Dimeric carbonylation of 1,3-butadiene

Claim 2

A process for producing and recovering alkyl nonadienoate which comprises the steps of (1) reacting 1,3-butadiene with carbon monoxide and a water-soluble alkanol containing between about 0.5-10 weight percent of water, in the presence of a catalyst complex of palladium and tertiary phosphine ligand, to yield a liquid phase product mixture containing alkyl nonadienoate; (2) contacting the product mixture with a hydrocarbon solvent to form two liquid phases; and (3) separating the two liquid phases, and recovering alkyl nonadienoate from the hydrocarbon solvent phase.

Claim 3

A process in accordance with claim 1 wherein the tertiary phosphine ligand has a ΔHNP between about 70-350, and a steric parameter θ between about 136°-190°.

Claim 4

A process for producing and recovering alkyl nonadienoate which comprises the steps of (1) reacting 1,3-butadiene with at least molar equivalents of carbon monoxide and water-soluble alkanol in the presence of a hydrocarbon solvent and a catalytic quantity of a complex of palladium and tertiary phosphine ligand, at a temperature between about 30° C. and 150° C. and a pressure between about 200 and 3000 psi, to yield a reaction mixture containing alkyl nonadienoate; (2) adjusting the relative quantities of hydrocarbon solvent and alkanol in the reaction mixture, and adding water as required, sufficient to provide a hydrocarbon solvent phase and an alkanol phase containing between about 0.5-10 percent of water; and (3) separating the two phases and recovering alkyl nonadienoate from the hydrocarbon solvent phase.

Claim 5

A process for producing and recovering alkyl nonadienoate which comprises the steps of (1) reacting 1,3-butadiene with at least molar equivalents of carbon monoxide and water-soluble alkanol in the presence of a hydrocarbon solvent and a catalytic quantity of a complex of palladium and tertiary phosphine ligand, at a temperature between about 30° C. and 150° C. and a pressure between about 200 and 3000 psi, to yield a reaction mixture containing alkyl nonadienoate; (2) adjusting the relative quantities of hydrocarbon solvent and alkanol in the reaction mixture, and adding water as required, sufficient to provide a hydrocarbon solvent phase and an alkanol phase containing between about 0.5-10 percent of water; and (3) separating the two phases and recovering alkyl nonadienoate from the hydrocarbon solvent phase.

Claim 6

A process in accordance with claim 3 wherein the dimeric carbonylation of the 1,3-butadiene proceeds in a substantially homogeneous liquid phase reaction medium.

Claim 7

A process in accordance with claim 3 wherein the water-soluble alkanol contains between 1 and about 5 carbon atoms and between 1 and about 4 hydroxyl groups.

Claim 8

A process in accordance with claim 3 wherein the water-soluble alkanol is methanol.

Claim 9

A process in accordance with claim 3 wherein the water-soluble alkanol is ethanol.

Claim 10

A process in accordance with claim 3 wherein the water-soluble alkanol is ethylene glycol.

Claim 11

A process in accordance with claim 3 wherein the water-soluble alkanol is 1,4-butanediol.

Claim 12

A process in accordance with claim 3 wherein the water-soluble alkanol is pentaerythritol.

Claim 13

A process in accordance with claim 3 wherein the hydrocarbon solvent is selected from acyclic and cyclic paraffins containing between 3 and about 8 carbon atoms.

Claim 14

A process in accordance with claim 3 wherein the molar ratio of butadiene to catalyst complex of palladium and tertiary phosphine ligand is at least 25:1.

Claim 15

A process in accordance with claim 3 wherein the palladium and tertiary phosphine ligand in the reaction medium are in a ratio between about 2-8 moles of tertiary phosphine ligand per gram atom of palladium metal.

Claim 16

A process in accordance with claim 3 wherein the tertiary phosphine ligand is trialkylphosphine.

Claim 17

A process in accordance with claim 14 wherein the trialkylphosphine is triisopropylphosphine.

Claim 18

A process in accordance with claim 14 wherein the trialkylphosphine is tri-n-butylphosphine.

Claim 19

A process in accordance with claim 14 wherein the trialkylphosphine is triisobutylphosphine.

Claim 20

A process in accordance with claim 14 wherein the trialkylphosphine is tri-secondary-butylphosphine.

Claim 21

A process in accordance with claim 3 wherein the tertiary phosphine ligand in the catalyst complex comprises between about 70 and 99 mole percent trialkylphosphine and between about 1 and 30 mole percent triarylphosphine.

Claim 22

A process in accordance with claim 19 wherein the trialkylphosphine is triisopropylphosphine and the triarylphosphine is triphenylphosphine.

Claim 23

A process in accordance with claim 3 wherein a vinyl polymerization inhibitor is present in the step (1) reaction medium.

Claim 24

A process in accordance with claim 3 wherein the tertiary phosphine ligand has a ΔHNP between about 70-350, and a steric parameter θ between about 136°-190°.

Claim 25

A process in accordance with claim 3 wherein the separate alkanol phase recovered in step (3) is recycled in the process.

Claim 26

A process in accordance with claim 23 wherein the alkanol phase is extracted with hydrocarbon solvent to remove residual alkyl nonadienoate before the alkanol phase is recycled in the process.

Claim 27

A process in accordance with claim 3 wherein the hydrocarbon solvent recovered in step (3) is recycled in the process.

Claim 28

A process in accordance with claim 25 wherein the hydrocarbon solvent phase is extracted with water-soluble alkanol to remove residual catalyst complex before the respective alkyl nonadienoate and hydrocarbon solvent components of the hydrocarbon solvent phase are separately recovered, and the hydrocarbon solvent is recycled in the process.

Claim 29

A process in accordance with claim 3 wherein the conversion of 1,3-butadiene is at least 80 percent and the selectivity to alkyl nonadienoate and nonadienoic acid product is at least 80 mole percent.

Claim 30

A process in accordance with claim 3 wherein the alkyl nonadienoate product comprises a mixture of alkyl 3,8-nonadienoate and alkyl 2,8-nonadienoate.

Claim 31

A process in accordance with claim 28 wherein the molar ratio of alkyl 3,8-nonadienoate to alkyl 2,8-nonadienoate is at least 4:1.

Claim 32

A continuous process for producing and recovering alkyl nonadienoate which comprises the steps of (1) continuously charging and substantially filling an elongated reactor with a liquid phase reaction medium comprising water-soluble alkanol having a water content of between about 0.5-10 weight percent; (2) maintaining the reactor contents at a temperature between about 50° C. and 140° C. and under a partial pressure between about 100 and 1000 psi of carbon monoxide; (3) continuously introducing 1,3-butadiene and hydrocarbon solvent into the first end of the reactor; (4) continuously withdrawing hydrocarbon solvent as a separate phase from the second end of the reactor; (5) continuously separating alkyl nonadienoate product from the withdrawn hydrocarbon solvent phase; and (6) continuously recycling recovered hydrocarbon solvent to step (2) of the process.

Claim 33

A continuous process for producing and recovering alkyl nonadienoate which comprises the steps of (1) continuously charging and substantially filling an elongated reactor with a liquid phase reaction medium comprising water-soluble alkanol having a water content of between about 0.5-10 weight percent; (2) maintaining the reactor contents at a temperature between about 50° C. and 140° C. and under a partial pressure between about 100 and 1000 psi of carbon monoxide; (3) continuously introducing 1,3-butadiene and hydrocarbon solvent into the first end of the reactor; (4) continuously withdrawing hydrocarbon solvent as a separate phase from the second end of the reactor; (5) continuously separating alkyl nonadienoate product from the withdrawn hydrocarbon solvent phase; and (6) continuously recycling recovered hydrocarbon solvent to step (2) of the process.

Claim 34

A continuous process in accordance with claim 30 wherein the liquid phase reaction medium comprises a mixture of water-soluble alkanol and unreactive water-soluble diluent, and between about 0.5-10 weight percent of water, based on the total weight of the liquid phase reaction medium.

Claim 35

A continuous process in accordance with claim 30 wherein aqueous alkanol as a separate phase is continuously withdrawn from the second end of the reactor and recycled to step (1) of the process.