Abstract: An aromatics hydrogenation catalyst composition which comprises a noble metal component and a support comprising zirconia, silica, and, optionally, alumina. The catalyst composition is manufactured by co-mulling silica, a zirconium compound, and, optionally, alumina to form a mixture that is formed into a shape, such as by extrusion to form an extrudate, with the shape being calcined and noble metal being incorporated into the shape. The catalyst composition may be used in the saturation of aromatic compounds.

Abstract: The present invention relates to a process for hydrogenating an aldehyde. An aldehyde is contacted with a catalyst comprising a support containing at least 95% ?-alumina and non-support metals dispersed on the surface of the support. The non-support metals comprise nickel and/or one or more compounds thereof and molybdenum and/or one or more compounds thereof. The nickel and/or one or more compounds thereof comprise from 3 wt. % to 9 wt. % of the catalyst, by metallic weight, and the molybdenum and/or one or more compounds thereof comprise from 1 wt. % to 4 wt. % of the catalyst, by metallic weight.

Abstract: The present invention provides a hydrogenation catalyst effective for hydrogenating 3-hydroxypropionaldehyde to 1,3-propanediol. The hydrogenation catalyst comprises an ?-alumina support, nickel, ruthenium, and a promoter. The nickel is deposited on the ?-alumina support, and the ruthenium and the promoter are deposited on the nickel and the ?-alumina support. The ?-alumina support comprises at least 92 wt. % of the catalyst, and the nickel comprises from 1 wt. % to 6 wt. % of the catalyst. The present invention also provides a process of hydrogenating 3-hydroxypropionaldehyde to 1,3-propanediol with the catalyst.

Abstract: In a process for the hydrogenation of nitrogen-containing hydrocarbons in a hydrocarbon feedstock, the feedstock is contacted at a temperature between about 575.degree. F. and about 775.degree. F. and a pressure between about 600 psi and about 2500 psi in the presence of added hydrogen with a first catalyst bed containing a hydrotreating catalyst containing nickel, tungsten and optionally phosphorous supported on an alumina support, and, after contact with the first catalyst bed, the hydrogen and feedstock without modification is passed from the first catalyst bed to a second catalyst bed where it is contacted at a temperature between about 575.degree. F. and about 775.degree. F. and a pressure between about 600 psi and about 2500 psi with a hydrotreating catalyst containing nickel, molybdenum and optionally phosphorous supported on an alumina support.

Abstract: The instant invention comprises an improved hydrorefining process which comprises contacting hydrocarbonaceous oil feed and hydrogen with a catalyst comprising a hydrogenation component selected from the group consisting of Group VIB metal component, Group VIII non-noble metal component and mixtures thereof, optionally comprising a phosphorous-containing component or compound, and an alumina-containing support, at hydrorefining conditions, wherein the improvement comprises heating the catalyst in substantially non-sulfided form at initial start-up from a temperature below about 450.degree. F. to hydrorefining temperature at an average rate of less than 30.degree. F. per hour in the presence of hydrogen and a start-up hydrocarbonaceous oil feed having a sulfur content in the form of organosulfides of greater than 0.5 moles (basis elemental sulfur) per kilogram of start-up feed.

Abstract: The instant invention comprises an improved hydrorefining process which comprises contacting hydrocarbonaceous oil feed and hydrogen with a catalyst comprising a hydrogenation component selected from the group consisting of Group VIB metal component, Group VIII non-noble metal component and mixtures thereof, optionally comprising a phosphorous-containing component or compound, and an alumina-containing support, at hydrorefining conditions, wherein the improvement comprises heating the catalyst at initial start-up from a temperature below about 450.degree. F. to hydrorefining temperature at an average rate of less than 30.degree. F. per hour in the presence of hydrogen and said oil feed.