Various processes for preparing aldaric acids, aldonic acids, uronic acids, and/or lactone(s) thereof are described. For example, processes for preparing a C.sub.2-C.sub.7 aldaric acid and/or lactone(s) thereof by the catalytic oxidation of a C.sub.2-C.sub.7 aldonic acid and/or lactone(s) thereof and/or a C.sub.2-C.sub.7 aldose are described.

The present invention concerns a method of oxidizing a cycloalkane to form a product mixture containing a corresponding alcohol and ketone, said method comprising contacting the cycloalkane with a hydroperoxide compound in the presence of a heterogenous catalyst comprising gold.

Zeolites having highly dispersed bimetallic clusters, uniformly distributed in size and composition, encapsulated therein are disclosed. Metal encapsulation and alloying is conferred by introducing ligated metal cation precursors into zeolite synthesis gels, which are subsequently crystallized hydrothermally to form zeolites with metal cations occluded in the pores. The ligated cations are anchored to the zeolite framework via siloxane bridges which enforces their uniform dispersion throughout the zeolite crystals. Treatment of the crystallized zeolites in O.sub.2 and then H.sub.2 forms bimetallic clusters, which remain narrowly distributed in size and composition.

Methods of producing gold-palladium catalysts suitable for use in the production of vinyl acetate may include drying the catalyst after the incorporation of a promoter at higher temperatures (e.g., 160° C. or greater) to restructure the metals and/or alloys on the catalyst. The restructured catalyst advantageously has increased catalytic activity and improved stability.

A long life catalyst is provided that is conveniently and inexpensively capable of being produced and that is highly active and has inhibited metal leakage. According to aspects of the present invention, a catalyst is provided that includes: a polymer including a plurality of first structural units and a plurality of second structural units; and metal acting as a catalytic center, wherein at least part of the metal is covered with the polymer, each of the plurality of first structural units has a first atom constituting a main chain of the polymer and a first substituent group bonded to the first atom, a second atom included in each of the plurality of second structural units is bonded to the first atom, and the second atom is different from the first atom, or at least one of all substituent groups on the second atom is different from the first substituent group.

A process for preparing a catalyst for selective hydrogenation of acetylene to ethylene, comprises: mixing palladium, gallium, and gold sources, silica, and a solvent to form a suspension, which is then subjected to filtration and drying so as to obtain a catalyst precursor; subjecting the catalyst precursor obtained to a calcination treatment; and subjecting a calcinated product obtained to a reduction reaction in a reducing atmosphere so as to obtain the catalyst. The catalyst prepared according to this process exhibits a high stability and high catalytic performance, and has a large number of active sites uniformly distributed.

The disclosure relates to a process to perform an endothermic dehydrogenation and/or aromatization reaction of hydrocarbons, said process comprising the steps of providing at least one fluidized bed reactor comprising at least two electrodes and a bed comprising particles; putting the particles in a fluidized state to obtain a fluidized bed; heating the fluidized bed to a temperature ranging from 480° C. to 700° C. to conduct the reaction; and obtaining a reactor effluent containing hydrogen, unconverted hydrocarbons, and olefins and/or aromatics; wherein the particles of the bed comprise electrically conductive particles and particles of a catalytic composition, wherein at least 10 wt. % of the particles are electrically conductive particles and have a resistivity ranging from 0.001 Ohm.Math.cm to 500 Ohm.Math.cm at 500° C. and wherein the step of heating the fluidized bed is performed by passing an electric current of through the fluidized bed.

The invention relates to a process for removing dienes from a material stream comprising C.sub.3 to C.sub.5 hydrocarbons by selective hydrogenation at a specified reaction pressure and a specified reaction temperature in the presence of a hydrogenation catalyst, wherein the reaction pressure and the reaction temperature at the reactor inlet are regulated such that the reaction pressure at the reactor inlet does not deviate by more than 0.01 bar from the specified reaction pressure and the reaction temperature at the reactor inlet does not deviate by more than 0.1° C. from the specified reaction temperature and the proportion of hydrogen supplied to the selective hydrogenation is in the range from 2 to 20 moles per mole of diene present in the material stream comprising C.sub.3 to C.sub.5 hydrocarbons.

The disclosure relates to a process to perform an endothermic dehydrogenation and/or aromatization reaction of hydrocarbons, said process comprising the steps of providing at least one fluidized bed reactor comprising at least two electrodes and a bed comprising particles; putting the particles in a fluidized state to obtain a fluidized bed; heating the fluidized bed to a temperature ranging from 480° C. to 700° C. to conduct the reaction; and obtaining a reactor effluent containing hydrogen, unconverted hydrocarbons, and olefins and/or aromatics; wherein the particles of the bed comprise electrically conductive particles and particles of a catalytic composition, wherein at least 10 wt. % of the particles are electrically conductive particles and have a resistivity ranging from 0.001 Ohm.Math.cm to 500 Ohm.Math.cm at 500° C. and wherein the step of heating the fluidized bed is performed by passing an electric current of through the fluidized bed.

The invention relates to a process for removing dienes from a material stream comprising C.sub.3 to C.sub.5 hydrocarbons by selective hydrogenation at a specified reaction pressure and a specified reaction temperature in the presence of a hydrogenation catalyst, wherein the reaction pressure and the reaction temperature at the reactor inlet are regulated such that the reaction pressure at the reactor inlet does not deviate by more than 0.01 bar from the specified reaction pressure and the reaction temperature at the reactor inlet does not deviate by more than 0.1° C. from the specified reaction temperature and the proportion of hydrogen supplied to the selective hydrogenation is in the range from 2 to 20 moles per mole of diene present in the material stream comprising C.sub.3 to C.sub.5 hydrocarbons.