초록 ▼

A improved process is provided for upgrading light olefins from hydrocarbon cracking, such as light crackate gas containing ethene, propene and other C 1 -C 4 lower aliphatics. The process comprises the steps of: maintaining an oligomerization reactor containing a fluidized bed of zeolite catalyst p

A improved process is provided for upgrading light olefins from hydrocarbon cracking, such as light crackate gas containing ethene, propene and other C 1 -C 4 lower aliphatics. The process comprises the steps of: maintaining an oligomerization reactor containing a fluidized bed of zeolite catalyst particles in a low severity reactor bed at oligomerization temperature conditions by passing hot olefinic gas upwardly through the fluidized catalyst bed under throughput rate conditions sufficient to convert at least 50 wt % of lower olefins to hydrocarbons in the C 5 -C 10 range; maintaining turbulent fluidized bed conditions through the fluidized bed by passing fresh ethene-rich feedstream gas upwardly through the fluidized catalyst bed and adding thereto sufficient recycled light byproduct gas to maintain a minimum gas velocity; cooling reaction effluent from the conversion zone to provide light gas byproduct and liquid hydrocarbon reaction product rich in C 5 -C 9 hydrocarbons; and recycling sufficient light byproduct gas recovered from effluent or maintaining turbulent regime gas velocity in the fluidized bed.

대표청구항 ▼

1. A process for upgrading light olefinic crackate gas from hydrocarbon cracking, said light crackate gas containing ethene, propene and other C 1 -C 4 lower aliphatics, comprising the steps of: (a) fractionating heavy oil crackate in a main fractionation column to recover distillate range hydroc

1. A process for upgrading light olefinic crackate gas from hydrocarbon cracking, said light crackate gas containing ethene, propene and other C 1 -C 4 lower aliphatics, comprising the steps of: (a) fractionating heavy oil crackate in a main fractionation column to recover distillate range hydrocarbon product, naphtha and light crackate gas; (b) compressing and cooling the light crackate gas to provide a first pressurized ethene-rich vapor stream and a first condensed crackate stream rich in C 3 + aliphatics; (c) contacting the first ethene-rich vapor stream under pressure with a C 5 + liquid sorbent stream in an absorber column under sorption conditions to selectively absorb a major amount of C 3 + components and recover a second ethene-rich vapor stream from the absorber column; (d) contacting said second ethene-rich vapor stream in a fluid bed reactor with a turbulent regime fluidized bed of acid medium pore zeolite oligomerization catalyst particles under oligomerization conditions to produce a hydrocarbon effluent stream rich in C 5 + hydrocarbons; (e) cooling the reaction effluent stream to provide light gas byproduct and liquid hydrocarbon reaction product; (f) contacting a first light gas byproduct portion from step (e) with a sponge oil in a secondary sponge absorber to recover liquid hydrocarbons; (g) recycling a second light byproduct gas portion for maintaining turbulent regime gas velocity in the fluid bed reactor of step (d); and (h) passing sponge oil sorbate liquid from the secondary absorber to the main fractionation column for recovery. 2. The process of claim 1 wherein a condensed liquid hydrocarbon stream from step (e) contains volatile components and passes into the absorber column at an upper portion thereof to be stabilized and provide sorbent liquid. 3. The process of claim 1 wherein the light olefinic crackate gas contains a minor amount of H 2 S, and including the step of contacting the absorber overhead vapor stream with liquid amine to remove H 2 S prior to contacting reaction catalyst; and wherein lean sponge oil liquid containing H 2 S is stripped free of H 2 S prior to contact with light gas in step (f). 4. The process of claim 1 wherein fluidized oligomerization catalyst has an apparent particle density of about 0.9 to 1.6 g/cm 3 and a size range of about 1 to 150 microns, average catalyst particle size of about 20 to 100 microns, and containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns. 5. The process of claim 4 wherein the oligomerization catalyst has an acid cracking value of about 2 to 50, based on total reactor fluidized catalyst weight. 6. The process of claim 1 including the step of maintaining turbulent fluidized bed conditions through the reactor bed by passing fresh ethene-rich gas from step (b) upwardly through the fluidized catalyst bed and adding thereto sufficient recycled light gas from step (g) to maintain a superficial fluid velocity of about 0.2 to 2 meters per second. 7. The process of claim 1 wherein said light crackate gas comprises at least 5 mole % ethylene. 8. The process of claim 1 comprising the steps of maintaining an oligomerization reactor containing a fluidized bed of zeolite catalyst particles in a low severity reactor bed at oligomerization temperature of about 260° to 650° C.; passing hot olefinic crackate gas upwardly through the fluidized catalyst bed under normal design capacity throughput rate conditions sufficient to convert at least 50 wt % of lower olefins to heavier hydrocarbons in the C 5 -C 10 range. 9. The process of claim 1 comprising the further step of withdrawing a portion of coked catalyst from the fluidized bed reactor, oxidatively regenerating the withdrawn catalyst and returning regenerated catalyst to the fluidized bed reactor at a rate to control catalyst activity whereby C 3 -C 5 alkane:alkene weight ratio in the hydrocarbon product is maintained at about 0.04:1 to 7:1 under conditions of reaction severity to effect feedstock conversion. 10. The process of claim 1 wherein the oligomerization catalyst consists essentially of a medium pore pentasil zeolite having an acid cracking value of about 0.1 to 20 and average particle size of about 20 to 100 microns; fluidized bed reactor catalyst inventory includes at least 10 weight percent fine particles having a particle size less than 32 microns; and wherein said catalyst particles comprise about 5 to 95 weight percent acid metallosilicate zeolite having the structure of ZSM-5 and having a crystal size of about 0.02-2 microns. 11. A continuous process for upgrading a variable throughput light olefinic gas feedstream rich in ethylene and C 3 -C 4 aliphatic hydrocarbons in a fluidized bed catalytic conversion zone, comprising the steps of: maintaining an oligomerization reactor containing a fluidized bed of zeolite catalyst particles in a low severity reactor bed at oligomerization temperature conditions by passing hot olefinic gas upwardly through the fluidized catalyst bed under throughput rate conditions sufficient to convert at least 50 wt % of lower olefins to hydrocarbons in the C 5 -C 10 range; maintaining turbulent fluidized bed conditions through the fluidized bed by passing fresh ethene-rich feedstream gas upwardly through the fluidized catalyst bed and adding thereto sufficient recycled light byproduct gas to maintain a superficial gas velocity of about 0.3 to 2 meters per second. cooling reaction effluent from the conversion zone to provide light gas byproduct and liquid hydrocarbon reaction product rich in C 5 -C 9 hydrocarbons; recycling sufficient light byproduct gas recovered from effluent for maintaining turbulent regime gas velocity in the fluidized bed. 12. The process of claim 11 including the steps of measuring flow rate of gas introduced below the fluidized bed, providing a signal representative of said gas flow rate, controlling addition rate of light byproduct gas to the fresh olefin feedstream to maintain superficial gas velocity at a predetermined rate in the range of 0.2 to 3 meters/second, thereby maintaining turbulent regime operating conditions in the fluidized bed under turndown feedstream operation. 13. A process for upgrading light olefinic crackate gas from hydrocarbon cracking, said light crackate gas containing ethene, propene and other C 1 -C 4 lower aliphatics, comprising the steps of: (a) fractionating heavy oil crackate in a main fractionation column to recover distillate range hydrocarbon product, naphtha and light crackate gas; (b) compressing and cooling the light crackate gas to provide a first pressurized ethene-rich vapor stream and a first condensed crackate stream rich in C 3 + aliphatics; (c) contacting the first ethene-rich vapor stream under pressure with a C 5 + liquid sorbent stream in an absorber column under sorption conditions to selectively absorb a major amount of C 3 + components and recover a second ethene-rich vapor stream from the absorber column; (d) contacting said second ethene-rich vapor stream in a fluid bed reactor with a turbulent regime fluidized bed of acid medium pore zeolite oligomerization catalyst particles under oligomerization conditions to produce a hydrocarbon effluent stream rich in C 5 + hydrocarbons; (e) cooling the reaction effluent stream to provide light gas byproduct and liquid hydrocarbon reaction product; (f) contacting a first light gas byproduct portion from step (e) with a sponge oil in a secondary sponge absorber having a bottom portion operatively connected to receive reaction effluent for recovery of liquid hydrocarbons; (g) recycling a second light byproduct gas portion in an amount sufficient to maintain turbulent regime gas velocity in the fluid bed reactor of step (d); (h) passing sponge oil sorbate liquid from the secondary absorber to the main fractionation column for recovery; (i) flashing substantially the entire cooled reaction effluent stream from step (e) into the bottom section of the secondary sponge absorber; and (j) passing liquid reaction product from step (e) with sponge oil liquid to the main fractionation column separation step (a) for recovery therein.