The present invention provides a process for producing butadiene by oxidative dehydrogenation of butylene, comprising: a reaction stage, wherein a multi-stage adiabatic fixed bed in series is used, wherein butylene, oxygen-comprising gas and water are reacted in the presence of a catalyst in each stage of the adiabatic fixed bed with the first stage of the adiabatic fixed bed being further separately fed a diluent, being nitrogen and/or carbon dioxide, and the molar ratio between this separately fed diluents and the oxygen of all the oxygen-comprising gases fed in the subsequent stage(s) of the adiabatic fixed bed being controlled, wherein the oxygen-comprising gas is air, oxygen-enriched air or oxygen, and at least one of all the oxygen-comprising gases fed in the subsequent stage(s) of the adiabatic fixed bed is oxygen-enriched air having a specific oxygen concentration or oxygen; and a post treatment stage, wherein the effluent from the last stage of the adiabatic fixed bed is treated to obtain a product butadiene. The present invention has an advantage that the whole process is with reduced total energy consumption.

An object of the present invention is to suppress performance deterioration of a molybdenum composite oxide-based catalyst at the time of performing gas-phase catalytic partial oxidation with molecular oxygen by using a tubular reactor. The present invention relates to a catalytic oxidation method using a tubular reactor in which a Mo compound layer containing a Mo compound and a composite oxide catalyst layer containing a Mo composite oxide catalyst are arranged in this order from a reaction raw material supply port side and under a flow of a mixed gas containing 75 vol % of air and 25 vol % of water vapor at 440 C., a Mo sublimation amount of the Mo compound is larger than a Mo sublimation amount of the Mo composite oxide catalyst under the same conditions.

A method for producing a hydrocarbon molecule by means of energy radiation, comprising: contacting a composite catalyst with at least one hydrogen-containing source and at least one carbon-containing source, and radiating energy to the composite catalyst, the hydrogen-containing source, and the carbon-containing source to produce a hydrocarbon molecule, wherein the composite catalyst contains at least one nano-base structure and at least one atom site, and the atom site comprises one or more chemical elements of Mn, Co, Fe, Ru, Rh, Al, Ag, Au, Pt, Pd, Cu, Ni, Zn, Ti, Os, Ir, and La.

The present disclosure provides an active material comprising a mixed metal oxide in a hydrotalcite derived rocksalt structure, a processes to convert paraffins to corresponding olefins and or heavier hydrocarbons using the active material, and a method of preparing the active material.

A catalyst which is highly active in dehydrogenation reaction of an alkylaromatic hydrocarbon not only in high-temperature regions (e.g. 600 to 650 C.) as found in the inlet of a catalyst bed in an apparatus for the production of SM but also in low-temperature regions (e.g. under 600 C.) as found in the outlet of a catalyst bed in an apparatus for the production of SM, where the temperature decreases as a result of endothermic reaction; and a process for producing the catalyst; and a dehydrogenation process using the catalyst. The catalyst contains iron (Fe), potassium (K), and cerium (Ce), and at least one rare earth element other than cerium.

A method for preparing aromatic hydrocarbons with carbon dioxide hydrogenation, comprising: directly converting a mixed gas consisting of carbon dioxide and hydrogen with the catalysis of a composite catalyst under reaction conditions of a temperature of 250-450 C., a pressure of 0.01-10.0 MPa, a feedstock gas hourly space velocity of 500-50000 mL/(h.Math.g.sub.cat) and a H.sub.2/CO.sub.2 molar ratio of 0.5-8.0, to produce aromatic hydrocarbons. The composite catalyst is a mixture of a first component and a second component. The first component is an iron-based catalyst for making low-carbon olefin via carbon dioxide hydrogenation, and the second component is at least one of metal modified or non-modified molecular sieves which are mainly used for olefin aromatization. In the method, CO.sub.2 conversion per pass may be above 33%, the hydrocarbon product selectivity may be controlled to be above 80%, the methane content is lower than 8%, C.sub.5+ hydrocarbon content is higher than 65% and the proportion of the aromatic hydrocarbons in C.sub.5+ hydrocarbons may be above 63%.

A method of preparing a catalyst for oxidative dehydrogenation that includes coprecipitation and injecting inert gas or air at a specific time point to reduce the ratio of an inactive -Fe.sub.2O.sub.3 crystal structure, thereby improving the activity of the catalyst. Also provided is a method of performing oxidative dehydrogenation using the catalyst. When oxidative dehydrogenation of butene is performed using the catalyst, side reaction may be reduced, and selectivity for butadiene may be improved, providing butadiene with high productivity.

The present invention relates to a method for converting carbon dioxide (CO.sub.2) into high added value chemical compounds under continuous gas flow conditions. In particular, said process converts CO.sub.2 into a mixture of high added value chemical compounds comprising low molecular weight hydrocarbons, mainly methane, ethylene and ethane, along with products of mineral carbonation, mainly Mg and Fe carbonates. Such CO.sub.2 conversion is achieved through a mechanochemical process.

Bimetallic catalysts for the hydrodeoxygenation (HDO) conversion of lignin into useful hydrocarbons are provided. The catalysts are bifunctional bimetallic ruthenium catalysts Ru-M/X.sup.+Y comprising a metal M such as iron (Fe), nickel (Ni), copper (Cu) or zinc (Zn), zeolite Y and cation X.sup.+ (e.g. H.sup.+) associated with zeolite Y.

A methanation reaction catalyst for methanation by allowing carbon dioxide to react with hydrogen, wherein the methanation reaction catalyst includes a stabilized zirconia support having a tetragonal crystal structure and in which Ca and Ni are incorporated in the crystal structure, and Ni in the metal state supported on the stabilized zirconia support, includes the following in atomic % based on metals in the element state, A) Zr composing the stabilized zirconia support: 6 to 62 atomic %, B) Ca incorporated in the crystal structure: 1 to 20 atomic %, and C) a total of Ni incorporated in the crystal structure and Ni supported on the stabilized zirconia support: 30 to 90 atomic %, and the atomic ratio of Ca/(Zr+Ca) is 0.14 to 0.25.