The present invention relates to a method for preparing, activating and regenerating a metal supported catalyst, comprising: treating a M.sub.a-M.sub.b-M.sub.c metal supported catalyst at 10-700? C. by using an ammonia or nitrogen-containing organic matter, wherein the M.sub.a metal is an active metal selected from one or more of a noble metal atom or a transition metal, the support is a common industrial porous catalyst, and the M.sub.a metal is dispersed on the support in a state of single atomic site. According to the M.sub.d-M.sub.b-M.sub.c metal supported noble metal/zinc catalyst treated by the method of the present invention, the direct dehydrogenation conversion rate and selectivity of catalyzing light alkanes are remarkably improved; the method for preparing the catalyst is simple in process, the catalytic activity after regeneration is still kept, and the catalyst can be industrially produced on a large scale.

This invention relates to a supported catalyst for synthesizing ammonia (NH.sub.3) from nitrogen gas (N.sub.2) and hydrogen gas (H.sub.2), method of making the support, and methods of decorating the support with the catalyst.

A process is disclosed for making CF.sub.3CF.sub.2CH.sub.3, CF.sub.3CFCH.sub.2 and/or CF.sub.3CClCH.sub.2. The process involves reacting at least one starting material selected from the group consisting of halopropanes of the formula CX.sub.3CH.sub.2CH.sub.2X, halopropenes of the formula CX.sub.3CHCH.sub.2 and halopropenes of the formula CX.sub.2CHCH.sub.2X, wherein each X is independently F or Cl, with HF and Cl.sub.2 in a reaction zone to produce a product mixture comprising HF, HCl, CF.sub.3CF.sub.2CH.sub.3, CF.sub.3CFCH.sub.2, and CF.sub.3CClCH.sub.2; and recovering the CF.sub.3CF.sub.2CH.sub.3, CF.sub.3CFCH.sub.2 and/or CF.sub.3CClCH.sub.2 from the product mixture. Also disclosed is a process for making CF.sub.3CH.sub.2CHF.sub.2, CF.sub.3CHCHF, and/or CF.sub.3CHCHCl. This process involves reacting at least one starting material selected from the group consisting of halopropenes of the formula CX.sub.3CHCH.sub.2 and halopropenes of the formula CX.sub.2CHCH.sub.2X, wherein each X is independently F or Cl, with HF and Cl.sub.2 in a reaction zone to produce a product mixture comprising HF, HCl, CF.sub.3CH.sub.2CHF.sub.2, CF.sub.3CHCHF and CF.sub.3CHCHCl; and recovering the CF.sub.3CH.sub.2CHF.sub.2, CF.sub.3CHCHF, and/or CF.sub.3CHCHCl from the product mixture. The molar ratio of HF to the total amount of starting materials fed to the reaction zone for both of these processes is at least stoichiometric, and the molar ratio of Cl.sub.2 to total amount of starting material fed to the reaction zone for both of these processes is 2:1 or less.

A process is disclosed for making CF.sub.3CF.sub.2CH.sub.3, CF.sub.3CFCH.sub.2 and/or CF.sub.3CClCH.sub.2. The process involves reacting at least one starting material selected from the group consisting of halopropanes of the formula CX.sub.3CH.sub.2CH.sub.2X, halopropenes of the formula CX.sub.3CHCH.sub.2 and halopropenes of the formula CX.sub.2CHCH.sub.2X, wherein each X is independently F or Cl, with HF and Cl.sub.2 in a reaction zone to produce a product mixture comprising HF, HCl, CF.sub.3CF.sub.2CH.sub.3, CF.sub.3CFCH.sub.2, and CF.sub.3CClCH.sub.2; and recovering the CF.sub.3CF.sub.2CH.sub.3, CF.sub.3CFCH.sub.2 and/or CF.sub.3CClCH.sub.2 from the product mixture. Also disclosed is a process for making CF.sub.3CH.sub.2CHF.sub.2, CF.sub.3CHCHF, and/or CF.sub.3CHCHCl. This process involves reacting at least one starting material selected from the group consisting of halopropenes of the formula CX.sub.3CHCH.sub.2 and halopropenes of the formula CX.sub.2CHCH.sub.2X, wherein each X is independently F or Cl, with HF and Cl.sub.2 in a reaction zone to produce a product mixture comprising HF, HCl, CF.sub.3CH.sub.2CHF.sub.2, CF.sub.3CHCHF and CF.sub.3CHCHCl; and recovering the CF.sub.3CH.sub.2CHF.sub.2, CF.sub.3CHCHF, and/or CF.sub.3CHCHCl from the product mixture. The molar ratio of HF to the total amount of starting materials fed to the reaction zone for both of these processes is at least stoichiometric, and the molar ratio of Cl.sub.2 to total amount of starting material fed to the reaction zone for both of these processes is 2:1 or less.

A process for the production of 1,1-difluoroethane by the catalytic fluorination, in the vapour phase, of a composition comprising vinyl chloride with hydrogen fluoride, wherein the vinyl chloride is contacted with hydrogen fluoride, at temperatures between 100 and 500 C., in the presence of a catalyst comprising a one or more of chromia, alumina, carbon.

A process for the production of 1,1-difluoroethane by the catalytic fluorination, in the vapour phase, of a composition comprising vinyl chloride with hydrogen fluoride, wherein the vinyl chloride is contacted with hydrogen fluoride, at temperatures between 100 and 500 C., in the presence of a catalyst comprising a one or more of chromia, alumina, carbon.

The present invention provides an iron and steel smelting method, wherein separating the product of the catalytic dehydrogenation reaction on propane to obtain a mixed gas containing hydrogen, methane, and ethane; and mixing the mixed gas with water and/or CO.sub.2 as a catalytic conversion raw material, and producing synthesis gas by means of a catalytic conversion reaction, the synthesis gas being used for iron smelting, and electricity being used to provide energy for the catalytic conversion reaction. The method catalytic dehydrogenation of propane is combined with steam cracking, and unconverted propane is prepared into methane, ethane, etc. by means of steam cracking; synthesis gas is further obtained by means of reforming and component adjustment, and the synthesis gas is a good raw material for direct reduction of iron.

The present invention provides an iron and steel smelting method, wherein separating the product of the catalytic dehydrogenation reaction on propane to obtain a mixed gas containing hydrogen, methane, and ethane; and mixing the mixed gas with water and/or CO.sub.2 as a catalytic conversion raw material, and producing synthesis gas by means of a catalytic conversion reaction, the synthesis gas being used for iron smelting, and electricity being used to provide energy for the catalytic conversion reaction. The method catalytic dehydrogenation of propane is combined with steam cracking, and unconverted propane is prepared into methane, ethane, etc. by means of steam cracking; synthesis gas is further obtained by means of reforming and component adjustment, and the synthesis gas is a good raw material for direct reduction of iron.

Processes for converting a hydrocarbon reactant into an alcohol compound and/or a carbonyl compound are disclosed in which the hydrocarbon reactant and either a supported chromium (VI) catalyst or a supported chromium (II) catalyst are contacted, optionally with UV-visible light irradiation, followed by exposure to an oxidizing atmosphere and then hydrolysis to form a reaction product containing the alcohol compound and/or the carbonyl compound. The presence of oxygen significant increases the amount of alcohol/carbonyl product formed, as well as the formation of oxygenated dimers and trimers of certain hydrocarbon reactants.

Processes for converting a hydrocarbon reactant into an alcohol compound and/or a carbonyl compound are disclosed in which the hydrocarbon reactant and either a supported chromium (VI) catalyst or a supported chromium (II) catalyst are contacted, optionally with UV-visible light irradiation, followed by exposure to an oxidizing atmosphere and then hydrolysis to form a reaction product containing the alcohol compound and/or the carbonyl compound. The presence of oxygen significant increases the amount of alcohol/carbonyl product formed, as well as the formation of oxygenated dimers and trimers of certain hydrocarbon reactants.