Ester synthesis
Process for making lower aliphatic ester, especially ethyl acetate, by reacting a lower olefin with a saturated lower aliphatic mono-carboxylic acid in the vapor phase using a heteropolyacid catalyst, wherein the reaction pressure is 11 to 20 barg (1100 to 2000 KPa), more preferably 12 to 15 barg (1200 to 1500 KPa). The reaction temperature is 140 to 250° C., more preferably 160 to 195° C. The process reduces the level of by-products, for example methyl ethyl ketone and/or acetaldehyde.
1 - 20 . (canceled)
21 . A process for the production of a lower aliphatic ester comprising reacting a lower olefin with a saturated lower aliphatic mono-carboxylic acid in the vapour phase in the presence of a heteropolyacid catalyst, characterised in that the reaction pressure employed lies in the range 12 to 18 barg (1300 to 1900 KPa).
22 . A process as claimed in claim 21 characterised in that the reaction pressure employed lies in the range preferably in the range 12 to 15 barg (1300 to 1600 KPa).
23 . A process for the production of ethyl acetate by reacting ethylene with acetic acid in the presence of a heteropolyacid catalyst at a temperature in the range 140 to 250° C., wherein the reaction pressure is maintained in the range 12 to 15 barg (1300 to 1600 Kpa).
24 . A process as claimed in claim 21 wherein the heteropolyacid is selected from 12-tungstophosphoric acid, 12-molybdophosphoric acid, 12-tungstosilicic acid and 12-molybdosilicic acid.
25 . A process as claimed in claim 21 or claim 23 wherein the heteropolyacid is supported.
26 . A process as claimed in claim 25 wherein the support is selected from silica, clay, zeolite, ion exchange resins and active carbon.
27 . A process as claimed in claim 26 wherein the support is derived from natural or synthetic amorphous silica.
28 . A process as claimed in claim 26 or 27 wherein the support is made by flame hydrolysis of SiH 4 or SiCl 4 .
29 . A process as claimed in claim 26 or 27 wherein the support is made by precipitation from aqueous silicate solution, or by gelling of silicic acid colloids.
30 . A process as claimed in claim 26 wherein the support has an average particle diameter of 4 to 6 mm.
31 . A process as clamed in claim 21 or 22 wherein the olefin is ethylene, propylene or mixtures thereof.
32 . A process as claimed in claim 21 or 22 wherein the saturated, lower aliphatic mono-carboxylic acid reactant is a C 1 -C 4 carboxylic acid.
33 . A process as claimed in claim 21 or 22 wherein the saturated, lower aliphatic mono-carboxylic acid reactant is acetic acid.
34 . A process as claimed in claim 21 or 22 wherein the mole ratio of olefin to the lower carboxylic acid in the reaction mixture is in the range from 1:1 to 15:1.
35 . A process as claimed in claim 34 wherein the mole ratio of olefin to the lower carboxylic acid in the reaction mixture in the range from 10:1 to 14:1.
36 . A process as claimed in claim 21 or 22 wherein at least some water is used in the reaction mixture.
37 . A process as claimed in claim 36 wherein the amount of water is in the range from 1-10 mole % based on the total amount of olefin, carboxylic acid and water.
38 . A process as claimed in claim 23 wherein the mole ratio of olefin to the lower carboxylic acid in the reaction mixture is in the range from 1:1 to 15:1.
39 . A process as claimed in claim 38 wherein the mole ratio of olefin to the lower carboxylic acid in the reaction mixture in the range from 10:1 to 14:1.
40 . A process as claimed in claim 23 wherein at least some water is used in the reaction mixture.
41 . A process as claimed in claim 40 wherein the amount of water is in the range from 1-10 mole % based on the total amount of olefin, carboxylic acid and water.