Process for reducing FCC transfer line coking

• US 5,258,113 A
• Filed: 02/04/1991
• Issued: 11/02/1993
• Est. Priority Date: 02/04/1991
• Status: Expired due to Fees

• Current Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Original Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Inventors: Edgerton, Mary E., Sapre, Ajit V.
• Primary Examiner(s): MYERS, HELANE ELEANORA
• Application Number:
  US07/650,160
• Time in Patent Office: 1,002 Days
• Field of Search: 208/48 AA
• US Class Current: 208/48.0AA
• CPC Class Codes: C10G 11/18 according to the "fluidised-bed" technique
• CPC Class Codes: C10G 75/04 by addition of antifouling agents

Abstract

Coke formation/deposition within and downstream of catalytic cracking reactors is suppressed by adding a coke suppressing additive to the cracking reactor and/or cracked product vapor. Free radical inhibitors, such as oxygenates, are preferred. The additive addition rate is preferably controlled based on temperature of regenerated catalyst, or a direct or indirect measurement of coke accumulation on the transfer line between the cracking reactor and the main fractionator.

Claims

1. A fluidized catalytic cracking process wherein a heavy hydrocarbon feed comprising hydrocarbons having a boiling point above about 650°

F. is catalytically cracked to produce spent catalyst and cracked products comprising coke precursors which form coke deposits on solid surfaces comprising;

a. adding to the base of a riser reactor at a heavy hydrocarbon feed addition point said heavy feed and mixing said feed with a source of hot regenerated catalytic cracking catalyst withdrawn from a catalyst regenerator;

b. catalytically cracking said feed in said riser catalytic cracking zone, at a temperature of 425°

to 600°

C., a catalyst to feed weight ratio of about 3;

1 to 10;

1 and in the absence of added hydrogen, to produce catalytically cracked vapor products and spent catalyst;

c. adding to said riser reactor, downstream of the point of feed addition to said riser and upstream of a transfer line used to transfer catalytically cracked products to a fractionation column, a coke suppressing additive in a form and in an amount sufficient to suppress coke deposition in said transfer line, and in a form and amount which has no adverse affect on the cracking activity of the cracking catalyst;

d. discharging from the top of said riser reactor a mixture of catalytically cracked vapor products containing said additive and spent catalyst;

e. separating in a spent catalyst/vapor disengaging zone said mixture of spent catalyst and cracked vapor products to produce a cracked product vapor phase containing said additive and spent catalyst;

f. transferring from said disengaging zone said separated cracked vapor products via said transfer line to a fractionator;

g. stripping said spent catalyst from said disengaging zone in a catalyst stripping means to produce stripped catalyst;

h. regenerating said stripped catalyst by contact with a regeneration gas to produce regenerated catalyst; and

i. recycling said regenerated catalyst to said base of said reactor to mix with said heavy feed.

2. The process of claim 1 wherein said additive is added just upstream of a riser catalyst outlet and disengaging zone.

3. The process of claim 1 wherein said additive is added downstream of said disengaging zone.

4. The process of claim 1 wherein said additive, exclusive of diluents, solvents or dispersants which may be present, is present in an amount equal to 0.1 to 1,000 wt ppm based on weight of cracked vapor product.

5. The process of claim 1 wherein said additive, exclusive of diluents, solvents or dispersants which may be present, is present in an amount equal to 0.5 to 100 wt ppm based on weight of cracked vapor product.

6. The process of claim 1 wherein said additive, exclusive of diluents, solvents or dispersants which may be present, is present in an amount equal to 1 to 10 wt ppm based on weight of cracked vapor product.

7. A fluidized catalytic cracking process wherein a heavy hydrocarbon feed comprising hydrocarbons having a boiling point above about 650°

F. is catalytically cracked to produce spent catalyst and cracked products comprising coke precursors which form coke deposits on solid surfaces comprising;

a. adding to the base of a riser reactor at a heavy hydrocarbon feed addition point said heavy feed and mixing said feed with a source of hot regenerated catalytic cracking catalyst having cracking activity withdrawn from a catalyst regenerator;

b. catalytically cracking said feed in said riser catalytic cracking zone, at a temperature of 425°

to 600°

C., a catalyst to feed weight ratio of about 3;

1 to 10;

1 and in the absence of added hydrogen, to produce catalytically cracked vapor products and spent catalyst;

c. adding to said riser reactor, downstream of the point of feed addition to said riser and upstream of a transfer line used to transfer catalytically cracked products to a fractionation column, a coke suppressing additive in a form and in an amount sufficient to suppress coke deposition in said transfer line, and in a form and amount such that at least 90% of said additive remains with cracked vapor product and less than 10% of said additive deposits on said cracking catalyst;

d. discharging from the top of said riser reactor a mixture of catalytically cracked vapor products containing said additive and spent catalyst;

e. separating in a spent catalyst/vapor disengaging zone said mixture of spent catalyst and cracked vapor products to produce a cracked product vapor phase containing said additive and spent catalyst;

f. transferring from said disengaging zone said separated cracked vapor products via said transfer line to a fractionator;

g. stripping said spent catalyst from said disengaging zone in a catalyst stripping means to produce stripped catalyst;

h. regenerating said stripped catalyst by contact with a regeneration gas to produce regenerated catalyst; and

i. recycling said regenerated catalyst to said base of said reactor to mix with said heavy feed.

8. The process of claim 7 wherein said additive, exclusive of diluents, solvents or dispersants which may be present, is present in an amount equal to 0.1 to 1000 wt ppm based on weight of cracked vapor product.

9. The process of claim 7 wherein said additive, exclusive of diluents, solvents or dispersants which may be present, is present in an amount equal to 0.5 to 100 wt ppm based on weight of cracked vapor product.

10. The process of claim 7 wherein said additive, exclusive of diluents, solvents or dispersants which may be present, is present in an amount equal to 1 to 10 wt ppm based on weight of cracked vapor product.

11. The process of claim 7 wherein the additive is a free radical scavenger.

12. The process of claim 7 wherein the additive is selected from the group of ammonium borate, ammonium biborate and ammonium pentaborate, boron oxides, borates, borate ester, peroxyborates, borane, organoboranes, and elemental phosphorous and compounds thereof, phosphate and phosphite mono and diesters and thioesters, and a salt of a metal of V, Mo, Cr, W, Fe, Co and Ni.

13. A fluidized catalytic cracking process wherein a heavy hydrocarbon feed comprising hydrocarbons having a boiling point above about 650°

F. is catalytically cracked to cracked products including coke precursors which form coke deposits on solid surfaces comprising;

a. adding to the base of a riser reactor a heavy hydrocarbon feed and mixing said feed with a source of hot regenerated catalytic cracking catalyst having cracking activity withdrawn from a catalyst regenerator;

b. catalytically cracking said feed in said riser catalytic cracking zone, at a temperature of 425°

to 600°

C., a catalyst to feed weight ratio of about 3;

1 to 10;

1 and in the absence of added hydrogen, to produce catalytically cracked vapor products containing coke precursors and spent catalyst;

c. discharging from the top of said riser reactor a mixture of catalytically cracked vapor products containing coke precursors and spent catalyst;

d. separating in a spent catalyst/vapor disengaging zone said mixture of spent catalyst and cracked vapor products to produce a cracked product vapor phase containing said coke precursors and spent catalyst;

e. adding to said separated cracked product vapor phase a coke suppressing additive;

f. transferring from said disengaging zone said separated cracked vapor products via said transfer line to a fractionator;

g. coking said transfer line with said coke precursors, measuring coke formation in said transfer line, and controlling the addition of said coke suppressing additive to said separated cracked product vapor phase based on said measurement of coke formation in said transfer line;

h. stripping said spent catalyst from said disengaging zone in a catalyst stripping means to produce stripped catalyst;

i. regenerating said stripped catalyst by contact with a regeneration gas to produce regenerated catalyst; and

j. recycling said regenerated catalyst to said base of said reactor to mix with said heavy feed.

14. The control method of claim 13 wherein additive addition rate is controlled based on the temperature of said regenerated catalyst.

15. The control method of claim 13 wherein the additive addition rate is determined by a direct or indirect measurement of a coke buildup in the transfer line.