Benzene derivatives of the formula (I); ##STR00001##
wherein R.sup.1 and R.sup.2, are the same or different and independently are selected from the group consisting of hydrogen, alkyl, aralkyl, CHO, CH.sub.2OR.sup.3, CH(OR.sup.4)(OR.sup.5) and COOR.sup.6, wherein R.sup.3, R.sup.4 and R.sup.5 are the same or different and are selected from hydrogen, alkyl, aryl, alkaryl, aralkyl, alkylcarbonyl or arylcarbonyl, or wherein R.sup.4 and R.sup.5 together form an alkylene group and wherein R.sup.6 is selected from hydrogen, alkyl and aryl, are prepared in a process, which comprises:
reacting a furan derivative of formula (II): ##STR00002##
wherein R.sup.1 and R.sup.2 have the meanings above, with ethylene under cycloaddition reaction conditions in the presence of an acid solvent to produce the benzene derivative, wherein the acid solvent is a carboxylic acid and is present in a weight ratio acid solvent to furan derivative from 1:1 to 250:1.

The present disclosure relates to catalyst support materials and cobalt catalyst materials including such support materials, and their uses in Fischer-Tropsch processes. In certain aspects, a catalyst support material includes alumina, silicon oxide and titanium dioxide. In other aspects, a catalyst material includes a catalyst support material as described herein, with a catalytic metal such as cobalt disposed thereon.

The present invention relates to a catalytically active material, the preparation thereof, and the use of the catalytically active material, e.g. in the catalytic hydrogenation of CO.sub.2 to methanol. The catalytically active material comprising a metal oxide doped with a doping metal, wherein the metal oxide is selected from CeO.sub.2, ZnO, Ga.sub.2O.sub.3, In.sub.2O.sub.3, ZrO.sub.2, Fe.sub.2O.sub.3 and Al.sub.2O.sub.3, the doping metal is selected from Cu, Rd and Au, and the catalytically active material is obtainable by a method comprising a step of non-thermal plasma treatment.

Captured carbon dioxide is converted into ultra-high purity hydrocarbons, particularly methane. A gas stream containing carbon dioxide is fed to a reactor containing both sorbent and catalyst, until the sorbent portions are substantially saturated with carbon dioxide; non-sorbed species are removed from the first reactor via vacuum and/or purge cycles with high-purity gas; hydrogen gas is introduced to the first reactor to a pressure above ambient; reactor temperature is raised to facilitate desorption of carbon dioxide; and the carbon dioxide is catalytically transformed with the hydrogen gas into methane by recirculating the gas through the reactor. Carbon dioxide adsorption and desorption occur within the sorbent portions, while methanation takes place on the catalytic portions assisted by the sorbent at a temperature substantially consistent with the desorption. Downstream upgrading steps may remove or reduce impurities to produce ultra-high purity methane for chemical vapor deposition or other processes.

The present invention provides a Fischer-Tropsch catalyst comprising greater than about 40% by weight of cobalt, and having a packed apparent bulk density greater than about 1.30 g/mL.

A supported bimetallic catalyst according to the formula Pd-M/Support, which includes palladium and a metal M on a support, wherein M represents Cu or Ag, for use in a method for preparing ethylene glycol from an alcohol. The method includes two reaction steps catalyzed by the bimetallic catalyst of formula Pd-M/Support.

Described are a catalyst for producing isopropylbenzene and the production method and use thereof. The catalyst includes a support and an active component supported on the support, wherein the support comprises a support substrate and a modifying auxiliary component supported on the support substrate, wherein the active component includes metal palladium and/or an oxide thereof, and the modifying auxiliary component is phosphorus and/or an oxide thereof; optionally, the active component further includes metal copper and/or an oxide thereof; the catalyst further includes a sulfur-containing compound.

A method for producing olefins using a circulating fluidized bed process, includes: supplying a propane-containing hydrocarbon mixture and a dehydrogenation catalyst into a riser, which is a fast fluidization regime, to cause a dehydrogenation reaction; separating, from a propylene mixture, the catalyst which is a product of the dehydrogenation reaction; removing unseparated hydrocarbon compounds remaining in the catalyst separated in the separating; continuously regenerating the catalyst by mixing the catalyst stripped in the removing with a gas containing oxygen; circulating the catalyst regenerated in the continuously regenerating to the supplying and resupplying it into the riser; and preparing propylene by cooling, compressing, and separating the propylene mixture which is a reaction product separated in the separating.

The disclosure provides a method of converting carbon dioxide into a reaction product. The method comprises providing a switchable dual function material (DFM) loaded with carbon dioxide; and contacting the switchable DFM loaded with carbon dioxide and a co-reactant, thereby causing the carbon dioxide to react with the co-reactant to produce the reaction product. The switchable DFM comprises an adsorbent, configured to adsorb carbon dioxide; and a switchable catalyst configured to catalyse the conversion of carbon dioxide into a reaction product. The disclosure extends to the switchable DFM per se.

A method may include contacting a hydrocarbon-containing feed with a catalyst in a reactor to form an olefin-containing effluent, then at least partially separating the olefin-containing effluent from the catalyst. Passing the catalyst to a combustor and heating the catalyst by combusting a supplemental fuel. The supplemental fuel includes methane in an amount greater than or equal to 1 mol. %. Passing the catalyst from the combustor to the reactor, such that at least a portion of the catalyst continuously cycles between the reactor and the combustor. The catalyst includes from 0.1 wt. % to 10 wt. % of one or more metals chosen from gallium, indium, thallium or combinations thereof, from 5 ppmw to 1000 ppmw of one or more metals chosen from platinum, palladium, rhodium, iridium, ruthenium, osmium, or combinations thereof, from 100 ppmw to 30000 ppmw of iron, and at least 85 wt. % support.