Systems and methods for the production of n-butene isomers and/or 1,3-butadiene are disclosed. The systems and method involve an oxidative dehydrogenation (ODH) process for the production of n-butene isomers and 1,3-butadiene light olefins using an adjustable, multi-purpose, and multi-layer-catalyst bed for a reactor.

Disclosed is a cyclopropanation process comprising the step of reacting an alkene compound having at least one carbon-carbon double bond with at least one dihaloalkane. The reaction is carried out in the presence of (i) particulate metal Zn, (ii) catalytically effective amount of particulate metal Cu or a salt thereof, (iii) at least one haloalkylsilane, and (iv) at least one solvent.

The current invention belongs to the technical fields of fine chemicals and related chemistry, and provides a preparation method for butadiene derivatives. Arylacetylenes and derivatives using as raw materials react in an anhydrous organic solvent in the presence of a metal catalyst and an additive, and are converted into 2,3-disubstituted-1,3-butadiene derivatives. The current invention has some beneficial characteristics such as cheap and readily available raw material, mild reaction conditions, environmentally friendly property and possibility of realizing industrialization, and obtains the 1,3-butadiene derivatives in high yields. The 1,3-butadiene derivatives synthesized by this method can be further functionalized into various compounds which have potential applications in development and research of natural products, functional materials and fine chemicals.

A process for preparing C.sub.2 to C.sub.3 olefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350 C. to 450 C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of C.sub.2 to C.sub.3 olefins greater than 15 kg C.sub.2 to C.sub.3 olefins/kg catalyst.

This method for producing a fullerene derivative is a method for producing a fullerene derivative having a partial structure shown by formula (1) by reacting a predetermined halogenated compound and two carbon atoms adjacent to each other for forming a fullerene skeleton in a mixed solvent of an aromatic solvent and an aprotic polar solvent having a CO or SO bond in the presence of at least one metal selected from the group comprising manganese, iron, and zinc; ##STR00001## (in formula (1), C* are each carbon atoms adjacent to each other for forming a fullerene skeleton, A is a linking group having 1-4 carbon atoms for forming a ring structure with two C*, in which a portion thereof may be a substituted or condensed group).

The invention relates to a process for the production of an alkene by alkane oxidative dehydrogenation, comprising: (a) subjecting a stream comprising an alkane to oxidative dehydrogenation conditions, comprising contacting the alkane with oxygen in the presence of a catalyst comprising a mixed metal oxide, resulting in a stream comprising alkene, unconverted alkane, water, carbon dioxide, unconverted oxygen, carbon monoxide and optionally an alkyne; (b) removing water from at least part of the stream comprising alkene, unconverted alkane, water, carbon dioxide, unconverted oxygen, carbon monoxide and optionally an alkyne resulting from step (a), resulting in a stream comprising alkene, unconverted alkane, carbon dioxide, unconverted oxygen, carbon monoxide and optionally alkyne; (c) removing unconverted oxygen, carbon monoxide and optionally alkyne from at least part of the stream comprising alkene, unconverted alkane, carbon dioxide, unconverted oxygen, carbon monoxide and optionally alkyne resulting from step (b), wherein carbon monoxide and optionally alkyne are oxidized into carbon dioxide, resulting in a stream comprising alkene, unconverted alkane and carbon dioxide; (d) optionally removing carbon dioxide from at least part of the stream comprising alkene, unconverted alkane in and carbon dioxide resulting from step (c), resulting in a stream comprising alkene and unconverted alkane; (e) optionally separating at least part of the stream comprising alkene and unconverted alkane resulting from step (d), into a stream comprising alkene and a stream comprising unconverted alkane; (f) optionally recycling unconverted alkane from at least part of the stream comprising unconverted alkane resulting from step (e), to step (a).

A hybrid catalyst including a metal oxide catalyst component comprising chromium, zinc, and at least one additional metal selected from the group consisting of aluminum and gallium, and a microporous catalyst component that is a molecular sieve having 8-MR pore openings. The metal oxide catalyst component includes anatomic ratio of chromium:zinc (Cr:Zn) from 0.35 to 1.00, and the at least one additional metal is present in an amount from 25.0 at % to 40.0 at %. A process for preparing C2 and C3 olefins comprising: a) introducing a feed stream comprising hydrogen gas and a carbon-containing gas selected from the group consisting of carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor; and b) converting the feed stream into a product stream comprising C2 and C3 olefins in the reaction zone in the presence of said hybrid catalyst.

Processes for producing two or more different C.sub.2-C.sub.6 linear or branched olefins are disclosed herein. In one exemplary implementation, the process can include contacting a first feed stream that includes -valerolactone with one or more first catalysts in a first reactor to form a mixture. The mixture includes two or more different C.sub.2-C.sub.6 linear or branched olefins at a yield of at least 60%, and the one or more first catalysts include a doped zeolite. Processes for converting levulinic acid to -valerolactone are also disclosed herein.

The present invention provides a pyrolysis tube for manufacturing olefin which tube can improve a yield of olefin in a pyrolysis reaction of a hydrocarbon raw material. The pyrolysis tube (1A) for manufacturing olefin includes a tubular base material (2) made of a heat resistant metal material and a dehydrogenating catalyst (4A) which is supported on an inner surface of the tubular base material (2).

This present disclosure relates to catalytic processes for upgrading crude and/or refined fusel oil mixtures to higher value renewable chemicals, via mixed metal oxide or zeolite catalysts. Disclosed herein are processes passing a vaporized stream of crude and/or refined fusel oils over various mixed metal oxide catalysts, metal doped zeolites, or non-metal doped zeolites and/or metal oxides providing options to valorize fusel oil mixtures to higher value products. Renewable chemicals formed, via these upgrading catalyst platforms, are comprised of, but not limited to, methyl isobutyl ketone (MIBK), di-isobutyl ketone (DIBK), isoamylene, and isoprene.