy naphtha, hydrotreated light cycle oil, light reformate, and olefins.

8. The process of claim 1 wherein a lift gas contacts said regenerated catalyst particles in a section of said riser upstream of the contacting of said regenerated catalyst particles and said feedstock and said lift gas comprises a compressed gas fraction of said quenched overhead stream.

9. The process of claim 1 wherein said quenched overhead stream is condensed and separated into a first absorber gas that supplies an input to said reactor absorber and a first recycle liquid that is returned to said primary fractionation zone.

10. The process of claim 8 wherein said quenched overhead stream is condensed and separated into a first absorber gas and a first recycle liquid that is returned to said primary fractionation zone, said first absorber gas is compressed condensed and separated into a second absorber gas and a second recycle liquid, said second recycle liquid is combined with said gasoline stream, a first portion of said second absorber gas comprises said lift gas and a second portion of said second absorber gas is passed to said reactor absorber.

11. The process of claim 1 wherein said reactor product stream comprises less than 10 wt. % of the gaseous products entering said separation zone.

12. A process for the fluidized catalytic cracking (FCC) of an FCC feedstock and the recovery of a riser product stream and a reactor product stream, said process comprising:

a) passing said FCC feedstock and regenerated catalyst particles to a reactor riser and transporting said catalyst and feedstock upwardly through said riser thereby converting said feedstock to a riser gaseous product stream;

b) discharging a mixture of catalyst particles and gaseous products from a discharge end of said riser directly into a disengaging vessel, separating gaseous components from catalyst containing adsorbed hydrocarbons in said disengaging vessel and recovering a riser product stream from said disengaging vessel;

c) passing said catalyst containing adsorbed hydrocarbons from said disengaging vessel into a reaction vessel, maintaining a dense bed of catalyst in said reaction vessel and withdrawing a reactor product stream from said reactor vessel;

d) passing spent catalyst from said reactor vessel into a regeneration zone and contacting said spent catalyst with a regeneration gas in said regeneration zone to combust coke from said catalyst particles and produce regenerated catalyst particles for transfer to said reactor riser;

e) separating said riser product stream in a primary fractionation zone and producing a heavy hydrocarbon stream, a light cycle oil stream and a gasoline stream;

f) condensing said gasoline stream and separating said gasoline stream into a first vapor gasoline fraction and a first liquid gasoline fraction;

g) passing said reactor product stream to a reactor quench zone and contacting said reactor product stream with a portion of said heavy hydrocarbon stream in said quench zone to absorb C₃ and higher hydrocarbons from said reactor product stream and produce a quenched overhead stream and a heavy hydrocarbon recycle stream and returning said heavy hydrocarbon recycle stream to said primary fractionation zone;

h) separating said quenched overhead fraction into a first absorber gas stream and a first recycle liquid and passing at least a portion of said first recycle liquid to said primary fractionation zone;

i) separating said first absorber gas into a second absorber gas stream and a second recycle liquid;

j) passing said second absorber gas stream to a reactor absorber and contacting said second absorber gas with a portion of said light cycle oil stream in said reactor absorber to absorb C₃ and higher hydrocarbons from said second absorber gas and produce a reactor gas stream comprising C₂ hydrocarbons and lower boiling gases and a C₃ rich light cycle oil stream and returning said C₃ rich light cycle oil stream to said primary fractionation zone;

k) combining said second recycle liquid with said first vapor gasoline fraction and separating the combined stream into a second vapor gasoline fraction and second gasoline liquid fraction;

l) stripping and debutanizing said second gasoline fraction to produce a gasoline product stream; and

,

m) contacting said second gasoline vapor stream with a portion of at least one of said gasoline product stream and said first liquid gasoline fraction to absorb C₂ and lower boiling hydrocarbons and produce a light gas stream and a gasoline recycle stream.

13. The process of claim 12 wherein said light gas stream contacts a portion of said light cycle oil in a secondary absorber to absorb C₄ and higher boiling hydrocarbons and the light cycle oil from said secondary absorber is recycled to said primary fractionation zone.

14. The process of claim 12 wherein a stripping zone is located subadjacent to said reactor vessel, said catalyst is passed from said reactor vessel to said stripping zone, a stripping fluid is passed upwardly through said stripping zone and said spent catalyst is transferred from said stripping zone to said regeneration vessel.

15. The process of claim 14 wherein a secondary feed is injected into said stripping zone.

16. The process of claim 12 wherein said disengaging vessel is located in said reactor vessel.

17. The process of claim 16 wherein a dense bed of said partially spent catalyst is maintained in said disengaging vessel and a stripping medium passes upwardly through said dense bed of catalyst in said disengaging vessel and is withdrawn with said riser product stream.

18. The process of claim 12 wherein said light cycle oil stream has an end boiling point in a range of 500°

-650°

F. and a portion of said light cycle oil is contacted with catalyst in said dense bed of said reaction vessel.

19. The process of claim 12 wherein a benzene containing stream is passed to said dense bed of said reaction vessel and alkylated to produce C₇ and C₈ aromatics.

20. The process of claim 19 wherein said benzene containing stream is a light reformate stream.

21. A process for the fluidized catalytic cracking (FCC) of an FCC feedstock and the recovery of a riser product stream and a reactor product stream, said process comprising:

a) passing said FCC feedstock and regenerated catalyst particles to a reactor riser and transporting said catalyst and feedstock upwardly through said riser thereby converting said feedstock to a riser gaseous product stream;

b) discharging a mixture of catalyst particles and gaseous products from a discharge end of said riser directly into a separation zone, separating gaseous components from catalyst containing adsorbed hydrocarbons in said disengaging vessel and recovering a riser product stream from said separation zone;

c) passing said catalyst containing adsorbed hydrocarbons from said separation zone into a reaction vessel, maintaining a dense bed of catalyst in said reaction vessel and withdrawing a reactor product stream from said reactor vessel;

d) separating said riser product stream in a primary fractionation zone and producing a heavy hydrocarbon stream, a light cycle oil stream and a gasoline stream;

e) condensing said gasoline stream and separating said gasoline stream into a first vapor gasoline fraction and a first liquid gasoline fraction;

f) passing said reactor product stream to a reactor quench zone and contacting said reactor product stream with a portion of said heavy hydrocarbon stream in said quench zone to absorb C₃ and higher hydrocarbons from said reactor product stream and produce a quenched overhead stream and a heavy hydrocarbon recycle stream and returning said heavy hydrocarbon recycle stream to said primary fractionation zone;

g) condensing said quenched overhead stream and separating said quenched overhead stream into a first absorber gas stream and a first recycle liquid and passing at least a portion of said first recycle liquid to said to said primary fractionation zone;

h) condensing said first absorber gas stream and separating said first absorber gas stream into a second absorber gas stream and a second recycle liquid;

i) combining said second recycle liquid with said first vapor gasoline fraction and separating the combined stream into a second vapor gasoline fraction and second gasoline liquid fraction;

j) stripping and debutanizing said second gasoline fraction to produce a gasoline product stream;

k) contacting said second gasoline vapor stream with a portion of said gasoline product stream and a portion of said first liquid gasoline fraction to absorb C₂ and lower boiling hydrocarbons and produce a light gas stream and a gasoline recycle stream and recycling said gasoline recycle stream to said first gasoline vapor stream; and

,

l) contacting said light gas stream and said second absorber gas stream with a portion of said light cycle oil in a secondary absorber to absorb C₄ and higher boiling hydrocarbons, recycling the light cycle oil from said secondary absorber to said primary fractionation zone and recovering a net gas stream from said secondary absorber.