A method for regenerating a deNO.sub.x catalyst includes contacting the catalyst with steam at a temperature in the range of from 250 to 390° C. The method also includes reducing the amount of nitrogen oxide components in a process gas stream that includes a) contacting the process gas with a deNO.sub.x catalyst which results in the conversion of nitrogen oxide components as well as a decline in the NO.sub.x conversion over the deNO.sub.x catalyst; and b) regenerating the deNO.sub.x catalyst to improve the NO.sub.x conversion by contacting the deNO.sub.x catalyst with steam at a temperature in the range of from 250 to 390° C.

A method for regenerating a deNO.sub.x catalyst includes contacting the catalyst with steam at a temperature in the range of from 250 to 390° C. The method also includes reducing the amount of nitrogen oxide components in a process gas stream that includes a) contacting the process gas with a deNO.sub.x catalyst which results in the conversion of nitrogen oxide components as well as a decline in the NO.sub.x conversion over the deNO.sub.x catalyst; and b) regenerating the deNO.sub.x catalyst to improve the NO.sub.x conversion by contacting the deNO.sub.x catalyst with steam at a temperature in the range of from 250 to 390° C.

The oxidative dehydrogenation of ethane comprises contacting a mixture of ethane and oxygen in an ODH reactor with an ODH catalyst under conditions that promote oxidation of ethane into ethylene. Conditions within the reactor are controlled by the operator and include, but are not limited to, parameters such as 5 temperature, pressure, and flow rate. Conditions will vary and can be optimized for a specific catalyst, or whether an inert diluent is used in the mixing of the reactants. Disclosed herein is a catalyst consisting of: Mo.sub.0-1W.sub.0.3-1V.sub.0.2-0.4Te.sub.0.06-0.10Fe.sub.0.0-0.10Nb.sub.0.08-0.18O.sub.X where X is determined by the valance of the metals.

A method of recovering catalyst performance includes providing a vanadium selective catalytic reduction (VSCR) catalyst. The method includes exposing the VSCR catalyst to a first humidity level in a range of 50%-100% relative humidity, at a first temperature in a range of 20° C.-100° C., for a first period of time of at least two hours. The method includes thermally treating the VSCR catalyst at a second temperature in a range of 300° C.-600° C. for a second period of time of at least than one hour.

A method of recovering catalyst performance includes providing a vanadium selective catalytic reduction (VSCR) catalyst. The method includes exposing the VSCR catalyst to a first humidity level in a range of 50%-100% relative humidity, at a first temperature in a range of 20° C.-100° C., for a first period of time of at least two hours. The method includes thermally treating the VSCR catalyst at a second temperature in a range of 300° C.-600° C. for a second period of time of at least than one hour.

Processes for forming multimetallic catalysts by grafting nickel precursors to metal oxide supports. Dry reforming reaction catalysts having nickel and promotors grafted to metal oxides supports. Methanation reaction catalysts having nickel and promotors grafted to metal oxides supports.

Processes for forming multimetallic catalysts by grafting nickel precursors to metal oxide supports. Dry reforming reaction catalysts having nickel and promotors grafted to metal oxides supports. Methanation reaction catalysts having nickel and promotors grafted to metal oxides supports.

The present invention provides a catalyst composition for the production of olefins from lighter alkanes by oxidative dehydrogenation route and methods of making the dehydrogenation catalyst composites.

The present invention provides a catalyst composition for the production of olefins from lighter alkanes by oxidative dehydrogenation route and methods of making the dehydrogenation catalyst composites.

The invention relates to a shaped catalyst body in the form of a tetralobe having four circular through-passages, with the midpoints of the through-passages forming a square and the spacings between in each case two adjacent through-passages being from 0.8 to 1.2 times the thickness of the outer walls of the through-passages. The shaped catalyst body is used for the oxidation of S02 to S03.