The present invention relates to a catalytic system comprising:—a support comprising cerium and/or zirconium,—nickel, and—a promoter chosen from lanthanides, yttrium, strontium, copper, manganese, cobalt and mixtures thereof, wherein it is not possible for the lanthanide to be cerium. It also relates to a process for preparing such a catalytic system, and also to a process for converting a gas comprising CO2 and/or CO in the presence of such a catalytic system and of a cold plasma, preferentially generated by dielectric barrier discharge (DBD).

An OCM nanoplate catalyst comprising ≥25 wt. % nanoplates; wherein a nanoplate is a three-dimensional object defined in accordance with ISO/TS 80004-2:2015; wherein a nanoplate is characterized by a first external dimension (thickness (t)≤100 nm), a second external dimension (length (l)>t), and a third external dimension (width (w)>t); wherein l and w can be the same or different; and wherein l≥5 t, w≥5 t, or l≥5 t and w≥5 t; and wherein the OCM nanoplate catalyst has general formula A.sub.aZ.sub.bE.sub.cD.sub.dO.sub.x; wherein A=alkaline earth metal; Z=first rare earth element; E=second rare earth element; D=redox agent/third rare earth element; wherein the first, second, and third rare earth element are not the same; wherein a=1.0; wherein b=1.0 to 3.0; wherein c=0 to 1.5; wherein d=0 to 1.5; wherein (b>(c+d)); and wherein x balances the oxidation states.

The invention relates to a method for converting a gas into methane (CH4) which includes: a step of activating a catalytic material including praseodymium oxide (Pr6O11) associated with nickel oxide (NiO) and alumina (Al2O3), the respective proportions of which are, relative to the total mass of these three compounds: Pr6O11: 1 wt % to 20 wt %, NiO: 1 wt % to 20 wt %, and A12O3: 60 to 98 wt %; and a step of passing a gas including at least one carbon monoxide (CO) over the activated catalytic material.

Nanowires useful as heterogeneous catalysts are provided. The nanowire catalysts are useful in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons. Related methods for use and manufacture of the same are also disclosed.

A mixed oxide catalyst for the oxidative coupling of methane can include a catalyst with the formula A.sub.aB.sub.bC.sub.cD.sub.dO.sub.x, wherein: element A is selected from alkaline earth metals; elements B and C are selected from rare earth metals, and wherein elements B and C are different rare earth metals; the oxide of at least one of A, B, C, and D has basic properties; the oxide of at least one of A, B, C, and D has redox properties; and elements A, B, C, and D are selected to create a synergistic effect whereby the catalytic material provides a methane conversion of greater than or equal to 15% and a C.sub.2.sup.+ selectivity of greater than or equal to 70%. Systems and methods can include contacting the catalyst with methane and oxygen and purifying or collecting C.sub.2.sup.+ products.

Direct conversion of syngas produces liquid fuels and light olefins. The catalytic reaction is conducted on a fixed bed or a moving bed. The catalyst comprises A and B components. The component A is composed of active metal oxides, and the active ingredients of the component B are zeolites with a MEL structure. The distance between the geometric centers of catalyst A and catalyst B particles is 2 nm-10 mm; a weight ratio of the catalyst A to the catalyst B is 0.1-20. The pressure of the syngas is 0.1-10 MPa; reaction temperature is 300-600° C.; and space velocity is 300-10000 h.sup.−1. The reaction mainly produces gasoline with high octane number, and co-generates light olefins. Meanwhile, the selectivity for a methane byproduct is low (less than 10%).

A process for direct synthesis of light olefins uses syngas as the feed raw material. This catalytic conversion process is conducted in a fixed bed or a moving bed using a composite catalyst containing components A and B (A+B). The active ingredient of catalyst A is metal oxide; and catalyst B is an oxide supported zeolite. A carrier is one or more of Al.sub.2O.sub.3, SiO.sub.2, TiO.sub.2, ZrO.sub.2, CeO.sub.2, MgO and Ga.sub.2O.sub.3 having hierarchical pores; the zeolite is one or more of CHA and AEI structures. The loading of the zeolite is 4%-45% wt. A weight ratio of the active ingredients in the catalyst A and the catalyst B is within a range of 0.1-20, and preferably 0.3-5. The total selectivity of the light olefins comprising ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane byproduct is less than 15%.

A catalyst composition, suitable for producing ethylene and other C.sub.2+ hydrocarbons from methane. The composition includes a blended product of two distinct catalyst components, blended at such synergistic proportions, that results in a catalyst having high C.sub.2+ hydrocarbon selectivity while maintaining an overall sufficient catalyst activity and low ethyne selectivity. Methods for preparing such a catalyst composition and a process for producing C.sub.2+ hydrocarbons using such a catalyst composition are provided.

Methods, compositions, and articles of manufacture for alkane activation with single- or bi-metallic catalysts on crystalline mixed oxide supports.

The invention relates to a catalyst composition suitable for the dehydrogenation of paraffins having 2-8 carbon atoms comprising zinc oxide and titanium dioxide, optionally further comprising oxides of cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), lanthanum (La), neodymium (Nd), praseodymium (Pr), samarium (Sm), terbium (Tb), ytterbium (Yb), yttrium (Y), tungsten (W) and Zirconium (Zr) or mixtures thereof, wherein said catalyst composition is substantially free of chromium and platinum. The catalysts possess unique combinations of activity, selectivity, and stability. Methods for preparing improved dehydrogenation catalysts and a process for dehydrogenating paraffins having 2-8 carbon atoms, comprising contacting the mixed metal oxide catalyst with paraffins are also described. The catalyst may also be disposed on a porous support in an attrition-resistant form and used in a fluidized bed reactor.