The present application relates to methods for the reduction of halogenated hydrocarbons using compounds of Formula (I): ##STR00001##
wherein the reduction of the halogenated compounds is carried out, for example, under ambient conditions without the need for a transition metal containing co-factor. The present application also relates to methods of recovering precious metals using compounds of Formula (I) that are absorbed onto a support material.

The invention discloses a method for the preparation of fluoro alkylated compounds by homogeneous Ni catalyzed fluoro alkylation with fluoro alkyl halides in the presence of a base.

The invention discloses a method for the preparation of fluoro alkylated compounds by homogeneous Ni catalyzed fluoro alkylation with fluoro alkyl halides in the presence of a base.

A process for producing 2,3,3,3-tetrafluoropropene comprises i) in a first adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing hydrofluoric acid into contact, in the gas phase with at least one chlorinated compound in order to produce a stream A comprising 2-chloro-3,3,3-trifluoropropene, ii) in a second adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing the stream A into contact, in the gas phase in the presence of a catalyst, with hydrofluoric acid, to produce a stream B comprising 2,3,3,3-tetrafluoropropene. The temperature at the inlet of the fixed bed of one of said first or second reactors is between 300° C. and 400° C. The longitudinal temperature difference between the inlet and the outlet of the fixed bed of the reactor is less than 20° C.

A process for producing 2,3,3,3-tetrafluoropropene comprises i) in a first adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing hydrofluoric acid into contact, in the gas phase with at least one chlorinated compound in order to produce a stream A comprising 2-chloro-3,3,3-trifluoropropene, ii) in a second adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing the stream A into contact, in the gas phase in the presence of a catalyst, with hydrofluoric acid, to produce a stream B comprising 2,3,3,3-tetrafluoropropene. The temperature at the inlet of the fixed bed of one of said first or second reactors is between 300° C. and 400° C. The longitudinal temperature difference between the inlet and the outlet of the fixed bed of the reactor is less than 20° C.

A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene comprises contacting 1,1,2,4,4-pentachlorobuta-1,3-diene with hydrogen fluoride in the vapor phase in the presence of a fluorination catalyst comprising a metal halide to produce E- and Z-1,1,1,4,4,4-hexafluoro-2-chloro-2-butene. A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene further comprises contacting E- and Z-1,1,1,4,4,4-hexafluoro-2-chloro-2-butene with base to produce 1,1,1,4,4,4-hexafluoro-2-butyne, and subsequently hydrogenating hexafluoro-2-butyne to produce Z-1,1,1,4,4,4-hexafluoro-2-butene.

A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene comprises contacting 1,1,2,4,4-pentachlorobuta-1,3-diene with hydrogen fluoride in the vapor phase in the presence of a fluorination catalyst comprising a metal halide to produce E- and Z-1,1,1,4,4,4-hexafluoro-2-chloro-2-butene. A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene further comprises contacting E- and Z-1,1,1,4,4,4-hexafluoro-2-chloro-2-butene with base to produce 1,1,1,4,4,4-hexafluoro-2-butyne, and subsequently hydrogenating hexafluoro-2-butyne to produce Z-1,1,1,4,4,4-hexafluoro-2-butene.

A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene comprises contacting 1,1,2,4,4-pentachlorobuta-1,3-diene with hydrogen fluoride in the vapor phase in the presence of a fluorination catalyst comprising a metal halide to produce E- and Z-1,1,1,4,4,4-hexafluoro-2-chloro-2-butene. A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene further comprises contacting E- and Z-1,1,1,4,4,4-hexafluoro-2-chloro-2-butene with base to produce 1,1,1,4,4,4-hexafluoro-2-butyne, and subsequently hydrogenating hexafluoro-2-butyne to produce Z-1,1,1,4,4,4-hexafluoro-2-butene.

Processes for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene and intermediates for producing same. A process for producing 2-chloro-1,1,1,4,4,4-hexafluorobutane comprises contacting 1,1,2,4,4-pentachlorobuta-1,3-diene with HF in the liquid phase in the presence of a fluorination catalyst. A process for producing 2,2-dichloro-1,1,1,4,4,4-hexafluorobutane comprises contacting 2-chloro-1,1,1,4,4,4-hexafluorobutane with a chlorine source. A process for producing 1,1,1,4,4,4-hexafluoro-2-butyne comprises contacting 2,2-dichloro-1,1,1,4,4,4-hexafluorobutane with a base. A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene comprises contacting 1,1,1,4,4,4-hexafluoro-2-butyne with hydrogen.

Processes for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene and intermediates for producing same. A process for producing 2-chloro-1,1,1,4,4,4-hexafluorobutane comprises contacting 1,1,2,4,4-pentachlorobuta-1,3-diene with HF in the liquid phase in the presence of a fluorination catalyst. A process for producing 2,2-dichloro-1,1,1,4,4,4-hexafluorobutane comprises contacting 2-chloro-1,1,1,4,4,4-hexafluorobutane with a chlorine source. A process for producing 1,1,1,4,4,4-hexafluoro-2-butyne comprises contacting 2,2-dichloro-1,1,1,4,4,4-hexafluorobutane with a base. A process for producing Z-1,1,1,4,4,4-hexafluorobut-2-ene comprises contacting 1,1,1,4,4,4-hexafluoro-2-butyne with hydrogen.