The invention discloses a process for hydrogenation (alkenes, carbonyl compounds and aromatics) and hydrodeoxygenation (methoxy phenols) of organic molecules using hydrous ruthenium oxide (HRO) and its supported form as a recyclable heterogeneous catalyst in aqueous medium with good yield of desired products (70-100%) under mild reaction conditions.

The invention discloses a process for hydrogenation (alkenes, carbonyl compounds and aromatics) and hydrodeoxygenation (methoxy phenols) of organic molecules using hydrous ruthenium oxide (HRO) and its supported form as a recyclable heterogeneous catalyst in aqueous medium with good yield of desired products (70-100%) under mild reaction conditions.

The invention discloses a process for hydrogenation (alkenes, carbonyl compounds and aromatics) and hydrodeoxygenation (methoxy phenols) of organic molecules using hydrous ruthenium oxide (HRO) and its supported form as a recyclable heterogeneous catalyst in aqueous medium with good yield of desired products (70-100%) under mild reaction conditions.

A process for catalytic hydrogenation of aromatic amines can be performed. The aromatic amines can be methylenedianiline and/or tolylenediamine. The ring-hydrogenated equivalents can be obtained by contacting an input product, which have the aromatic amines and impurities, such as, alcohols, glycols, polyols, organic acids and/or water, with hydrogen in the presence of a catalyst. The catalyst can be platinum, palladium, rhodium, ruthenium, nickel, cobalt and/or iron. The catalyst is applied to a support, wherein the input product that has aromatic amines result from a PU decomposition process and contains impurities from this decomposition process.

A process for catalytic hydrogenation of aromatic amines can be performed. The aromatic amines can be methylenedianiline and/or tolylenediamine. The ring-hydrogenated equivalents can be obtained by contacting an input product, which have the aromatic amines and impurities, such as, alcohols, glycols, polyols, organic acids and/or water, with hydrogen in the presence of a catalyst. The catalyst can be platinum, palladium, rhodium, ruthenium, nickel, cobalt and/or iron. The catalyst is applied to a support, wherein the input product that has aromatic amines result from a PU decomposition process and contains impurities from this decomposition process.

A process for catalytic hydrogenation of aromatic amines can be performed. The aromatic amines can be methylenedianiline and/or tolylenediamine. The ring-hydrogenated equivalents can be obtained by contacting an input product, which have the aromatic amines and impurities, such as, alcohols, glycols, polyols, organic acids and/or water, with hydrogen in the presence of a catalyst. The catalyst can be platinum, palladium, rhodium, ruthenium, nickel, cobalt and/or iron. The catalyst is applied to a support, wherein the input product that has aromatic amines result from a PU decomposition process and contains impurities from this decomposition process.

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.

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.

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.

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.