The present disclosure provides a control method for a rectification and purification system of electronic-grade chlorine trifluoride. A rectification device of electronic-grade chlorine trifluoride includes a two-stage cryogenic rectification device including a low-boiling column and a high-boiling column. An extraction agent is arranged in the two-stage cryogenic rectification device for further dissociating associated molecules of hydrogen fluoride and chlorine trifluoride to meet the requirements of electronic-grade chlorine trifluoride. The reflux ratio parameter stability of a vapor-liquid (chlorine trifluoride-hydrogen fluoride) phase equilibrium system can be effectively improved by a column plate temperature control method, thus realizing wide dynamic smooth running under various working conditions. The column plate temperature control method can achieve an effective separation of chlorine trifluoride and various impurity components by deep rectification technology, yielding electronic-grade chlorine trifluoride through purification.

The present disclosure provides a control method for a rectification and purification system of electronic-grade chlorine trifluoride. A rectification device of electronic-grade chlorine trifluoride includes a two-stage cryogenic rectification device including a low-boiling column and a high-boiling column. An extraction agent is arranged in the two-stage cryogenic rectification device for further dissociating associated molecules of hydrogen fluoride and chlorine trifluoride to meet the requirements of electronic-grade chlorine trifluoride. The reflux ratio parameter stability of a vapor-liquid (chlorine trifluoride-hydrogen fluoride) phase equilibrium system can be effectively improved by a column plate temperature control method, thus realizing wide dynamic smooth running under various working conditions. The column plate temperature control method can achieve an effective separation of chlorine trifluoride and various impurity components by deep rectification technology, yielding electronic-grade chlorine trifluoride through purification.

Heterogenous azeotrope or azeotrope-like compositions comprising 2-chloro-3,3,3-trifluoropropene (HFCO-1233xf) and water which may include from about 0.09 wt. % to about 92.69 wt. % 2-chloro-3,3,3-trifluoropropene (HFCO-1233xf) and from about 7.31 wt. % to about 99.91 wt. % water and having a boiling point between about 12.0° C. and about 13.6° C. at a pressure of between about 12.5 psia and about 16.5 psia. The azeotrope or azeotrope-like compositions may be used to separate impurities, including water, from 2-chloro-3,3,3-trifluoropropene (HFCO-1233xf).

Heterogenous azeotrope or azeotrope-like compositions comprising 2-chloro-3,3,3-trifluoropropene (HFCO-1233xf) and water which may include from about 0.09 wt. % to about 92.69 wt. % 2-chloro-3,3,3-trifluoropropene (HFCO-1233xf) and from about 7.31 wt. % to about 99.91 wt. % water and having a boiling point between about 12.0° C. and about 13.6° C. at a pressure of between about 12.5 psia and about 16.5 psia. The azeotrope or azeotrope-like compositions may be used to separate impurities, including water, from 2-chloro-3,3,3-trifluoropropene (HFCO-1233xf).

Continuous acetic acid production with a process to remove and/or reduce permanganate reducing compounds (PRCs), including acetaldehyde. The process involves obtaining a stream comprising the PRCs and removing water from the stream through a dehydrating step, involving distillation, extraction, or phase separation. After removing water, an alkane may be combined to enhance the separation of PRCs from alkyl iodides.

Continuous acetic acid production with a process to remove and/or reduce permanganate reducing compounds (PRCs), including acetaldehyde. The process involves obtaining a stream comprising the PRCs and removing water from the stream through a dehydrating step, involving distillation, extraction, or phase separation. After removing water, an alkane may be combined to enhance the separation of PRCs from alkyl iodides.

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 present disclosure provides a method for producing purified trans-1,2-difluoroethylene (HFO-1132(E)) and/or 1,1,2-trifluoroethylene (HFO-1123), comprising a distillation step of distilling composition 1 comprising difluoromethane (HFC-32) and HFO-1132(E) and/or HFO-1123 to obtain composition 2 in which HFC-32 is reduced from composition 1; and an extractive distillation step of bringing composition 2 into contact with an extraction solvent to obtain a composition comprising HFO-1132(E) and/or HFO-1123, in which HFC-32 is reduced from composition 2, composition 2 being an azeotropic composition or azeotrope-like composition comprising HFC-32 and HFO-1132(E) and/or HFO-1123.