Process for the preparation of ethylene glycol

Claim 2

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of an oxalate ester having the formula ##STR3## wherein R is an alkyl or aralkyl group which may contain substituents which would not interfere with the reaction, said oxalate ester having a sulfur content of less then 0.4 ppm, with an essentially sulfur-free hydrogen at a pressure of between about 15 psia and 1000 psia, the molar ratio of hydrogen to oxalate ester in the reaction being from 4:1 to 30:1, at a temperature in the range of about 150° C. and 300° C., and at a space velocity between about 3000 hr -1 and 20,000 hr -1 and a liquid hourly space velocity of between about 0.001 hr -1 and 5.0 hr -1 in the presence of an effective amount of a copper-containing hydrogenation catalyst which catalyst has been subjected to a prereduction in hydrogen at a temperature of from about 100° C. to 450° C. and at a hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.

Claim 3

A process according to claim 1 wherein the oxalate ester is selected from the group consisting of dimethyl oxalate, diethyl oxalate and dibutyl oxalates.

Claim 4

A process according to claim 1 wherein the reaction is carried out at a temperature in the range of about 200° C. to 230° C.

Claim 5

A process according to claim 1 wherein the reaction is carried out at a pressure of between about 150 psia and 475 psia.

Claim 6

A process according to claim 1 wherein the space velocity is between about 8000 hr -1 and 15,000 hr -1 .

Claim 7

A process according to claim 1 wherein the liquid hourly space velocity is between 1.0 hr -1 and 3.5 hr -1 .

Claim 8

A process according to claim 1 wherein the hydrogenation catalyst is selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts.

Claim 9

A process according to claim 1 wherein the catalyst is diluted with an inert support material.

Claim 10

A process according to claim 8 wherein the inert support material is selected from the group consisting of alumina, silica and glass beads.

Claim 11

A process according to claim 1 wherein the hydrogenation catalyst is periodically purged with hydrogen at reaction conditions.

Claim 12

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of a diethyl oxalate having a sulfur content of less than 0.4 ppm, with an essentially sulfurfree hydrogen, at a molar ratio of hydrogen to diethyl oxalate of from 4:1 to 30:1 and which mixture is preheated in order to vaporize said oxalate, at a pressure of between about 150 psia and 475 psia, a temperature in the range of about 200° C. to 230° C., a space velocity between about 8000 hr -1 and 15,000 hr -1 and a liquid hourly space velocity of between about 1.0 hr -1 and 3.5 hr -1 in the presence of an effective amount of a hydrogenation catalyst selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts said hydrogenation catalyst having been prereduced in hydrogen at a temperature of from about 100° C. to 450° C. and at hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.

Claim 13

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of a diethyl oxalate having a sulfur content of less than 0.4 ppm, with an essentially sulfurfree hydrogen, at a molar ratio of hydrogen to diethyl oxalate of from 4:1 to 30:1 and which mixture is preheated in order to vaporize said oxalate, at a pressure of between about 150 psia and 475 psia, a temperature in the range of about 200° C. to 230° C., a space velocity between about 8000 hr -1 and 15,000 hr -1 and a liquid hourly space velocity of between about 1.0 hr -1 and 3.5 hr -1 in the presence of an effective amount of a hydrogenation catalyst selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts said hydrogenation catalyst having been prereduced in hydrogen at a temperature of from about 100° C. to 450° C. and at hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.

Claim 14

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of a dibutyl oxalate having a sulfur content of less than 0.4 ppm, with an essentially sulfurfree hydrogen, at a molar ratio of hydrogen to dibutyl oxalate of from 4:1 to 30:1 and which mixture is preheated in order to vaporize said oxalate, at a pressure of between about 150 psia and 475 psia, a temperature in the range of about 200° C. to 230° C., a space velocity between about 8000 hr -1 and 15,000 hr -1 and a liquid hourly space velocity of between about 1.0 hr -1 and 3.5 hr -1 in the presence of an effective amount of a hydrogenation catalyst selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts said hydrogenation catalyst having been prereduced in hydrogen at a temperature of from about 100° C. to 450° C. and at hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.

Claim 15

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of a dibutyl oxalate having a sulfur content of less than 0.4 ppm, with an essentially sulfurfree hydrogen, at a molar ratio of hydrogen to dibutyl oxalate of from 4:1 to 30:1 and which mixture is preheated in order to vaporize said oxalate, at a pressure of between about 150 psia and 475 psia, a temperature in the range of about 200° C. to 230° C., a space velocity between about 8000 hr -1 and 15,000 hr -1 and a liquid hourly space velocity of between about 1.0 hr -1 and 3.5 hr -1 in the presence of an effective amount of a hydrogenation catalyst selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts said hydrogenation catalyst having been prereduced in hydrogen at a temperature of from about 100° C. to 450° C. and at hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.

Claim 16

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of a dimethyl oxalate having a sulfur content of less than 0.4 ppm, with an essentially sulfur-free hydrogen, at a molar ratio of hydrogen to dimethyl oxalate of from 4:1 to 30:1 and which mixture is preheated in order to vaporize said oxalate, at a pressure of between about 150 psia and 475 psia, a temperature in the range of about 200° C. to 230° C., a space velocity between about 8000 hr -1 and 15,000 hr -1 and a liquid hourly space velocity of between about 1.0 hr -1 and 3.5 hr -1 in the presence of an effective amount of a hydrogenation catalyst selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts said hydrogenation catalyst having been prereduced in hydrogen at a temperature of from about 100° C. to 450° C. and at hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.

Claim 17

A process for the preparation of ethylene glycol which comprises reacting under vapor phase conditions a gaseous mixture of a dimethyl oxalate having a sulfur content of less than 0.4 ppm, with an essentially sulfur-free hydrogen, at a molar ratio of hydrogen to dimethyl oxalate of from 4:1 to 30:1 and which mixture is preheated in order to vaporize said oxalate, at a pressure of between about 150 psia and 475 psia, a temperature in the range of about 200° C. to 230° C., a space velocity between about 8000 hr -1 and 15,000 hr -1 and a liquid hourly space velocity of between about 1.0 hr -1 and 3.5 hr -1 in the presence of an effective amount of a hydrogenation catalyst selected from the group consisting of copper zinc chromite, copper chromite, copper barium chromite, and sodium hydroxide-promoted copper chromite catalysts said hydrogenation catalyst having been prereduced in hydrogen at a temperature of from about 100° C. to 450° C. and at hydrogen pressures of from about 0.01 to 10 atmospheres, and recovering the ethylene glycol.