Catalytic cracking with deasphalted oil

• US 4,940,529 A
• Filed: 07/18/1989
• Issued: 07/10/1990
• Est. Priority Date: 07/18/1989
• Status: Expired due to Term

• Current Assignee: Amoco Corporation (BP PLC), Toa Nenryo Kogyo Kabushiki Kaisha
• Original Assignee: Amoco Corporation (BP PLC)
• Inventors: Taylor, James L., Mosby, James F., Peck, Lawrence B., Beaton, William I.
• Primary Examiner(s): Myers, Helane
• Application Number:
  US07/381,295
• Time in Patent Office: 357 Days
• Field of Search: 208/86, 208/87, 208/108, 208/92, 208/251 H, 208/254 H, 208/143, 208/211, 208/212, 208/61
• US Class Current: 208/61
• CPC Class Codes: C10G 2300/1074 Vacuum distillates
• CPC Class Codes: C10G 2300/205 Metal content
• CPC Class Codes: C10G 2300/206 Asphaltenes
• CPC Class Codes: C10G 2300/708 Coking aspect, coke content and composition of deposits
• CPC Class Codes: C10G 67/0463 The hydrotreatment being a hydrorefining
• CPC Class Codes: C10G 69/04 including at least one step of catalytic cracking in the absence of hydrogen

Abstract

A process is provided in which solvent-extracted oil or other deasphalted oil derived from hydrotreated resid is catalytically cracked to increase the yield of gasoline and other high value products.

Claims

1. A catalytic cracking process, comprising the steps of:

hydrotreating resid;

thereafter deasphalting said hydrotreated resid to produce substantially deasphalted oil;

catalytically cracking said hydrotreated oil in a catalytic cracking unit in the presence of a cracking catalyst to produce upgraded oil leaving coked catalyst; and

regenerating said coked catalyst in the presence of a combustion-supporting gas comprising excess molecular oxygen in an amount greater than the stoichiometric amount required for substantially completely combusting the coke on said catalyst to carbon dioxide.

2. A catalytic cracking process in accordance with claim 1 wherein:

said hydrotreated resid comprises resid selected from the group consisting of high sulfur resid and low sulfur resid;

said gas comprises air; and

said cracking catalyst comprises a crystalline aluminosilicate catalyst.

3. A catalytic cracking process in accordance with claim 1 wherein said deasphalting comprises solvent extraction and said regeneration comprises recycling said regenerated catalyst to said catalytic cracking unit in the absence of substantially demetallizing said regenerated cracking catalyst.

4. A catalytic cracking process in accordance with claim 1 wherein said deasphalting includes separating asphaltenes, resins, and deasphalted oil from said hydotreated resid.

5. A catalytic cracking process in accordance with claim 4 including catalytically cracking said resins which have been added to said deasphalted oil.

6. A catalytic cracking process, comprising the steps of:

feeding virgin unhydrotreated resid to a reactor;

feeding resins to said reactor;

feeding hydrotreating catalyst to said reactor;

injecting hydrogen-rich gases to said reactor;

hydrotreating said virgin resid and resins in said reactor by contacting said virgin resid and resins with said hydrogen-rich gases in the presence of said hydrotreating catalyst and in the absence of a hydrogen donor under hydrotreating conditions to produce hydrotreated resid oil;

fractionating said hydrotreated resid oil into fractions of gas oil and resid bottoms;

separating asphaltenes, resins, and deasphalted oil from said resid bottoms by solvent extraction;

recycling said resins to said reactor; and

catalytically cracking said gas oil and deasphalted oil in the presence of a cracking catalyst and in the absence of hydrogen-rich gases to produce upgraded oil.

7. A catalytic cracking process in accordance with claim 6 wherein said gas oil and deasphalted oil is cracked in a riser reactor.

8. A catalytic cracking process in accordance with claim 6 wherein said gas oil and deasphalted oil is cracked in a catalytic cracker

9. A catalytic cracking process in accordance with claim 6 including simultaneously cracking catalytic feed hydrotreated oil with said gas oil and separated oil.

10. A catalytic cracking process in accordance with claim 6 wherein said resins and virgin resid are hydrotreated and ebullated in an ebullated bed reactor.

11. A catalytic cracking process in accordance with claim 6 wherein said fractionating occurs in a fractionator selected from the group consisting of an atmospheric tower and a vacuum tower and said hydrotreating occurs at a pressure ranging from about 2550 psia to about 3050 psia.

12. A catalytic cracking process in accordance with claim 6 wherein:

said cracking catalyst comprises a zeolite catalyst;

said zeolite catalyst is coked during said cracking; and

said coked catalyst is regenerated in the presence of excess air in an amount greater than the stoichiometric amount required for completely combusting the coke to carbon dioxide.

13. A catalytic cracking process in accordance with claim 6 wherein more than 95% by weight of metals in said resid bottoms is removed from said deasphalted oil during said solvent extraction.

14. A catalytic cracking process in accordance with claim 6 wherein said separation by solvent extraction occurs under about supercritical conditions with supercritical solvent recovery.

15. A catalytic cracking process in accordance with claim 6 including subsequently using said asphaltenes as fuel.

16. A catalytic cracking process in accordance with claim 6 including coking said asphaltenes in a coker.

17. A catalytic cracking unit in accordance with claim 6 wherein said deasphalted oil comprises less than 5 ppm nickel and less than 5 ppm vanadium.

18. A catalytic cracking process, comprising the steps of:

feeding atmospheric gas oil from an atmospheric tower to a cracking reactor of a catalytic cracking unit, said cracking reactor comprising at least one reactor selected from the group consisting of a riser reactor and a catalytic cracker;

feeding primary gas oil from a primary tower to said cracking reactor;

feeding hydrotreated oil from a catalytic feed hydrotreating unit to said cracking reactor;

feeding solvent-extracted oil comprising less than 5 ppm vanadium and less than 5 ppm nickel to said cracking reactor;

feeding fresh and regenerated crystalline aluminosilicate cracking catalyst to said cracking reactor;

catalytically cracking said gas oil, hydrotreated oil and solvent-extracted oil in said cracking reactor in the presence of said cracking catalyst under catalytic cracking conditions to produce cracked oil leaving spent coked catalyst;

conveying said spent coked catalyst to a regenerator of said catalytic cracking unit;

injecting air into said regenerator;

regenerating said spent catalyst by substantially combusting coke on said spent catalyst in the presence of air in said regenerator;

recycling said regenerated catalyst directly from said regenerator to said cracking reactor in the absence of substantially demetallizing said regenerated catalyst;

separating said cracked oil in a fractionator into streams of light hydrocarbon gases, catalytic naphtha, catalytic cycle oil, and decanted oil;

substantially desalting crude oil;

heating said desalted crude oil in a pipestill furnace;

pumping said heated crude oil to a primary distillation tower;

separating said heated crude oil in said primary distillation tower into streams of naphtha, kerosene, primary gas oil, and primary reduced crude oil;

conveying said primary gas oil to said catalytic cracker;

pumping said primary reduced crude oil to a pipestill vacuum tower;

separating said primary gas oil in said pipestill vacuum tower into streams of wet gas, heavy gas oil, and vacuum reduced crude oil providing resid oil;

feeding fresh feed comprising said resid oil from said pipestill vacuum tower to a resid hydrotreating unit comprising a series of three ebullated bed reactors;

injecting hydrogen-rich gases into said ebullated bed reactors;

conveying resid hydrotreating catalyst to said ebullated bed reactors;

ebullating said resid oil and said hydrogen-rich gases together in the presence of said resid hydrotreating catalyst in said ebullated bed reactors at a pressure ranging from about 2550 psia to about 3050 psia to produce upgraded hydrotreated resid oil;

separating at least a portion of said hydrotreated resid oil in an atmospheric tower into atmospheric streams of distillate, gas oil, and atmospheric tower bottoms comprising atmospheric resid oil;

conveying said atmospheric stream of gas oil from said atmospheric tower to said cracking reactor;

separating said atmospheric resid oil in a resid vacuum tower into vacuum streams of vacuum gas oil and vacuum tower bottoms comprising vacuum resid oil;

conveying said vacuum gas oil from said resid vacuum tower to a catalytic feed hydrotreating unit;

feeding coker gas oil to said catalytic feed hydrotreating unit;

injecting hydrogen-rich gases to said catalytic feed hydrotreating unit;

conveying catalytic feed hydrotreating catalyst to said catalytic feed hydrotreating unit;

hydrotreating said vacuum gas oil and said coker gas oil with said hydrogen-rich gases in the presence of said catalytic feed hydrotreating catalyst in said catalytic feed hydrotreating unit to produce hydrotreated oil;

passing said hydrotreated oil to said cracking reactor;

conveying a portion of said vacuum tower bottoms from said resid vacuum tower to a coker;

coking said vacuum tower bottoms in said coker to produce coke and coker resid oil;

conveying said coker resid oil to a combined tower;

separating said coker resid oil in said combined tower into streams of coker gases, coker naphtha, and coker gas oil;

conveying said coker gas oil from said coker to said catalytic feed hydrotreating unit;

conveying and feeding a substantial portion of said vacuum tower bottoms from said resid vacuum tower to a multistage solvent extraction unit;

feeding a solvent to said multistage solvent extraction unit, said solvent comprising a member selected from the group consisting of butane and pentane;

substantially deasphalting and solvent-extracting said vacuum tower bottoms with said solvent in said multistage solvent extraction unit to separate said vacuum tower bottoms into streams of substantially deasphalted solvent-extracted oil, substantially deasphalted solvent-extracted resins, and substantially deresined solvent-extracted asphaltenes;

recovering said solvent under supercritical conditions and recycling said solvent to said solvent extraction unit;

conveying said resins from said solvent extraction unit to said resid hydrotreating unit;

transporting at least some of said asphaltenes for use as solid fuel; and

conveying said solvent-extracted oil from said solvent extraction unit to said cracking reactor.

19. A catalytic cracking process in accordance with claim 18 wherein a substantial portion of said asphaltenes from said solvent extraction unit is conveyed to and coked in said coker.

20. A catalytic cracking process in accordance with claim 18 wherein said heavy gas oil from said pipestill vacuum tower is passed to and hydrotreated in said catalytic feed hydrotreating unit and subsequently catalytically cracked in said cracking reactor.

21. A catalytic cracking process in accordance with claim 18 including:

separating and flashing said hydrotreated resid oil in a flash drum into streams of vapors and gases, flash drum oil, and flashed hydrotreated resid oil before said hydrotreated oil is separated in said atmospheric tower; and

recycling said flash drum oil to said resid hydrotreating unit as part of said feed.

22. A catalytic cracking process in accordance with claim 18 including conveying at least part of said decanted oil from said fractionator to said resid hydrotreating unit as part of said feed to help inhibit the formation of carbonaceous solids in said hydrotreated resid oil.

23. A catalytic cracking process in accordance with claim 18 including passing at least part of said decanted oil from said fractionator to at least one tower selected from the group consisting of said atmospheric tower and said resid vacuum tower, to help decrease the amount and size of asphaltenes in said tower bottoms.

24. A catalytic cracking process in accordance with claim 18 wherein said coked catalyst is regenerated in said regenerator in the presence of excess air in an amount greater than the stoichiometric amount required for

25. A catalytic cracking process in accordance with claim 18 wherein the ratio of said solvent to said vacuum tower bottoms being fed into said multistage solvent extraction unit ranges from about 3:

1 to about 20;

1.

26. A catalytic cracking process in accordance with claim 25 wherein said ratio ranges from about 8:

1 to about 12;

1 and said solvent extraction unit comprises a three-stage solvent extraction unit.

27. A catalytic cracking process in accordance with claim 18 wherein said solvent-extracted oil is hydrotreated in said catalytic feed hydrotreating unit before being catalytically cracked in said cracking reactor.

28. A catalytic cracking process in accordance with claim 18 wherein said cracking catalyst comprises a zeolite catalyst and said solvent-extracted oil comprises less than 2 ppm nickel and less than 2 ppm vanadium.