Abstract: The apparatus for the esterification of a fatty acid F includes a column with a packing. In addition to functioning as a catalytic reactor, the packing functions as a stripping section. A heteregenous catalysis of a fatty acid is carried out with an alcohol used in the same molar ratio or in excess. A gaseous alcohol-rich counter-flow is produced in a sump of the column by vaporization. Water is removed from the reaction zone by means of the counter-flow acting as a stripping gas. The loaded stripping gas is at least partially liquefied at the head of the column. The head product is separated into a water-rich fraction as well as an alcohol-rich fraction. The alcohol-rich fraction is returned to the process as a starting material for the esterification and for the production of the stripping gas.

Abstract: Carboxylic acid ester is produced by esterification of carboxylic acid and an alcohol in a catalytic reaction zone of a first column at a pressure not greater than ambient pressure. The resultant sump product is distilled in a reaction zone of a second column at a pressure greater than 1.5 bar to obtain a second liquid sump product containing carboxylic acid ester with an carboxylic acid content of less than 100 ppm by weight at a lower end of the column. Neutralization of the second liquid sump product with a base is not required.

Abstract: The invention relates to an apparatus for the production of butylacetate by esterification of acetic acid with butanol in the presence of a solid acidic catalyst in which distillatory separation of components runs simultaneously with esterification. Thus, acetic acid and butanol are introduced in defined amounts and in the molar ratio 1:1 to 1:10 into a system, in which the reaction and the distillatory separation proceeds in three zones. The reaction together with distillatory separation of the components with different boiling points run in the reaction zone, while only distillation takes place in lower and upper separation zones. A volatile mixture is separated in the upper separation zone, from which, after being cooled at 5 to 80° C., water and organic phases are separated, the latest being refluxed into the system. The ratio of the feed amount to the organic phase reflux amount is 1:1 to 1:20, the reflux amount representing 60 to 100% of the whole amount of the organic phase.

Abstract: The PLANT for the esterification of a fatty acid F includes a column with a packing. In addition to functioning as a catalytic reactor, the packing functions as a stripping section. A heteregenous catalysis of a fatty acid is carried out with an alcohol used in the same molar ratio or in excess. A gaseous alcohol-rich counter-flow is produced in a sump of the column by vaporisation. Water is removed from the reaction zone by means of the counter-flow acting as a stripping gas. The loaded stripping gas is at least partially liquefied at the head of the column. The head product is separated into a water-rich fraction as well as an alcohol-rich fraction. The alcohol-rich fraction is returned to the process as a starting material for the esterification and for the production of the stripping gas.

Abstract: The method for the esterification of a fatty acid F is carried out in a column with a packing. In addition to functioning as a catalytic reactor, the packing functions as a stripping section. A heteregenous catalysis of a fatty acid is carried out with an alcohol used in the same molar ratio or in excess. A gaseous alcohol-rich counter-flow is produced in a sump of the column by vaporization. Water is removed from the reaction zone by means of the counter-flow acting as a stripping gas. The loaded stripping gas is at least partially liquefied at the head of the column. The head product is separated into a water-rich fraction as well as an alcohol-rich fraction. The alcohol-rich fraction is returned to the process as a starting material for the esterification and for the production of the stripping gas.

Abstract: Carboxylic acid ester is produced by esterification of carboxylic acid and an alcohol in a catalytic reaction zone of a first column at a pressure not greater than ambient pressure. The resultant sump product is distilled in a reaction zone of a second column at a pressure greater than 1.5 bar to obtain a second liquid sump product containing carboxylic acid ester with an carboxylic acid content of less than 100 ppm by weight at a lower end of the column. Neutralization of the second liquid sump product with a base is not required.

Abstract: The method for the esterification of a fatty acid F is carried out in a column with a packing. In addition to functioning as a catalytic reactor, the packing functions as a stripping section. A heteregenous catalysis of a fatty acid is carried out with an alcohol used in the same molar ratio or in excess. A gaseous alcohol-rich counter-flow is produced in a sump of the column by vaporisation. Water is removed from the reaction zone by means of the counter-flow acting as a stripping gas. The loaded stripping gas is at least partially liquefied at the head of the column. The head product is separated into a water-rich fraction as well as an alcohol-rich fraction. The alcohol-rich fraction is returned to the process as a starting material for the esterification and for the production of the stripping gas.

Abstract: The invention relates to a process of butylacetate production by esterification of acetic acid with butanol in the presence of a solid acidic catalyst in which distillatory separation of components runs simultaneously with esterification. Thus, acetic acid and butanol are introduced in defined amounts and in the molar ratio 1:1 to 1:10 into a system, in which the reaction and the distillatory separation proceeds in three zones. The reaction together with distillatory separation of the components with different boiling points run in the reaction zone, while only distillation takes place in lower and upper separation zones. A volatile mixture is separated in the upper separation zone, from which, after being cooled at 5 to 80 ° C. water and organic phases are separated, the latest being refluxed into the system. The ratio of the feed amount to the organic phase reflux amount is 1:1 to 1:20, the reflux amount representing 60 to 100 % of the whole amount of the organic phase.

Abstract: The invention relates to a process of butylacetate production by esterification of acetic acid with butanol in the presence of a solid acidic catalyst in which distillatory separation of components runs simultaneously with esterification. Thus, acetic acid and butanol are introduced in defined amounts and in the molar ratio 1:1 to 1:10 into a system, in which the reaction and the distillatory separation proceeds in three zones. The reaction together with distillatory separation of the components with different boiling points run in the reaction zone, while only distillation takes place in lower and upper separation zones. A volatile mixture is separated in the upper separation zone, from which, after being cooled at 5 to 80° C., water and organic phases are separated, the latest being refluxed into the system. The ratio of the feed amount to the organic phase reflux amount is 1:1 to 1:20, the reflux amount representing 60 to 100% of the whole amount of the organic phase.