The present invention discloses a catalytic hydrogenation method for carbon nine resin, comprising the following steps: 1) adding a Pt—W—Y/γ-Al.sub.2O.sub.3 catalyst in the first half of a fixed bed, adding a Pd—Zr—Nd/γ-Al.sub.2O.sub.3 catalyst in the second half of the fixed bed, and feeding hydrogen for reduction; and 2) catalytic hydrogenating the pretreated carbon nine resin in the fixed bed. In the present invention, different catalysts capable of reacting under the same catalytic conditions are added in the first and second halves of the fixed bed, and the two different catalysts play different roles, and can be active and complementary to each other under the same conditions. The synergistic effect of the two catalysts plays a good catalytic role. Moreover, the production process is simplified, and the production cost is saved.

The present invention discloses a catalytic hydrogenation method for carbon nine resin, comprising the following steps: 1) adding a Pt—W—Y/γ-Al.sub.2O.sub.3 catalyst in the first half of a fixed bed, adding a Pd—Zr—Nd/γ-Al.sub.2O.sub.3 catalyst in the second half of the fixed bed, and feeding hydrogen for reduction; and 2) catalytic hydrogenating the pretreated carbon nine resin in the fixed bed. In the present invention, different catalysts capable of reacting under the same catalytic conditions are added in the first and second halves of the fixed bed, and the two different catalysts play different roles, and can be active and complementary to each other under the same conditions. The synergistic effect of the two catalysts plays a good catalytic role. Moreover, the production process is simplified, and the production cost is saved.

An ammonia synthesis catalyst, includes a composite oxide carrier in which at least one additive metal element selected from the group consisting of titanium (Ti), zirconium (Zr), hafnium (Hf), aluminum (Al), gallium (Ga), indium (In), silicon (Si), germanium (Ge), and tin (Sn) is solid-solutionized in a composite oxide containing cerium (Ce) and a lanthanide other than Ce and having a composition represented by the following formula:

Ce.sub.xA.sub.1−x−yB.sub.yO.sub.d

(in the formula, A represents a lanthanide other than Ce, B represents the additive metal element, x represents a molar fraction of Ce, y represents a molar fraction of the additive metal element, 1−x−y represents a molar fraction of a lanthanide other than Ce, x and y satisfy 0.1≤x≤0.9, 0.01≤y≤0.3, and 0.11≤x+y≤0.91, d represents a molar ratio of oxygen atoms, and 1.5≤d≤2 is satisfied); and ruthenium (Ru) supported on the composite oxide carrier.

An ammonia synthesis catalyst, includes a composite oxide carrier in which at least one additive metal element selected from the group consisting of titanium (Ti), zirconium (Zr), hafnium (Hf), aluminum (Al), gallium (Ga), indium (In), silicon (Si), germanium (Ge), and tin (Sn) is solid-solutionized in a composite oxide containing cerium (Ce) and a lanthanide other than Ce and having a composition represented by the following formula:

Ce.sub.xA.sub.1−x−yB.sub.yO.sub.d

(in the formula, A represents a lanthanide other than Ce, B represents the additive metal element, x represents a molar fraction of Ce, y represents a molar fraction of the additive metal element, 1−x−y represents a molar fraction of a lanthanide other than Ce, x and y satisfy 0.1≤x≤0.9, 0.01≤y≤0.3, and 0.11≤x+y≤0.91, d represents a molar ratio of oxygen atoms, and 1.5≤d≤2 is satisfied); and ruthenium (Ru) supported on the composite oxide carrier.

Porous alumina having excellent heat resistance and coking resistance is provided. The porous alumina can include silica and barium oxide added to aluminum oxide, wherein a ratio of SiO2 addition amount to a total mass of aluminum oxide and SiO2 addition amount is defined as SiO2 addition ratio (mass %), a ratio of BaO addition amount to a total mass of aluminum oxide and SiO2 addition amount is defined as BaO addition ratio (mass %), when the SiO2 addition ratio is within a range of 3 mass % or less and the BaO addition ratio is within a range of 14 mass % or less, the silica and the barium oxide are respectively added to the aluminum oxide so that a specific surface area of the porous alumina measured by a measuring method after heat treatment is equal to or larger than a reference specific surface area of reference porous alumina.

Porous alumina having excellent heat resistance and coking resistance is provided. The porous alumina can include silica and barium oxide added to aluminum oxide, wherein a ratio of SiO2 addition amount to a total mass of aluminum oxide and SiO2 addition amount is defined as SiO2 addition ratio (mass %), a ratio of BaO addition amount to a total mass of aluminum oxide and SiO2 addition amount is defined as BaO addition ratio (mass %), when the SiO2 addition ratio is within a range of 3 mass % or less and the BaO addition ratio is within a range of 14 mass % or less, the silica and the barium oxide are respectively added to the aluminum oxide so that a specific surface area of the porous alumina measured by a measuring method after heat treatment is equal to or larger than a reference specific surface area of reference porous alumina.

The present disclosure provides an integrated process and a Cu/Zn-based catalyst system for synthesizing methanol from CO.sub.2 and generating electricity from hydrocarbon feedstock. The process includes steps of gasifying hydrocarbon feedstock into syngas by using oxygen and using the produced syngas as a fuel in a power generation unit, reusing a first part of an exhaust stream of the power generation unit as a reactant in the gasification unit. Using a second part of the said exhaust stream as a reactant for methanol synthesis in a methanol reactor, wherein, the second part is treated to separate CO.sub.2 and water, and CO.sub.2 is used as the reactant for methanol synthesis. Operating an electrolyzer during non-peak hours to produce hydrogen, wherein, a required stoichiometric ratio of the produced hydrogen is transferred into the methanol reactor for methanol synthesis, wherein, a Cu/Zn-based catalyst system is used for methanol synthesis through a direct hydrogenation reaction of CO.sub.2.

The present disclosure provides an integrated process and a Cu/Zn-based catalyst system for synthesizing methanol from CO.sub.2 and generating electricity from hydrocarbon feedstock. The process includes steps of gasifying hydrocarbon feedstock into syngas by using oxygen and using the produced syngas as a fuel in a power generation unit, reusing a first part of an exhaust stream of the power generation unit as a reactant in the gasification unit. Using a second part of the said exhaust stream as a reactant for methanol synthesis in a methanol reactor, wherein, the second part is treated to separate CO.sub.2 and water, and CO.sub.2 is used as the reactant for methanol synthesis. Operating an electrolyzer during non-peak hours to produce hydrogen, wherein, a required stoichiometric ratio of the produced hydrogen is transferred into the methanol reactor for methanol synthesis, wherein, a Cu/Zn-based catalyst system is used for methanol synthesis through a direct hydrogenation reaction of CO.sub.2.

A process for the production of an ester product from a mixture of at least two different ester compounds includes the steps of mixing together at least two different starting ester compounds to form a first ester mixture; and contacting the first ester mixture with a catalyst including from 30-60% of calcium oxide and at least one second metal oxide at a temperature of at least 180° C., for a duration of at least one hour, with mixing, to form a second ester mixture having a melting point which is lower than the melting point of the first ester mixture.

A process for the production of an ester product from a mixture of at least two different ester compounds includes the steps of mixing together at least two different starting ester compounds to form a first ester mixture; and contacting the first ester mixture with a catalyst including from 30-60% of calcium oxide and at least one second metal oxide at a temperature of at least 180° C., for a duration of at least one hour, with mixing, to form a second ester mixture having a melting point which is lower than the melting point of the first ester mixture.