Method for separating ethylene glycol (EG) and ethylene glycol diacetate (EGDA) with sulfolane entrainer, including: obtaining EG and a mixture of EGDA and sulfolane through separating a mixture of EG and EGDA under an action of sulfolane by an extractive distillation tower; obtaining EGDA and sulfolane through separating the mixture of the EGDA and the sulfolane by an entrainer recovery tower; and obtaining recycled sulfolane through cooling the sulfolane by a heat exchanger, and mixing the recycled sulfolane with fresh sulfolane and circulating into the extractive distillation tower for recycling. Through the method, a yield of the EG is greater than or equal to 99.50% and a mass purity of the EG is greater than or equal to 99.50%, and a yield of the EGDA is greater than or equal to 99.80% and a mass purity of the EGDA is greater than or equal to 99.90%.

Method for separating ethylene glycol (EG) and ethylene glycol diacetate (EGDA) with sulfolane entrainer, including: obtaining EG and a mixture of EGDA and sulfolane through separating a mixture of EG and EGDA under an action of sulfolane by an extractive distillation tower; obtaining EGDA and sulfolane through separating the mixture of the EGDA and the sulfolane by an entrainer recovery tower; and obtaining recycled sulfolane through cooling the sulfolane by a heat exchanger, and mixing the recycled sulfolane with fresh sulfolane and circulating into the extractive distillation tower for recycling. Through the method, a yield of the EG is greater than or equal to 99.50% and a mass purity of the EG is greater than or equal to 99.50%, and a yield of the EGDA is greater than or equal to 99.80% and a mass purity of the EGDA is greater than or equal to 99.90%.

Method for separating ethylene glycol (EG) and ethylene glycol diacetate (EGDA) with sulfolane entrainer, including: obtaining EG and a mixture of EGDA and sulfolane through separating a mixture of EG and EGDA under an action of sulfolane by an extractive distillation tower; obtaining EGDA and sulfolane through separating the mixture of the EGDA and the sulfolane by an entrainer recovery tower; and obtaining recycled sulfolane through cooling the sulfolane by a heat exchanger, and mixing the recycled sulfolane with fresh sulfolane and circulating into the extractive distillation tower for recycling. Through the method, a yield of the EG is greater than or equal to 99.50% and a mass purity of the EG is greater than or equal to 99.50%, and a yield of the EGDA is greater than or equal to 99.80% and a mass purity of the EGDA is greater than or equal to 99.90%.

A process for the recovery of substantially dry ethanol from a feedstock comprising ethyl acetate, ethanol and water, said process comprising: (a) passing said feedstock to a first separation column which includes a first separation column reboiler, and is maintained under distillation conditions to form an intermediate bottom stream comprising ethanol and water and having a higher ethanol concentration than the ethanol concentration in said feedstock; (b) passing said intermediate bottom stream to an azeotrope column maintained under distillation conditions to form an azeotrope column bottom stream, and an azeotrope column overhead stream which comprises ethanol and water; (c) feeding an ethanol make-up stream into said azeotrope column; (d) passing said azeotrope column overhead stream through a water removal section for separating water from ethanol to form a substantially dry ethanol stream; (e) using said substantially dry ethanol stream to provide heat in said first separation column reboiler.

A process for the recovery of substantially dry ethanol from a feedstock comprising ethyl acetate, ethanol and water, said process comprising: (a) passing said feedstock to a first separation column which includes a first separation column reboiler, and is maintained under distillation conditions to form an intermediate bottom stream comprising ethanol and water and having a higher ethanol concentration than the ethanol concentration in said feedstock; (b) passing said intermediate bottom stream to an azeotrope column maintained under distillation conditions to form an azeotrope column bottom stream, and an azeotrope column overhead stream which comprises ethanol and water; (c) feeding an ethanol make-up stream into said azeotrope column; (d) passing said azeotrope column overhead stream through a water removal section for separating water from ethanol to form a substantially dry ethanol stream; (e) using said substantially dry ethanol stream to provide heat in said first separation column reboiler.

According to an embodiment, a method for producing a (hydro)halocarbon includes a step of purifying the (hydro)halocarbon by reduced-pressure distillation of an azeotropic or azeotropic-like composition containing the (hydro)halocarbon and a compound different from the (hydro)halocarbon. According to another embodiment, a method for producing a (hydro)halocarbon includes a step purifying the (hydro)halocarbon by reduced-pressure distillation of an azeotropic or azeotropic-like composition containing the (hydro)halocarbon and a compound different from the (hydro)halocarbon, wherein standard boiling points of both the (hydro)halocarbon and the compound are 80 C. or lower.

According to an embodiment, a method for producing a (hydro)halocarbon includes a step of purifying the (hydro)halocarbon by reduced-pressure distillation of an azeotropic or azeotropic-like composition containing the (hydro)halocarbon and a compound different from the (hydro)halocarbon. According to another embodiment, a method for producing a (hydro)halocarbon includes a step purifying the (hydro)halocarbon by reduced-pressure distillation of an azeotropic or azeotropic-like composition containing the (hydro)halocarbon and a compound different from the (hydro)halocarbon, wherein standard boiling points of both the (hydro)halocarbon and the compound are 80 C. or lower.

According to an embodiment, a method for producing a (hydro)halocarbon includes a step of purifying the (hydro)halocarbon by reduced-pressure distillation of an azeotropic or azeotropic-like composition containing the (hydro)halocarbon and a compound different from the (hydro)halocarbon. According to another embodiment, a method for producing a (hydro)halocarbon includes a step purifying the (hydro)halocarbon by reduced-pressure distillation of an azeotropic or azeotropic-like composition containing the (hydro)halocarbon and a compound different from the (hydro)halocarbon, wherein standard boiling points of both the (hydro)halocarbon and the compound are 80 C. or lower.

The invention relates to a process for extracting alcohols from an initial mixture (1) comprising alcohols in aqueous phase, with: a distillative separation by an isopropanol-butanol distillation column (III) equipped at the top with a condenser (c3), intended for separating said mixture into a water-isopropanol azeotrope stream (6) at the top and into a water-butanol azeotrope stream (7) at the bottom, a distillative separation intended for separating the water-butanol azeotrope stream into water and butanol, by a hetero-azeotropic distillation system comprising at least one water-recovering water column (IV) and at least one butanol (9)-recovering butanol column (V) equipped with a reboiler (r5),
such that a heat transfer is performed from the top water-isopropanol azeotrope stream (6) entering the condenser of the isopropanol-butanol distillation column (III), to the stream entering the reboiler of the butanol column (V).

The invention relates to a process for extracting alcohols from an initial mixture (1) comprising alcohols in aqueous phase, with: a distillative separation by an isopropanol-butanol distillation column (III) equipped at the top with a condenser (c3), intended for separating said mixture into a water-isopropanol azeotrope stream (6) at the top and into a water-butanol azeotrope stream (7) at the bottom, a distillative separation intended for separating the water-butanol azeotrope stream into water and butanol, by a hetero-azeotropic distillation system comprising at least one water-recovering water column (IV) and at least one butanol (9)-recovering butanol column (V) equipped with a reboiler (r5),
such that a heat transfer is performed from the top water-isopropanol azeotrope stream (6) entering the condenser of the isopropanol-butanol distillation column (III), to the stream entering the reboiler of the butanol column (V).