Disclosed are processes for the production of fluorinated olefins, preferably adapted to commercialization of CF.sub.3CFCH.sub.2 (1234yf). Three steps may be used in preferred embodiments in which a feedstock such as CCl.sub.2CClCH.sub.2Cl (which may be purchased or synthesized from 1,2,3-trichloropropane) is fluorinated (preferably with HF in gas-phase in the presence of a catalyst) to synthesize a compound such as CF.sub.3CClCH.sub.2, preferably in a 80-96% selectivity. The CF.sub.3CClCH.sub.2 is preferably converted to CF.sub.3CFClCH.sub.3 (244-isomer) using a SbCl.sub.5 as the catalyst which is then transformed selectively to 1234yf, preferably in a gas-phase catalytic reaction using activated carbon as the catalyst. For the first step, a mixture of Cr.sub.2O.sub.3 and FeCl.sub.3/C is preferably used as the catalyst to achieve high selectivity to CF.sub.3CClCH.sub.2 (96%). In the second step, SbCl.sub.5/C is preferably used as the selective catalyst for transforming 1233xf to 244-isomer, CF.sub.3CFClCH.sub.3. The intermediates are preferably isolated and purified by distillation and used in the next step without further purification, preferably to a purity level of greater than about 95%.

Disclosed are processes for the production of fluorinated olefins, preferably adapted to commercialization of CF.sub.3CFCH.sub.2 (1234yf). Three steps may be used in preferred embodiments in which a feedstock such as CCl.sub.2CClCH.sub.2Cl (which may be purchased or synthesized from 1,2,3-trichloropropane) is fluorinated (preferably with HF in gas-phase in the presence of a catalyst) to synthesize a compound such as CF.sub.3CClCH.sub.2, preferably in a 80-96% selectivity. The CF.sub.3CClCH.sub.2 is preferably converted to CF.sub.3CFClCH.sub.3 (244-isomer) using a SbCl.sub.5 as the catalyst which is then transformed selectively to 1234yf, preferably in a gas-phase catalytic reaction using activated carbon as the catalyst. For the first step, a mixture of Cr.sub.2O.sub.3 and FeCl.sub.3/C is preferably used as the catalyst to achieve high selectivity to CF.sub.3CClCH.sub.2 (96%). In the second step, SbCl.sub.5/C is preferably used as the selective catalyst for transforming 1233xf to 244-isomer, CF.sub.3CFClCH.sub.3. The intermediates are preferably isolated and purified by distillation and used in the next step without further purification, preferably to a purity level of greater than about 95%.

Disclosed are processes for the production of fluorinated olefins, preferably adapted to commercialization of CF.sub.3CFCH.sub.2 (1234yf). Three steps may be used in preferred embodiments in which a feedstock such as CCl.sub.2CClCH.sub.2Cl (which may be purchased or synthesized from 1,2,3-trichloropropane) is fluorinated (preferably with HF in gas-phase in the presence of a catalyst) to synthesize a compound such as CF.sub.3CClCH.sub.2, preferably in a 80-96% selectivity. The CF.sub.3CClCH.sub.2 is preferably converted to CF.sub.3CFClCH.sub.3 (244-isomer) using a SbCl.sub.5 as the catalyst which is then transformed selectively to 1234yf, preferably in a gas-phase catalytic reaction using activated carbon as the catalyst. For the first step, a mixture of Cr.sub.2O.sub.3 and FeCl.sub.3/C is preferably used as the catalyst to achieve high selectivity to CF.sub.3CClCH.sub.2 (96%). In the second step, SbCl.sub.5/C is preferably used as the selective catalyst for transforming 1233xf to 244-isomer, CF.sub.3CFClCH.sub.3. The intermediates are preferably isolated and purified by distillation and used in the next step without further purification, preferably to a purity level of greater than about 95%.

A process is disclosed for making CF.sub.3CFCHF. The process involves reacting CF.sub.3CClFCCl.sub.2F with H.sub.2 in a reaction zone in the presence of a catalyst to produce a product mixture comprising CF.sub.3CFCHF. The catalyst has a catalytically effective amount of palladium supported on a support selected from the group consisting of alumina, fluorided alumina, aluminum fluoride and mixtures thereof and the mole ratio of H.sub.2 to CF.sub.3CClFCCl.sub.2F fed to the reaction zone is between about 1:1 and about 5:1. Also disclosed are azeotropic compositions of CF.sub.3CClFCCl.sub.2F and HF and azeotropic composition of CF.sub.3CHFCH.sub.2F and HF.

A process is disclosed for making CF.sub.3CFCHF. The process involves reacting CF.sub.3CClFCCl.sub.2F with H.sub.2 in a reaction zone in the presence of a catalyst to produce a product mixture comprising CF.sub.3CFCHF. The catalyst has a catalytically effective amount of palladium supported on a support selected from the group consisting of alumina, fluorided alumina, aluminum fluoride and mixtures thereof and the mole ratio of H.sub.2 to CF.sub.3CClFCCl.sub.2F fed to the reaction zone is between about 1:1 and about 5:1. Also disclosed are azeotropic compositions of CF.sub.3CClFCCl.sub.2F and HF and azeotropic composition of CF.sub.3CHFCH.sub.2F and HF.

A process is disclosed for making CF.sub.3CFCHF. The process involves reacting CF.sub.3CClFCCl.sub.2F with H.sub.2 in a reaction zone in the presence of a catalyst to produce a product mixture comprising CF.sub.3CFCHF. The catalyst has a catalytically effective amount of palladium supported on a support selected from the group consisting of alumina, fluorided alumina, aluminum fluoride and mixtures thereof and the mole ratio of H.sub.2 to CF.sub.3CClFCCl.sub.2F fed to the reaction zone is between about 1:1 and about 5:1. Also disclosed are azeotropic compositions of CF.sub.3CClFCCl.sub.2F and HF and azeotropic composition of CF.sub.3CHFCH.sub.2F and HF.

Methods and systems for electrochemical conversion of carbon dioxide to organic products including formate and formic acid are provided. A method may include, but is not limited to, steps (A) to (C). Step (A) may introduce an acidic anolyte to a first compartment of an electrochemical cell. The first compartment may include an anode. Step (B) may introduce a bicarbonate-based catholyte saturated with carbon dioxide to a second compartment of the electrochemical cell. The second compartment may include a high surface area cathode including indium and having a void volume of between about 30% to 98%. At least a portion of the bicarbonate-based catholyte is recycled. Step (C) may apply an electrical potential between the anode and the cathode sufficient to reduce the carbon dioxide to at least one of a single-carbon based product or a multi-carbon based product.

Embodiments of the present disclosure provide for methods of hydrocarbon functionalization, methods and systems for converting a hydrocarbon into a compound including at least one group ((e.g., hydroxyl group) (e.g., methane to methanol)), functionalized hydrocarbons, and the like. Systems and methods as described herein can utilize photocatalysis.

Embodiments of the present disclosure provide for methods of hydrocarbon functionalization, methods and systems for converting a hydrocarbon into a compound including at least one group ((e.g., hydroxyl group) (e.g., methane to methanol)), functionalized hydrocarbons, and the like. Systems and methods as described herein can utilize photocatalysis.

The present invention relates to a method for chlorination and dehydrogenation of ethane, comprising: mixing and reacting a low-melting-point metal chloride with C.sub.2H.sub.6, such that the low-melting-point metal chloride is reduced to a liquid-state low-melting-point metal, and the C.sub.2H.sub.6 is chlorinated and dehydrogenized to give a mixed gas containing HCl, C.sub.2H.sub.6, C.sub.2H.sub.4, C.sub.2H.sub.2 and C.sub.2H.sub.3Cl. In the method, the low-melting-point metal chloride is used as a raw material for chlorination and dehydrogenation, and the low-melting-point metal produced after the reaction is used as an intermediate medium. The method has the characteristics of simple process, low cost and high yield. Moreover, some acetylene and vinyl chloride can be produced as by-products at the same time when the ethylene is produced, by controlling the ratio of ethane to the chloride as desired in production.