The present invention relates to the use of adsorbents comprising zinc oxide nanowires decorated with catalytically active metal particles for the removal of sulfur from hydrocarbon feedstocks, including the desulfurization of diesel fuels and the deep desulfurization of natural gas, and to the use of decorated zinc oxide nanowire adsorbents for the hydrogenation of naphthalene selectively to tetralin in the presence of sulfur compounds. The adsorbent comprises nickel metal particles or nickel-zinc alloy particles deposited on zinc oxide nanowires.

A process for producing light olefins and aromatics, which comprises reacting a feedstock by contacting with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone among the reaction zones downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone, separating the spent catalyst from the reaction product vapor, regenerating the separated spent catalyst and returning the regenerated catalyst to the reactor, and separating the reaction product vapor to obtain the desired products, light olefins and aromatics. This process produces maximum light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

A process for producing light olefins and aromatics, which comprises reacting a feedstock by contacting with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone among the reaction zones downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone, separating the spent catalyst from the reaction product vapor, regenerating the separated spent catalyst and returning the regenerated catalyst to the reactor, and separating the reaction product vapor to obtain the desired products, light olefins and aromatics. This process produces maximum light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

A benzene selective hydrogenation reaction system and a method are provided. The system includes a benzene refiner, a first hydrogenation reactor, a second hydrogenation reactor and a separator which are connected in sequence. The first hydrogenation reactor is provided with a first inlet and a first outlet, and the second hydrogenation reactor is provided with a second inlet and a second outlet. The first inlet is connected to the discharge port of the benzene refiner; the first outlet is connected to the second inlet; the second outlet is connected to the separator. The catalyst outlet is connected to the first hydrogenation reactor for recycling the catalyst into the first hydrogenation reactor. Two micro-interface units are respectively disposed within the first hydrogenation reactor and the second hydrogenation reactor, and the micro-interface units are used for dispersing and breaking hydrogen into micro-bubbles with a micron-scale diameter.

A benzene selective hydrogenation reaction system and a method are provided. The system includes a benzene refiner, a first hydrogenation reactor, a second hydrogenation reactor and a separator which are connected in sequence. The first hydrogenation reactor is provided with a first inlet and a first outlet, and the second hydrogenation reactor is provided with a second inlet and a second outlet. The first inlet is connected to the discharge port of the benzene refiner; the first outlet is connected to the second inlet; the second outlet is connected to the separator. The catalyst outlet is connected to the first hydrogenation reactor for recycling the catalyst into the first hydrogenation reactor. Two micro-interface units are respectively disposed within the first hydrogenation reactor and the second hydrogenation reactor, and the micro-interface units are used for dispersing and breaking hydrogen into micro-bubbles with a micron-scale diameter.

A benzene selective hydrogenation reaction system and a method are provided. The system includes a benzene refiner, a first hydrogenation reactor, a second hydrogenation reactor and a separator which are connected in sequence. The first hydrogenation reactor is provided with a first inlet and a first outlet, and the second hydrogenation reactor is provided with a second inlet and a second outlet. The first inlet is connected to the discharge port of the benzene refiner; the first outlet is connected to the second inlet; the second outlet is connected to the separator. The catalyst outlet is connected to the first hydrogenation reactor for recycling the catalyst into the first hydrogenation reactor. Two micro-interface units are respectively disposed within the first hydrogenation reactor and the second hydrogenation reactor, and the micro-interface units are used for dispersing and breaking hydrogen into micro-bubbles with a micron-scale diameter.

Catalyst comprising a nickel-based active phase and an alumina support, characterized in that: the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst; the nickel density ratio between the crust and the core is strictly greater than 3; said crust comprises between 40% and 80% by weight of nickel element relative to the total weight of nickel contained in the catalyst.

Catalyst comprising nickel and sulfur on an alumina support, said catalyst being characterized in that: the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst; the nickel density ratio between the crust and the core is strictly greater than 3; said crust comprises more than 25% by weight of nickel element relative to the total weight of nickel contained in the catalyst, the size of the nickel particles in the catalyst, measured in oxide form, is between 7 and 25 nm.

Catalyst comprising nickel and sulfur on an alumina support, said catalyst being characterized in that: the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst; the nickel density ratio between the crust and the core is strictly greater than 3; said crust comprises more than 25% by weight of nickel element relative to the total weight of nickel contained in the catalyst, the size of the nickel particles in the catalyst, measured in oxide form, is between 7 and 25 nm.

A benzene selective hydrogenation reaction system and a method are provided. The system includes a benzene refiner, a first hydrogenation reactor, a second hydrogenation reactor and a separator which are connected in sequence. The first hydrogenation reactor is provided with a first inlet and a first outlet, and the second hydrogenation reactor is provided with a second inlet and a second outlet. The first inlet is connected to the discharge port of the benzene refiner; the first outlet is connected to the second inlet; the second outlet is connected to the separator. The catalyst outlet is connected to the first hydrogenation reactor for recycling the catalyst into the first hydrogenation reactor. Two micro-interface units are respectively disposed within the first hydrogenation reactor and the second hydrogenation reactor, and the micro-interface units are used for dispersing and breaking hydrogen into micro-bubbles with a micron-scale diameter.