A process for dehydrogenating alkane or alkylaromatic compounds comprising contacting the given compound and a dehydrogenation catalyst in a fluidized bed. The dehydrogenation catalyst is prepared from an at least partially deactivated platinum/gallium catalyst on an alumina-based support that is reconstituted by impregnating it with a platinum salt solution, then calcining it at a temperature from 400° C. to 1000° C., under conditions such that it has a platinum content ranging from 1 to 500 ppm, based on weight of catalyst; a gallium content ranging from 0.2 to 2.0 wt %; and a platinum to gallium ratio ranging from 1:20,000 to 1:4. It also has a Pt retention that is equal to or greater than that of a fresh catalyst being used in a same or similar catalytic process.

An apparatus to decompose a hydrocarbon reactant into a gaseous product and a solid product includes a reactor volume, a reservoir of liquid material, a plurality of nozzles connected to the reservoir of liquid material, the plurality of nozzles configured to distribute the liquid material into the reactor volume from the reservoir as a liquid mist, a gas inlet connected to a hydrocarbon gas source to receive hydrocarbon gas reactant, a distributor connected to the inlet to distribute the hydrocarbon gas reactant into the reactor volume, a heat source located adjacent the reactor volume configured to heat the reactor volume, a separator to separate the solid product from the liquid material, a re-circulation path connected between the reactor volume and the reservoir to re-circulate the liquid material from the reactor volume to the reservoir, a gas outlet connected to the reactor volume configured to outlet hydrogen gas from the reactor volume, and at least one filter connected to the gas outlet to remove entrained solid product from the hydrogen gas.

An apparatus to decompose a hydrocarbon reactant into a gaseous product and a solid product includes a reactor volume, a reservoir of liquid material, a plurality of nozzles connected to the reservoir of liquid material, the plurality of nozzles configured to distribute the liquid material into the reactor volume from the reservoir as a liquid mist, a gas inlet connected to a hydrocarbon gas source to receive hydrocarbon gas reactant, a distributor connected to the inlet to distribute the hydrocarbon gas reactant into the reactor volume, a heat source located adjacent the reactor volume configured to heat the reactor volume, a separator to separate the solid product from the liquid material, a re-circulation path connected between the reactor volume and the reservoir to re-circulate the liquid material from the reactor volume to the reservoir, a gas outlet connected to the reactor volume configured to outlet hydrogen gas from the reactor volume, and at least one filter connected to the gas outlet to remove entrained solid product from the hydrogen gas.

A method to decompose a hydrocarbon reactant into a gaseous product and a solid product includes generating a mist of a liquid material within a reactor volume, heating the reactor volume, introducing a hydrocarbon reactant into the reactor volume to produce a solid product and a gaseous product, separating the solid product from the liquid material, removing the solid product and gaseous product from the reactor volume, and recirculating the liquid material be re-introduced to the reactor volume.

A method to decompose a hydrocarbon reactant into a gaseous product and a solid product includes generating a mist of a liquid material within a reactor volume, heating the reactor volume, introducing a hydrocarbon reactant into the reactor volume to produce a solid product and a gaseous product, separating the solid product from the liquid material, removing the solid product and gaseous product from the reactor volume, and recirculating the liquid material be re-introduced to the reactor volume.

A lignocellulosic starting material can be converted into an aqueous phase and a hydrocarbon phase in a one-step process by subjecting a mixture of the lignocellulosic starting material, an amorphous and unsupported sulfided nickel-molybdenum catalyst, and optionally a co-feed, to not less than a stoichiometric amount of hydrogen, elevated pressure and a temperature in the interval of 350-450° C. A novel catalyst for use in said process and a method for its production are also disclosed.

A system and method of producing carbon nanotubes from flare gas and other gaseous carbon-containing sources.

A system and method of producing carbon nanotubes from flare gas and other gaseous carbon-containing sources.

A catalytic upgrading process includes introducing a feed comprising crude oil to a first catalytic deasphalting reactor to deasphalt the feed, thereby producing polymerized asphaltenes and deasphalted oil (DAO). The DAO is introduced to a steam cracking unit, thereby producing pyrolysis gas (PG), which is introduced into a selective hydrogenation unit, thereby producing an olefin-free product, which can then be introduced to a separation unit. The resulting benzene-toluene-xylenes (BTX)-containing stream and liquid petroleum gas (LPG) are separated, and the BTX-containing stream is introduced to a BTX complex to produce refined BTX. After deasphalting, a wash solvent may be introduced into the first catalytic deasphalting reactor to remove the polymerized asphaltenes, regenerate the catalyst, and produce a mixture comprising the wash solvent and the polymerized asphaltenes. The wash solvent is separated from the polymerized asphaltenes.

A mesoporous ozonation catalyst including a cerium-titanium-zirconium composite oxide. The catalyst is in the form of a solid spherical particle having a diameter of between 0.7 and 1.2 mm. The solid spherical particle exhibits lattice fringes under transmission electron microscope, and the lattice fringes have a spacing between 0.332 and 0.339 nm.