A catalyst for oxidising ammonia comprises a selective catalytic reduction (SCR) catalyst and a composite heterogeneous extruded honeycomb having longitudinally extending parallel channels, which channels being defined in part by channel walls having a total longitudinal length, wherein the channel walls comprise a pore structure including a periodic arrangement of porous cells embedded in an inorganic matrix component, at least some of which porous cells are defined at least in part by an active interface layer of a catalytically active material comprising a precious metal supported on particles of a support material.

Disclosed is a catalyst for producing the olefin. The catalyst includes a support including alumina and a sub-support component, and a metal oxide impregnated on the support. The metal oxide includes anyone selected from an oxide of chromium, vanadium, manganese, iron, cobalt, molybdenum, copper, zinc, cerium and nickel; and the sub-support component includes anyone selected from zirconium, zinc and platinum.

In order to improve the lifetime of an SCR catalyst in the waste gas purification by means of the SCR process of waste gas of a biomass combustion plant, the catalyst comprises a sacrificial component selected from a zeolite and/or a clay mineral, in particular halloysite. During operation, catalyst poisons contained in the waste gas, in particular alkali metals, are absorbed by the sacrificial component so that catalytically active centers of the catalyst are not blocked by the catalyst poisons.

In order to improve the lifetime of an SCR catalyst in the waste gas purification by means of the SCR process of waste gas of a biomass combustion plant, the catalyst comprises a sacrificial component selected from a zeolite and/or a clay mineral, in particular halloysite. During operation, catalyst poisons contained in the waste gas, in particular alkali metals, are absorbed by the sacrificial component so that catalytically active centers of the catalyst are not blocked by the catalyst poisons.

The invention relates to a process for methanol synthesis comprising the steps of providing a syngas feed stream comprising hydrogen and a mixture of carbon dioxide and carbon monoxide, wherein carbon dioxide represents from 1 to 50 mol % of the total molar content of the feed stream, carbon monoxide is contained from 0.1 to 85 mol % of the total molar content, and H.sub.2 is comprised from 5 to 95 mol % of the total molar content of the feed stream; providing an indium oxide catalyst selected from a bulk catalyst and a supported catalyst comprising indium oxide (In.sub.2O.sub.3) as the main active phase; putting in contact said stream with said catalyst at a reaction temperature of at least 373 K (99.85 C.) and under a pressure ranging of at least 1 MPa; and recovering the methanol effluents. The invention also relates to an indium oxide based catalyst.

Commercial production of sulfuric acid is almost entirely accomplished nowadays using the contact process. And the trend is to increase conversion efficiency and reduce emissions of unconverted sulfur dioxide. By using a special combination of contact catalyst beds, a single contact single absorption (SCSA) system can be engineered to achieve the conversion and emission capabilities of conventional double contact double absorption systems. Thus, the complexity and cost of incorporating a second absorption tower and associated heat exchanger in the system can be omitted. In the SCSA system, the initial catalyst bed or beds comprise vanadium oxide catalyst and the last catalyst bed or beds comprise platinum catalyst operating at a much lower temperature than the initial beds.

Commercial production of sulfuric acid is almost entirely accomplished nowadays using the contact process. And the trend is to increase conversion efficiency and reduce emissions of unconverted sulfur dioxide. By using a special combination of contact catalyst beds, a single contact single absorption (SCSA) system can be engineered to achieve the conversion and emission capabilities of conventional double contact double absorption systems. Thus, the complexity and cost of incorporating a second absorption tower and associated heat exchanger in the system can be omitted. In the SCSA system, the initial catalyst bed or beds comprise vanadium oxide catalyst and the last catalyst bed or beds comprise platinum catalyst operating at a much lower temperature than the initial beds.

A system and method for the conversion of a levulinate ester to maleic anhydride using a reducible oxide catalyst. Levulinic acid oxidation delivers maleic anhydride in good yields without viscosity and stability issues that make continuous production problematic. Due to the fact that levulinate esters are more amenable to processing, the conversion of levulinate esters to maleic anhydride represents an appropriate for the commercial production of maleic anhydride from renewable resources.

A system and method for the conversion of a levulinate ester to maleic anhydride using a reducible oxide catalyst. Levulinic acid oxidation delivers maleic anhydride in good yields without viscosity and stability issues that make continuous production problematic. Due to the fact that levulinate esters are more amenable to processing, the conversion of levulinate esters to maleic anhydride represents an appropriate for the commercial production of maleic anhydride from renewable resources.

Provided in this disclosure are oxidative dehydrogenation catalysts that include a mixed metal oxide having the empirical formula:

Mo.sub.1.0V.sub.0.12-0.49Te.sub.0.05-0.17Nb.sub.0.10-0.20O.sub.d

wherein d is a number to satisfy the valence of the oxide. The oxidative dehydrogenation catalyst is characterized by having XRD diffraction peaks (2 degrees) at 220.2, 270.2, 28.00.2, and 28.30.1. The disclosure also provides methods of making the catalysts that include wet ball milling.