Oligomerization reaction system

Claim 2

In the process for the oligomerization of ethylene to linear alpha-olefins wherein (1) ethylene is oligomerized by contact in liquid phase at elevated pressure with a solution of an oligomerization catalyst composition comprising catalytically active nickel complex in a polar organic solvent; (2) at least part of the resulting reaction product is separated at elevated pressure into a liquid solvent phase and a liquid hydrocarbon product phase containing dissolved ethylene, catalyst and solvent; and (3) said product phase is separated into unreacted ethylene and ethylene oligomers, the improvement which comprises scrubbing said hydrocarbon product phase, after separation from the solvent phase and while at sufficiently elevated pressure to maintain said ethylene dissolved therein, with sufficient polar organic solvent to remove the residual amount of catalytically active nickel complex from said product phase.

Claim 3

Process according to claim 1 wherein the solvent employed in said scrubbing step is the same as the solvent employed in the oligomerization reaction.

Claim 4

Process according to claim 2 wherein the solvent extract from said scrubbing step is returned to the oligomerization reaction zone.

Claim 5

Process according to claim 3 wherein said extract is employed in the preparation of additional oligomerization catalyst.

Claim 6

Process according to claim 2 wherein said solvent is 1,4-butanediol.

Claim 7

In the process for the oligomerization of ethylene to linear alpha-olefins wherein 1 a nickel complex catalyst solution in a diol solvent is prepared in a catalyst preparation zone; 2ethylene is contacted with said catalyst solution in a reaction zone at a temperature in the range from about 25° to 150° C at a partial presure of ethylene in the range from 400 to 2,500 psig; 3. a portion of the reaction mixture is continuously removed from the reaction zone and gaseous ethylene separated therefrom for recycle to the reaction zone; 4. at least part of the liquid reaction mixture, after ethylene removal, is separated in a solvent/product separation zone into a liquid solvent phase and a liquid hydrocarbon product phase containing dissolved ethylene, catalyst and solvent; 5. said separated product phase is deethenized; 6. the separated ethylene is recycled to the reactor and; 7. oligomer fractions are recovered from the deethenized product; wherein the system is maintained at substantially superatomspheric pressure, sufficient to maintain dissolved ethylene in solution in the hydrocarbon phase, from the reaction zone through the deethenization zone, the improvement which comprises 1. removing a bleed stream of solvent phase from the solvent/product separation zone and subjecting it in a solvent purification zone to fractionation for recovery of a purified solvent stream; 2. passing the liquid hydrocarbon product stream from said solvent/product phase separation to a scrubbing vessel; 3. in said scrubbing vessel, passing said liquid hydrocarbon product stream countercurrently to a sufficient amount of liquid purified solvent from said solvent purification zone to remove the residual amount of nickel complex from said product stream; 4. recovering solvent, containing catalyst complex, from said scrubbing vessel and returning it to the catalyst preparation zone; 5. deethenizing the catalyst-free product stream recovered from said scrubbing vessel 6. passing the deethenized product to a second scrubbing zone in which it is contacted countercurrently with water to remove residual diol solvent; 7. dehydrating the aqueous solvent stream removed from acid second scrubbing zone and returning resulting dehydrated solvent to said solvent purification zone; and 8. passing the water-scrubbed product to a product work-up zone wherein oligmer fractions are recovered.

Claim 8

In the process for the oligomerization of ethylene to linear alpha-olefins wherein 1 a nickel complex catalyst solution in a diol solvent is prepared in a catalyst preparation zone; 2ethylene is contacted with said catalyst solution in a reaction zone at a temperature in the range from about 25° to 150° C at a partial presure of ethylene in the range from 400 to 2,500 psig; 3. a portion of the reaction mixture is continuously removed from the reaction zone and gaseous ethylene separated therefrom for recycle to the reaction zone; 4. at least part of the liquid reaction mixture, after ethylene removal, is separated in a solvent/product separation zone into a liquid solvent phase and a liquid hydrocarbon product phase containing dissolved ethylene, catalyst and solvent; 5. said separated product phase is deethenized; 6. the separated ethylene is recycled to the reactor and; 7. oligomer fractions are recovered from the deethenized product; wherein the system is maintained at substantially superatomspheric pressure, sufficient to maintain dissolved ethylene in solution in the hydrocarbon phase, from the reaction zone through the deethenization zone, the improvement which comprises 1. removing a bleed stream of solvent phase from the solvent/product separation zone and subjecting it in a solvent purification zone to fractionation for recovery of a purified solvent stream; 2. passing the liquid hydrocarbon product stream from said solvent/product phase separation to a scrubbing vessel; 3. in said scrubbing vessel, passing said liquid hydrocarbon product stream countercurrently to a sufficient amount of liquid purified solvent from said solvent purification zone to remove the residual amount of nickel complex from said product stream; 4. recovering solvent, containing catalyst complex, from said scrubbing vessel and returning it to the catalyst preparation zone; 5. deethenizing the catalyst-free product stream recovered from said scrubbing vessel 6. passing the deethenized product to a second scrubbing zone in which it is contacted countercurrently with water to remove residual diol solvent; 7. dehydrating the aqueous solvent stream removed from acid second scrubbing zone and returning resulting dehydrated solvent to said solvent purification zone; and 8. passing the water-scrubbed product to a product work-up zone wherein oligmer fractions are recovered.

Claim 9

The process according to claim 6 wherein said diol is 1,4-butanediol.