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Hydrocarbon feedstock containing resid is cracked by a process comprising: (a) heating the hydrocarbon feedstock; (b) mixing the heated hydrocarbon feedstock with steam and optionally water to form a mixture stream; (c) introducing the mixture stream to a flash/separation apparatus to form i) a vapo

Hydrocarbon feedstock containing resid is cracked by a process comprising: (a) heating the hydrocarbon feedstock; (b) mixing the heated hydrocarbon feedstock with steam and optionally water to form a mixture stream; (c) introducing the mixture stream to a flash/separation apparatus to form i) a vapor phase at its dew point which partially cracks and loses/or heat causing a temperature decrease and partial condensation of the vapor phase in the absence of added heat to provide coke precursors existing as uncoalesced condensate, and ii) a liquid phase; (d) removing the vapor phase as overhead and the liquid phase as bottoms from the flash/separation apparatus; (e) treating the overhead by contacting with a hydrocarbon-containing nucleating liquid substantially free of resid and comprising components boiling at a temperature of at least about 260�� C. (500�� F.) under conditions sufficient to at least partially coalesce the coke precursors to provide coke precursor liquid, in the form of hydrocarbon droplets or a continuous hydrocarbon liquid phase; (f) collecting and removing the droplets; (g) directing the treated overhead from which the droplets are removed, to a heater to provide a heated vapor phase; (h) cracking the heated vapor phase in a radiant section of a pyrolysis furnace to produce an effluent comprising olefins, the pyrolysis furnace comprising a radiant section and a convection section; and (i) quenching the effluent and recovering cracked product therefrom. An apparatus for carrying out the process is also provided.

대표청구항 ▼

What is claimed is: 1. A process for cracking a hydrocarbon feedstock containing resid, said process comprising: (a) heating said hydrocarbon feedstock; (b) mixing the heated hydrocarbon feedstock with steam and optionally water to form a mixture stream; (c) introducing the mixture stream to a flas

What is claimed is: 1. A process for cracking a hydrocarbon feedstock containing resid, said process comprising: (a) heating said hydrocarbon feedstock; (b) mixing the heated hydrocarbon feedstock with steam and optionally water to form a mixture stream; (c) introducing the mixture stream to a flash/separation apparatus to form i) a vapor phase which partially cracks and/or loses heat causing partial condensation of said vapor phase to provide coke precursors existing as uncoalesced condensate, and ii) a liquid phase; (d) removing the vapor phase as overhead; (e) treating said overhead by contacting with a hydrocarbon-containing nucleating liquid substantially free of resid and comprising components boiling at a temperature of at least about 260�� C. (500�� F.) under conditions sufficient to at least partially coalesce said coke precursors to provide coke precursor liquid; (f) removing said coke precursor liquid; (g) heating the treated overhead from which said coke precursor liquid is removed to provide a heated vapor phase; (h) cracking the heated vapor phase in a pyrolysis furnace to produce an effluent comprising olefins; and (i) quenching the effluent and recovering cracked product therefrom. 2. The process of claim 1 wherein said uncoalesced condensate comprises particles of less than about ten microns in their largest dimension. 3. The process of claim 1 wherein said uncoalesced condensate comprises particles of less than about one micron in their largest dimension. 4. The process of claim 1 wherein said vapor phase from step (c) is supersaturated with said coke precursors. 5. The process of claim 4 wherein said vapor phase from step (c) has a homogeneous nucleation parameter, S, which is less than about 1.4. 6. The process of claim 4 wherein said vapor phase from step (c) has a homogeneous nucleation parameter, S, which ranges from about 0.0034 to about 0.016. 7. The process of claim 1 wherein said vapor phase from step (c) further contains at least trace amounts of coke precursor liquid. 8. The process of claim 7 which further comprises at least partially removing said coke precursor liquid from said overhead in a centrifugal separator. 9. The process of claim 8 wherein said centrifugal separator comprises a cylinder having an upper portion and a lower portion, said upper portion having an upper vapor inlet with deflectors which impart a downward swirling motion to said vapor, and an upper vapor outlet, and said lower portion having a lower liquid outlet for removing said coke precursor liquid. 10. The process of claim 9 wherein said contacting is carried out upstream of said centrifugal separator. 11. The process of claim 9 wherein said contacting is carried out in the upper portion of said centrifugal separator. 12. The process of claim 11 wherein said hydrocarbon-containing nucleating liquid is introduced adjacent said upper vapor inlet. 13. The process of claim 11 wherein said hydrocarbon-containing nucleating liquid is introduced adjacent said upper vapor outlet. 14. The process of claim 9 which further comprises removing said coalesced coke precursor droplets through said lower liquid outlet. 15. The process of claim 14 which further comprises introducing effluent from said lower liquid outlet to said flash/separation apparatus. 16. The process of claim 15 wherein a quenching additive is introduced to said effluent from said lower liquid outlet prior to introducing said effluent to said flash/separation apparatus. 17. The process of claim 16 wherein said quenching additive is selected from the group consisting of steam cracker gas oil, quench oil, and cycle oil, and is introduced to said effluent at a temperature no greater than about 260�� C. (500�� F.). 18. The process of claim 17 wherein said quenching additive is steam cracker gas oil introduced to said effluent at a temperature of about 140�� C. (280�� F.). 19. The process of claim 8 wherein (e) further comprises treating said overhead by contacting with a condensing means downstream of said flash/separation apparatus to at least partially coalesce said coke precursors to provide coke precursor liquid. 20. The process of claim 19 wherein said condensing means is located in said upper portion of said centrifugal separator which further condenses and coalesces said overhead. 21. The process of claim 1 wherein (e) further comprises treating said overhead by contacting with a condensing means downstream of said flash/separation apparatus to at least partially coalesce said coke precursors to provide coke precursor liquid. 22. The process of claim 1 wherein said nucleating liquid comprises components boiling at a temperature of at least about 450�� C. (840�� F.). 23. The process of claim 1 wherein said nucleating liquid comprises components boiling at a temperature below about 600�� C. (1110�� F.). 24. The process of claim 1 wherein said nucleating liquid is selected from vacuum gas oil and deasphalted vacuum resid. 25. The process of claim 1 wherein said nucleating liquid comprises heavy vacuum gas oil. 26. The process of claim 1 wherein said nucleating liquid is at a temperature below about 260�� C. (500�� F.). 27. The process of claim 1 wherein said nucleating liquid is at a temperature ranging from about 450 to about 550�� C. (840 to 1020�� F.). 28. The process of claim 1 wherein said bottoms from said flash/separation apparatus are cooled and then recycled as quench to said flash/separation apparatus. 29. The process of claim 1 wherein said bottoms from said flash/separation apparatus are utilized as fuel. 30. The process of claim 1 wherein superheated steam is added to said treated overhead prior to directing the treated overhead to a heater. 31. The process of claim 1 wherein at least about 50 wt % of said coke precursor liquid is coalesced by said treating and removed as droplets or a continuous liquid phase. 32. The process of claim 31 wherein at least about 75 wt % of said coke precursor liquid is coalesced by said treating and removed as droplets or a continuous liquid phase. 33. The process of claim 1 wherein said mixture stream is introduced through a side of said flash/separation apparatus via at least one tangential inlet. 34. The process of claim 1 wherein said mixture stream is introduced as a two-phase stratified open channel flow. 35. The process of claim 1 wherein said vapor phase throughput for said flash/separation apparatus ranges from about 9,000 to about 90,000 kg/hour (20,000 to 200,000 pounds/hour) steam, from about 25,000 to about 80,000 kg/hour (55,000 to 180,000 pounds/hour) hydrocarbons. 36. The process of claim 1 wherein said vapor phase throughput for said flash/separation apparatus is about 15,000 kg/hour (33,000 pounds/hour) steam, about 33,000 kg/hour (73,000 pounds/hour) hydrocarbons.