An oxidative dehydrogenation catalyst having: a structure having a formula Mo.sub.vV.sub.wNb.sub.yBi.sub.zO.sub.x, where v is 1, w is from 0.1 to 0.5, y is from 0.001 to 0.3, z is from 0.01 to 0.3, and x is the oxygen content required to charge-balance the structure. The oxidative dehydrogenation catalyst has a Pba2-32 space group, characterized by reflections determined with CuK.sub. X-ray diffraction (XRD) as follows.

The present invention relates to a catalyst having at least one peak in each of a range of a pore diameter of 0.45 m to 10.0 m and a range of a pore diameter of 0.040 m to 0.45 m in a pore distribution (dV/d (log D) vs D) measured by mercury porosimetry, in which when a maximum value of dV/d (log D) in the range of the pore diameter of 0.45 m to 10.0 m is represented by A and a maximum value of dV/d (log D) in the range of the pore diameter of 0.040 m to 0.45 m is represented by B, (B/A) is 0.20 to 13.0 (V represents a volume (unit: mL/g) of filled mercury per sample weight, D represents the pore diameter (unit: m), log D represents a natural logarithm of D, and dV/d (log D) represents a reciprocal of a value obtained by differentiating a cumulative pore volume in a specific pore diameter range by a logarithm of the pore diameter).

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.

The precursor of a hydroprocessing catalyst is made by impregnating a metal oxide component comprising at least one metal from Group 6 of the Periodic Table and at least one metal from Groups 8-10 of the Periodic Table with an amide formed from a first organic compound containing at least one amine group, and a second organic compound containing at least one carboxylic acid group. Following impregnation heat treatment follows to form in situ generated unsaturation additional to that in the two organic compounds. The catalyst precursor is sulfided to form an active, sulfide hydroprocessing catalyst.

The precursor of a hydroprocessing catalyst is made by impregnating a metal oxide component comprising at least one metal from Group 6 of the Periodic Table and at least one metal from Groups 8-10 of the Periodic Table with an amide formed from a first organic compound containing at least one amine group, and a second organic compound containing at least one carboxylic acid group. Following impregnation heat treatment follows to form in situ generated unsaturation additional to that in the two organic compounds. The catalyst precursor is sulfided to form an active, sulfide hydroprocessing catalyst.

An apparatus for efficiently removing the exuded substance and/or the attached substance on the surface of a catalyst (catalyst surface substance) from the catalyst is provided. The apparatus comprising a main body, the apparatus for removing a catalyst surface substance present on a surface of a catalyst from the catalyst by bringing a gas flow into contact with the catalyst housed in the main body, wherein a gas flow length in a flow direction of the gas flow is 55 mm or more, and an average flow velocity of the gas flow is 80 m/s or more and 500 m/s or less in terms of a linear velocity at 15 C. and 1 atm.

An apparatus for efficiently removing the exuded substance and/or the attached substance on the surface of a catalyst (catalyst surface substance) from the catalyst is provided. The apparatus comprising a main body, the apparatus for removing a catalyst surface substance present on a surface of a catalyst from the catalyst by bringing a gas flow into contact with the catalyst housed in the main body, wherein a gas flow length in a flow direction of the gas flow is 55 mm or more, and an average flow velocity of the gas flow is 80 m/s or more and 500 m/s or less in terms of a linear velocity at 15 C. and 1 atm.

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420 C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with H.sub.2O.sub.2 in an amount equivalent to 0.30-2.8 mL H.sub.2O.sub.2 of a 30% solution per gram of catalyst precursor prior to calcining and treating the resulting catalyst with the equivalent amount of peroxide after calcining.

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420 C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with H.sub.2O.sub.2 in an amount equivalent to 0.30-2.8 mL H.sub.2O.sub.2 of a 30% solution per gram of catalyst precursor prior to calcining and treating the resulting catalyst with the equivalent amount of peroxide after calcining.

The present disclosure relates to a composition that includes, in order: a first layer that includes MA.sub.w; a second layer that includes MO.sub.yA.sub.z; and a third layer that includes MO.sub.x, where M includes a transition metal, A includes at least one of sulfur, selenium, and/or tellurium, w is between greater than zero and less than or equal to five, x is between greater than zero and less than or equal to five, y is between greater than zero and less than or equal to five, and z is between greater than zero and less than or equal to five. In some embodiments of the present disclosure, the transition metal may include at least one of molybdenum and/or tungsten. In some embodiments of the present disclosure, A may be sulfur.