Polyols from scrap polyethylene terephthalate and dimethyl terephthalate process residue

Claim 2

A mixture of liquid terephthalate acid ester polyols that is free from solids upon standing and is prepared by (a) reacting a mixture comprised of scrap polyethylene terephthalate, dimethyl terephthalate process residue and at least two glycols having a molecular weight higher than that of ethylene glycol, in the presence of an esterification/transesterification catalyst, where the mole ratio of glycols to scrap polyethylene terephthalate and dimethyl terephthalate process residue is from about 2:1 to about 6.5:1 and the mole ratio of scrap polyethylene terephthalate to dimethyl terephthalate process residue is from about 96/5 to about 50/50, to yield a reaction product comprising terephthalic acid ester polyols, ethylene glycol and unreacted glycols having a molecular weight higher than that of ethylene glycol, and (b) subsequently removing glycols from the reaction product from step (a) until from about 2% to about 25% by weight glycols are present in said reaction product.

Claim 3

The mixture of polyols of claim 1 wherein the glycols having a molecular weight higher than that of ethylene glycol are a mixture of diethylene glycol, dipropylene glycol and tripropylene glycol.

Claim 4

The mixture of polyols of claim 1 wherein the reaction mixture of step (a) additionally comprises from about 0.1 to about 0.3 moles methyl alpha-d-glucoside per mole of scrap polyethylene terephthalate and dimethyl terephthalate process residue.

Claim 5

The mixture of polyols of claim 1 wherein removal of glycols from the reaction product from step (a) is accomplished by vacuum stripping.

Claim 6

The mixture of polyols of claim 1 wherein the reaction is conducted at a temperature of 150°-250° C.

Claim 7

The mixture of polyols of claim 1 wherein the reaction is conducted at atmospheric pressure.

Claim 8

The mixture of polyols of claim 1 wherein the esterification/transesterification catalyst is zinc oxide.

Claim 9

The mixture of polyols of claim 1 wherein the average hydroxyl number of the mixture of polyols is from about 240 to about 500.

Claim 10

The mixture of polyols of claim 1 wherein the ratio of scrap polyethylene terephthalate to dimethyl terephthalate process residue is about 70/30.

Claim 11

A process for producing a mixture of liquid terephthalic acid ester polyols that is free from solids upon standing comprising (a) reacting a mixture comprised of scrap polyethylene terephthalate, dimethyl terephthalate process residue and at least two glycols having a molecular weight higher than that of ethylene glycol, in the presence of an esterification/transesterification catalyst, where the mole ratio of glycols to scrap polyethylene terephthalate and dimethyl terephthalate process residue is from about 2:1 to about 6.5:1 and the mole ratio of scrap polyethylene terephthalate to dimethyl terephthalate process residue is from about 95/5 to about 50/50, to yield a reaction product comprising terephthalic acid ester polyols, ethylene glycol and unreacted glycols having a molecular weight higher than that of ethylene glycol, and (b) subsequently removing glycols from the reaction product from step (a) until from about 2% to about 25% by weight glycols are present in said reaction product.

Claim 12

A process for producing a mixture of liquid terephthalic acid ester polyols that is free from solids upon standing comprising (a) reacting a mixture comprised of scrap polyethylene terephthalate, dimethyl terephthalate process residue and at least two glycols having a molecular weight higher than that of ethylene glycol, in the presence of an esterification/transesterification catalyst, where the mole ratio of glycols to scrap polyethylene terephthalate and dimethyl terephthalate process residue is from about 2:1 to about 6.5:1 and the mole ratio of scrap polyethylene terephthalate to dimethyl terephthalate process residue is from about 95/5 to about 50/50, to yield a reaction product comprising terephthalic acid ester polyols, ethylene glycol and unreacted glycols having a molecular weight higher than that of ethylene glycol, and (b) subsequently removing glycols from the reaction product from step (a) until from about 2% to about 25% by weight glycols are present in said reaction product.

Claim 13

The process of claim 10 wherein the glycols having a molecular weight higher than ethylene glycol are a mixture of diethylene glycol, dipropylene glycol and tripropylene glycol.

Claim 14

The process of claim 10 wherein the reaction mixture of step (a) additionally comprises from about 0.1 to about 0.3 moles methyl alpha-d-glucoside per mole of scrap polyethylene terephthalate and dimethyl terephthalate process residue.

Claim 15

The process of claim 10 wherein removal of glycols from the reaction product from step (a) is accomplished by vacuum stripping.

Claim 16

The process of claim 10 wherein the reaction is conducted at a temperature of 150°-250° C.

Claim 17

The process of claim 10 wherein the reaction is conducted at atmospheric pressure.

Claim 18

The process of claim 10 wherein the esterification/transesterification catalyst is zinc oxide.

Claim 19

The process of claim 10 wherein the average hydroxyl number of the mixture of polyols is from about 240 to about 500.

Claim 20

The process of claim 10 wherein the ratio of scrap polyethylene terephthalate to dimethyl terephthalate process residue is about 70/30.