Abstract: The invention relates to a method for producing vinyl acetate, said method being characterized in that a) the gaseous product mixture leaving the reactor is cooled to a temperature of 100° C. to 120° C. using one or more heat exchangers, b) the thus obtained product mixture is supplied to a distillation column which is equipped with filling elements (pre-dehydration column), c) the pre-dehydration column head product which substantially contains wafer, vinyl acetate, and ethylene is cooled, and the condensate (head product condensate) produced in the process is separated into a water phase and an organic phase (vinyl acetate phase), which substantially comprises vinyl acetate, in a phase separator, d) at least 99 wt. % of the acetic acid contained in the product mixture is separated via the bottom of the pre-dehydration column, and the head product of the pre-dehydration column contains <0.1 wt.

Abstract: The invention relates to a method for producing vinyl acetate, said method being characterized in that a) the gaseous product mixture leaving the reactor is cooled to a temperature of 100° C. to 120° C. using one or more heat exchangers, b) the thus obtained product mixture is supplied to a distillation column which is equipped with filling elements (pre-dehydration column), c) the pre-dehydration column head product which substantially contains wafer, vinyl acetate, and ethylene is cooled, and the condensate (head product condensate) produced in the process is separated into a water phase and an organic phase (vinyl acetate phase), which substantially comprises vinyl acetate, in a phase separator, d) at least 99 wt. % of the acetic acid contained in the product mixture is separated via the bottom of the pre-dehydration column, and the head product of the pre-dehydration column contains <0.1 wt.

Abstract: Vinyl acetate is prepared by a) continuous gas-phase reaction of ethylene, acetic acid and oxygen at 1 to 30 bar and 130° C. to 200° C., the process heat being removed by heat exchange with water at 120° C. to 185° C. and 1 to 10 bar, b) the product gas stream consisting essentially of ethylene, vinyl acetate, acetic acid, water, carbon dioxide and further inert gases is fractionated, and c) all or part of the ethylene is recycled to the recycle gas process, wherein all or part of steam formed in the gas-phase reaction by heat exchange, with a temperature of from 120° C. to 185° C. and pressure of from 1 to 10 bar, is compressed by a differential pressure of at least 0.5 bar and used further.

Abstract: Vinyl acetate is prepared by a) continuous gas-phase reaction of ethylene, acetic acid and oxygen at 1 to 30 bar and 130° C. to 200° C., the process heat being removed by heat exchange with water at 120° C. to 185° C. and 1 to 10 bar, b) the product gas stream consisting essentially of ethylene, vinyl acetate, acetic acid, water, carbon dioxide and further inert gases is fractionated, and c) all or part of the ethylene is recycled to the recycle gas process, wherein all or part of steam formed in the gas-phase reaction by heat exchange, with a temperature of from 120° C. to 185° C. and pressure of from 1 to 10 bar, is compressed by a differential pressure of at least 0.5 bar and used further.

Abstract: A process and apparatus for hydrolytic cleavage of carboxylic esters and water into carboxylic acid and alcohol hydrolysis products. In the process, a portion of water required for hydrolysis is replaced by a recycled mixture of carboxylic acid and water from previously hydrolyzed carboxylic ester.

Abstract: A process and apparatus for hydrolytic cleavage of carboxylic esters and water into carboxylic acid and alcohol hydrolysis products. In the process, a portion of water required for hydrolysis is replaced by a recycled mixture of carboxylic acid and water from previously hydrolyzed carboxylic ester.

Abstract: A process and a device for the catalytic hydrolysis of a carboxylate, e.g., methyl acetate, ethyl acetate, i- or n-propyl acetate, i- or n-butyl acetate, allyl acetate and methyl formate, into the corresponding carboxylic acid and alcohol, by a combination of a pre-reactor and a reactive distillation column are disclosed. By the combination of a pre-reactor and a reactor distillation column, the conversion ratio can be substantially improved. The device can compensate for fluctuations in the supply quantity or in the composition of the feed flow. The product composition can also be controlled in a wide range.