A catalyst for pyrolysis of 1,2-dichloroethane (1,2-DCE) to prepare vinyl chloride monomer (VCM), a preparation method, a use, and a regeneration method thereof are provided. The catalyst for pyrolysis of 1,2-DCE to prepare VCM includes a silicon-aluminum molecular sieve. The catalyst for pyrolysis of 1,2-DCE to prepare VCM has high reaction activity and excellent selectivity and solves the problem that the pyrolysis of 1,2-DCE to prepare VCM in the prior art involves high reaction temperature and large energy consumption and is prone to coking and carbon deposition.

A catalyst for pyrolysis of 1,2-dichloroethane (1,2-DCE) to prepare vinyl chloride monomer (VCM), a preparation method, a use, and a regeneration method thereof are provided. The catalyst for pyrolysis of 1,2-DCE to prepare VCM includes a silicon-aluminum molecular sieve. The catalyst for pyrolysis of 1,2-DCE to prepare VCM has high reaction activity and excellent selectivity and solves the problem that the pyrolysis of 1,2-DCE to prepare VCM in the prior art involves high reaction temperature and large energy consumption and is prone to coking and carbon deposition.

A process for preventing hazardous conditions at startup and shutdown of a reactor by sending an inert gas such as nitrogen to strip entrained oxygen from the catalyst when reactor temperatures are below about 240° C. During normal operation the entrained oxygen reacts with hydrocarbons to produce oxides but at the lower temperatures that are present at startup or shutdown these reactions do not occur sufficiently leaving oxygen that can cause hazardous conditions as temperatures increase upon startup. When the temperature is in the safe operating zone above 240° C., the nitrogen gas is stripped by air or other oxygen containing gas.

A process for preventing hazardous conditions at startup and shutdown of a reactor by sending an inert gas such as nitrogen to strip entrained oxygen from the catalyst when reactor temperatures are below about 240° C. During normal operation the entrained oxygen reacts with hydrocarbons to produce oxides but at the lower temperatures that are present at startup or shutdown these reactions do not occur sufficiently leaving oxygen that can cause hazardous conditions as temperatures increase upon startup. When the temperature is in the safe operating zone above 240° C., the nitrogen gas is stripped by air or other oxygen containing gas.

Processes and apparatuses for regenerating catalysts used in a hydrocarbon conversion process. The catalyst is separated into a bypass portion and an adsorption portion. The bypass portion is passed to a regeneration zone where coke may be removed. A vent gas from the regeneration zone may include an active additive from the catalyst, like a halogen. The vent gas is sent to an adsorption zone which also receives the adsorption portion. In the adsorption zone, the catalyst will contact and adsorb the active additive and then pass to the regeneration zone. The amount of active additive in the vent gas from the regeneration zone and the adsorption zone is reduced.

This disclosure relates to red mud compositions. This disclosure also relates to methods of making red mud compositions. This disclosure additionally relates to methods of using red mud compositions.

An active material useful in an oxidative dehydrogenation reactor system has an active phase, a support phase, and an intermediate composite phase. The active phase includes a transition metal oxide such as manganese oxide, which is reversibly oxidizable and/or reducible between oxidized and reduced states. The support phase includes an oxide of a IUPAC Group 2-14 element. The composite phase is a mixed metal oxide of the transition metal and the Group 2-14 element. The active phase can also include a promoter such as Na-W04 and/or a selectivity modifier such as A1 or ceria. Also, a reactor including the active material in a reactor, a method of making the active material, and a method of using the active material in a regenerative reaction process.

Disclosed are a catalyst pre-hydrocarbon-pooling method and a pre-hydrocarbon-pooling device, relating to the technical field of preparation of low carbon olefins. A regenerated catalyst enters a pre-hydrocarbon-pooling reactor, and a pre-hydrocarbon-pooling reaction occurs between the regenerated catalyst and an activation medium to form “hydrocarbon pool” active species. “Pre-hydrocarbon-pooling” treatment is performed on the regenerated catalyst by providing a pre-hydrocarbon-pooling device, so that the regenerated catalyst forms the “hydrocarbon pooled” active species and carbon deposition before entering into an oxygenate conversion reactor, by way of which “hydrocarbon pool” active species distribution and coke distribution of the catalyst in the conversion reactor are improved. This shortens or eliminates a reaction “induction period” and improves the catalytic activity and selectivity of the regenerated catalyst for a reaction of an oxygenate to low-carbon olefins.

A dehydrogenation catalyst for producing olefins from alkane gases, in which cobalt and zinc are supported on alumina. A method for preparing the dehydrogenation catalyst for producing olefins from alkane gases, includes: preparing a mixed solution by mixing cobalt and zinc precursors with water; preparing a supported catalyst by impregnating alumina with the mixed solution; drying the supported catalyst; and calcining the dried supported catalyst at 500° C. to 900° C.

A coke control reactor, a device for preparing low-carbon olefins from an oxygen-containing compound, and a use thereof are provided. The coke control reactor includes a riser reactor and a bed reactor; the bed reactor includes a bed reactor shell, and the bed reactor shell encloses a reaction zone I, a transition zone, and a gas-solid separation zone I from bottom to top; a bed reactor distributor is arranged in the reaction zone I; a coke controlled catalyst delivery pipe is arranged outside the reaction zone I; an upper section of the riser reactor penetrates through a bottom of the bed reactor and is axially inserted in the bed reactor; and an outlet end of the riser reactor is located in the transition zone. The coke control reactor can control the conversion and generation of coke species in a catalyst.