The present invention relates to a catalyst for fixed bed aniline rectification residue recycling and preparation method thereof. Based on the total weight of the catalyst, the catalyst comprises the following components in percentage by weight: 5-40% of an active component, 2-30% of a first cocatalyst component, 10-30% of a second cocatalyst component and the balance of carrier, wherein the active component is NiO; the first cocatalyst component is one or more of Fe, Mo, Cr or Co oxide; and the second cocatalyst component is one or more of La, Zr, Y or Ce oxide. The catalyst is prepared through co-precipitation. The catalyst shows high activity and stability in the waste liquid treatment process, and can still maintain high rectification residue cracking rate after reaction of 200 hours.

A hydrogenation treatment catalyst is provided for heavy hydrocarbon oil, in which a hydrogenation-active component is supported on a silica-containing porous alumina carrier containing 0.1% to 1.5% by mass of silica based on the carrier. The total pore volume is 0.55 to 0.75 mL/g. Of the total volume of pores having a pore diameter of 3 to 30 nm (1) 30% to 45% have a pore diameter of 5 to 10 nm, (2) 50% to 65% have a pore diameter of 10 to 15 nm, and (3) the total volume of pores having a pore diameter in a range of ?1 nm from the average pore diameter is 25% or more. The total volume of pores having a pore diameter of 30 nm or more is 3% or less. The average pore diameter of pores having a pore diameter of 10 to 30 nm is 10.5 to 13 nm.

A hydrogenation treatment catalyst is provided for heavy hydrocarbon oil, in which a hydrogenation-active component is supported on a silica-containing porous alumina carrier containing 0.1% to 1.5% by mass of silica based on the carrier. The total pore volume is 0.55 to 0.75 mL/g. Of the total volume of pores having a pore diameter of 3 to 30 nm (1) 30% to 45% have a pore diameter of 5 to 10 nm, (2) 50% to 65% have a pore diameter of 10 to 15 nm, and (3) the total volume of pores having a pore diameter in a range of ?1 nm from the average pore diameter is 25% or more. The total volume of pores having a pore diameter of 30 nm or more is 3% or less. The average pore diameter of pores having a pore diameter of 10 to 30 nm is 10.5 to 13 nm.

A method for producing diene comprises a step 1 of obtaining a straight chain internal olefin by removing a branched olefin from a raw material including at least the branched olefin and a straight chain olefin; and a step 2 of producing diene from the internal olefin by oxidative dehydrogenation using a first catalyst and a second catalyst, and the first catalyst has a complex oxide including bismuth, molybdenum and oxygen, and the second catalyst includes at least one selected from the group consisting of silica and alumina.

A method for producing diene comprises a step 1 of obtaining a straight chain internal olefin by removing a branched olefin from a raw material including at least the branched olefin and a straight chain olefin; and a step 2 of producing diene from the internal olefin by oxidative dehydrogenation using a first catalyst and a second catalyst, and the first catalyst has a complex oxide including bismuth, molybdenum and oxygen, and the second catalyst includes at least one selected from the group consisting of silica and alumina.

Disclosed are a composite oxide catalyst for preparing butadiene and a method of preparing the same. More particularly, a composite oxide catalyst, for preparing butadiene, including a metal composite oxide and AlPO.sub.4, and a method of preparing the same are disclosed. According to the present disclosure, a composite oxide catalyst for preparing butadiene, which includes a specific binder material, prevents generation of ingredients with a high boiling point, has superior catalyst strength, catalytic activity and butadiene yield, and a method of preparing the same are provided.

Disclosed are a composite oxide catalyst for preparing butadiene and a method of preparing the same. More particularly, a composite oxide catalyst, for preparing butadiene, including a metal composite oxide and AlPO.sub.4, and a method of preparing the same are disclosed. According to the present disclosure, a composite oxide catalyst for preparing butadiene, which includes a specific binder material, prevents generation of ingredients with a high boiling point, has superior catalyst strength, catalytic activity and butadiene yield, and a method of preparing the same are provided.

Provided are a catalyst which, in a reaction. for producing a conjugated diolefin by catalytic oxidative dehydrogenation from a mixed gas including a monoolefin having 4 or more carbon atoms and molecular oxygen, may suppress the production of a coke-like substance and improve the long-term stability of the reaction; and a method for producing the same. Disclosed is a composite metal oxide catalyst for producing a conjugated diolefin by a gas phase catalytic oxidative dehydrogenation reaction from a mixed gas including a monoolefin having 4 or more carbon atoms and molecular oxygen, the composite metal oxide catalyst having a solid acidity of 35 to 172 mol/g.

Provided are a catalyst which, in a reaction. for producing a conjugated diolefin by catalytic oxidative dehydrogenation from a mixed gas including a monoolefin having 4 or more carbon atoms and molecular oxygen, may suppress the production of a coke-like substance and improve the long-term stability of the reaction; and a method for producing the same. Disclosed is a composite metal oxide catalyst for producing a conjugated diolefin by a gas phase catalytic oxidative dehydrogenation reaction from a mixed gas including a monoolefin having 4 or more carbon atoms and molecular oxygen, the composite metal oxide catalyst having a solid acidity of 35 to 172 mol/g.

A catalyst for treating heavy hydrocarbon feedstocks. The catalyst comprises a calcined particle comprising a co-mulled mixture made by co-mulling inorganic oxide powder, molybdenum trioxide powder, and a nickel compound or cobalt compound, or both compounds, and then forming the co-mulled mixture into a particle that is calcined to provide the calcined particle. The calcination is conducted at a temperature such that at least 20% of the pore volume of the calcined particle is in pores of greater than 5,000 ? and less than 70% of the pore volume of the calcined particle is in the pores having a pore size in the range of from 70 to 250 ?.