An ammoxidation catalyst includes a metal oxide represented by Chemical Formula 1 supported on a silica carrier, wherein the catalyst has pores having a diameter of 5 to 200 nm, a pore volume of 0.1 to 3.0 cm.sup.3/g, and a BET surface area of 50 m2/g to 1,000 m2/g:
Mo.sub.12Bi.sub.aFe.sub.bA.sub.cB.sub.dC.sub.eO.sub.xChemical Formula 1 wherein in Chemical Formula 1, A is one or more elements of Ni, Mn, Co, Zn, Mg, Ca, and Ba, B is one or more elements of Li, Na, K, Rb, and Cs, C is one or more elements of Cr, W, B, Al, Ca, and V, and a to e, and x are respectively fractions of each atom or atomic group, wherein a is 0.1 to 5, b is 0.1 to 5, c is 0.1 to 10, d is 0.1 to 2, e is 0 to 10, and x is 24 to 48.

An ammoxidation catalyst includes a metal oxide represented by Chemical Formula 1, wherein a first peak having intensity of A appears in the 2 range of 26.3=0.5, and a second peak having intensity of B appears in the 2 range of 28.30.5 in X ray diffraction analysis by CuK, and an intensity ratio (A/B) of the first peak to the second peak is 1.5 or more:
Mo.sub.xBi.sub.aFe.sub.bA.sub.cB.sub.dC.sub.eD.sub.fO.sub.yChemical Formula 1 wherein in Chemical Formula 1, A and B are different from each other, and each independently, are one or more elements of Ni, Mn, Co, Zn, Mg, Ca, and Ba, C is one or more elements of Li, Na, K, Rb, and Cs, D is one or more elements of Cr, W, B, Al, Ca, and V, a to f, x, and y are respectively mole fractions of each atom or atomic group, a is 0.1 to 7, b is 0.1 to 7, provided that the sum of a and b is 0.1 to 7, c is 0.1 to 10, d is 0.01 to 5, e is 0.1 to 10, f is 0 to 10, x is 11 to 14, y is a value determined by each oxidation number of Mo, Bi, Fe, A, B, C, and D.

A porous metal-oxide composite particle suitable for use as a oxygen reduction reaction or oxygen evolution reaction catalyst and sacrificial support based methods for making the same.

A catalyst layer including: (i) a first catalytic material, wherein the first catalytic material facilitates a hydrogen oxidation reaction suitably selected from platinum group metals, gold, silver, base metals or an oxide thereof; and (ii) a second catalytic material, wherein the second catalytic material facilitates an oxygen evolution reaction, wherein the second catalytic material includes iridium or iridium oxide and one or more metals M or an oxide thereof, wherein M is selected from the group consisting of transition metals and Sn, wherein the transition metal is preferably selected from the group IVB, VB and VIB; and the first catalytic material is supported on the second catalytic material. The catalyst can be used in fuel cells, supported on electrodes or polymeric membranes for increasing tolerance to cell voltage reversal.

Oxidative dehydrogenation of paraffins to olefins provides a lower energy route to produce olefins. Oxidative dehydrogenation processes may be integrated with a number of processes in a chemical plant such as polymerization processes, manufacture of glycols, and carboxylic acids and esters. Additionally, oxidative dehydrogenation processes can be integrated with the back end separation process of a conventional steam cracker to increase capacity at reduced cost.

Variations of ZPGM catalyst material compositions including doped CuMn spinel supported on doped zirconia support oxide are disclosed. The disclosed ZPGM catalyst compositions include a small substitution of Ni within the A-site or B-site cation of a CuMn spinel supported on doped zirconia support oxide, and produced by the incipient wetness (IW) methodology. Bulk powder ZPGM catalyst compositions are subjected to XRD analyses to determine the spinel phase formation and stability. Additionally, bulk powder ZPGM catalyst compositions are subjected to a steady-state isothermal sweep test to determine NO, CO, and THC conversion. The ZPGM catalyst material compositions including Ni-doped CuMn spinel supported on doped zirconia support oxide exhibit improved levels in NO and CO conversions, which can be employed in ZPGM catalysts for a plurality of TWC applications, thereby leading to a more effective utilization of ZPGM catalyst materials with high thermal and chemical stability in TWC products.

Variations of coating processes of CuMnFe ZPGM catalyst materials for TWC applications are disclosed. The disclosed coating processes for CuMnFe spinel materials are enabled in the preparation ZPGM catalyst samples according to a plurality of catalyst configurations, which may include an alumina only washcoat layer coated on a suitable ceramic substrate, and an overcoat layer with or without an impregnation layer, including CuMnFe spinel and doped Zirconia support oxide, prepared according to variations of disclosed coating processes. Activity measurements are considered under variety of lean condition to rich condition to analyze the influence of disclosed coating processes on TWC performance of ZPGM catalysts for a plurality of TWC applications. Different coating processes may substantially increase thermal stability and TWC activity, providing improved levels of NO.sub.x conversion that may lead to cost effective manufacturing solutions for ZPGM-TWC systems.

It is possible to obtain a visible light-responsive photocatalytic nanoparticle dispersion liquid containing copper-containing titanium oxide nanoparticles by subjecting an aqueous peroxotitanic acid solution containing a copper compound to hydrothermal reaction for crystallizing the aqueous solution by means of heat under high pressure. The visible light-responsive photocatalytic nanoparticle dispersion liquid thus obtained exhibits excellent dispersion stability of titanium oxide nanoparticles within a water-based dispersion medium even when left in a cold and dark indoor area for a long period of time, expresses photocatalytic activity even in visible light (400 to 800 nm) alone, and can easily create a photocatalytic thin film which is extremely transparent and exhibits excellent durability, and in which the state of copper coordination when exposed to heat or ultraviolet rays is stable and cannot be easily modified.

An iron-free supported catalyst for the selective conversion of hydrocarbons to carbon nanotubes may include cobalt and vanadium as active catalytic metals in any oxidation state on a catalyst support comprising aluminum oxide hydroxide. The mass ratio of cobalt to vanadium is between 2 and 15; the mass ratio of cobalt to aluminum is between 5.810.sup.2 and 5.810.sup.1; and the mass ratio vanadium to aluminum is between 5.810.sup.3 and 8.710.sup.2. The present disclosure is further related to a method for the production of this iron-free supported catalyst and to a method for the production of carbon nanotubes using the iron-free supported catalyst.

This invention relates to a method for the preparation of a hydrocarbon synthesis catalyst material, in the form of a hydrocarbon synthesis catalyst precursor and/or catalyst, preferably, a Fischer Tropsch synthesis catalyst precursor and/or catalyst. The invention also extends to the use of a catalyst precursor and/or catalyst prepared by the method according to the invention in a hydrocarbon synthesis process, preferably, a Fischer Tropsch synthesis process. According to this invention, a method for the preparation of a hydrocarbon synthesis catalyst material includes the steps of treating Fe(II) carboxylate in solution with an oxidizing agent to convert it to Fe(III) carboxylate in solution under conditions which ensure that such oxidation does not take place simultaneously with any dissolution of Fe(0); and hydrolyzing the Fe(III) carboxylate solution resulting from step (iii) and precipitating one or more Fe(III) hydrolysis products.