Method for oligomerization of ethylene
The present invention relates to a method for oligomerization of ethylene, comprising the steps: a) feeding ethylene, solvent and a catalyst composition comprising catalyst and cocatalyst into a reactor, b) oligomerizing ethylene in the reactor, c) discharging a reactor effluent comprising linear alpha-olefins including 1-butene, solvent, unconsumed ethylene dissolved in the reactor effluent, and catalyst composition from the reactor, d) separating ethylene and 1-butene collectively from the remaining reactor effluent, and e) recycling at least a part of the ethylene and the 1-butene separated in step d) into the reactor.
1. A method for oligomerization of ethylene, comprising the steps:
a) feeding ethylene, solvent and a catalyst composition comprising catalyst and cocatalyst into a reactor,
b) oligomerizing ethylene in the reactor,
c) discharging a reactor effluent comprising linear alpha-olefins including C 6+ linear alpha olefins and 1-butene, solvent, unconsumed ethylene dissolved in the reactor effluent, and catalyst composition from the reactor,
d) separating ethylene and 1-butene collectively from the remaining reactor effluent comprising the C 6+ linear alpha olefins, and
e) recycling at least a part of the ethylene and the 1-butene separated in step d) into the reactor; and
wherein a constant 1-butene content is in the reactor.
2. Method according to claim 1 , wherein the recycling stream of ethylene and 1-butene of step e) is purged at least partly by a purge stream.
3. The method according to claim 1 , wherein step b) is carried out at a temperature of 10-100° C. and/or a pressure of about 10-100 bar.
4. The method according to claim 1 , wherein additional 1-butene is fed into the reactor, from an external source at an initial start-up period of the method for oligomerization.
5. The method according to claim 1 , wherein the separation of step d) is carried out at a pressure below reaction pressure of step b).
6. The method according to claim 1 , wherein ethylene and 1-butene are recycled into the reactor in liquid form.
7. The method according to claim 1 , which is a trimerisation.
8. The method according to claim 1 , wherein the catalyst composition comprises a catalyst comprising a chromium compound and a ligand of the general structure (A) R 1 R 2 P—N(R 3 )—P(R 4 )—N(R 5 )—H or (B) R 1 R 2 P—N(R 3 )—P(R 4 )—N(R 5 )—PR 6 R 7 , wherein R 1 -R 7 are independently selected from halogen, amino, trimethylsilyl, C 1 -C 10 -alkyl, C 6 -C 20 aryl or any cyclic derivatives of (A) and (B), wherein at least one of the P or N atoms of the PNPN-unit or PNPNP-unit is a member of a ring system, the ring system being formed from one or more constituent compounds of structures (A) or (B) by substitution.
9. The method according to claim 8 , wherein the chromium compound is selected from organic or inorganic salts, coordination complexes and organometallic complexes of Cr(II) or Cr(III).
10. The method according to claim 1 , wherein the co-catalyst is selected from trimethylaluminum, triethylaluminum, triisopropylaluminum, triisobutyl-aluminum, ethylaluminumsesquichloride, diethylaluminumchloride, ethylaluminumdichloride, methylaluminoxane (MAO) or mixtures thereof.
11. The method according to claim 1 , wherein the catalyst composition additionally comprises a modifier containing organic or inorganic halide.
12. The method according to claim 8 , wherein the ligand is selected from Ph 2 P—N(i-Pr)—P(Ph)—N(i-Pr)—H, Ph 2 P—N(i-Pr)—P(Ph)—N(Ph)-H, Ph 2 P—N(i-Pr)—P(Ph)—N(tert-butyl)-H and Ph 2 P—N(i-Pr)—P(Ph)—N(CH(CH 3 )(Ph))—H.
13. The method according to claim 1 , wherein the solvent is selected from aromatic hydrocarbons, straight chain and cyclic aliphatic hydrocarbons, and ethers.
14. The method according to claim 13 , wherein the solvent is selected from toluene, benzene, ethylbenzene, cumene, xylenes, mesitylene, hexane, octane, cyclohexane, methylcyclohexane, diethylether, tetrahydrofurane, and mixtures thereof.
15. The method according to claim 13 , wherein the solvent is toluene.
16. The method according to claim 1 , wherein the amount of 1-butene in the reactor is at least 5 percent, based on the total weight of liquids in the reactor.
17. The method according to claim 1 , wherein the amount of 1-butene in the reactor is at least 10 percent, based on the total weight of liquids in the reactor.
18. The method according to claim 1 , wherein the amount of 1-butene in the reactor is at least 25 percent, based on the total weight of liquids in the reactor.
19. The method according to claim 8 , wherein the chromium compound is CrCl 3 (THF) 3 , Cr(III)acetyl acetonate, Cr(III)octanoate, chromium hexacarbonyl, Cr(III)-2-ethylhexanoate, benzene(tricarbonyl)-chromium or Cr(III)chloride.
20. The method according to claim 1 , wherein the amount of 1-butene in the reactor is at least 1 weight percent and up to 30 weight percent, based on the total weight of liquids in the reactor.