Abstract: An iridium-based catalyst and method of making the catalyst are described. The catalyst comprises a catalytic material comprising iridium oxide or a mixture of iridium and iridium oxide nanoplates. It may have a BET surface area of at least 50 m2/g and a pore volume of at least 0.10 cc/g. The nanoplates are less than 50 nm thick. The catalyst is made using organic and inorganic structure directing agents.

Abstract: Catalyst-coated ionically conductive membranes are described. The catalyst-coated ionically conductive membranes comprise an ionically conductive membrane, an anode catalyst coating layer on a first surface of the ionically conductive membrane, or, a cathode catalyst coating layer on a second surface of the ionically conductive membrane, or both wherein the anode catalyst coating layer, or the cathode catalyst coating layer, or both comprises a conductive polymer. Membrane electrode assemblies and electrolysis systems incorporating the catalyst-coated ionically conductive membranes are also described.

Abstract: Water electrolysis catalysts having reduced precious metal loading which are highly active and stable and methods of preparing the water electrolysis catalysts are described. The methods involve depositing a substantially continuous thin shell layer of a platinum group metal (PGM)-based precursor on a nano-sized inorganic oxide core to form a coated inorganic oxide core. The coated inorganic oxide core is heated in the presence of a template to convert the substantially continuous thin shell layer of the PGM-based precursor to a substantially continuous thin shell layer of PGM oxide. The template is then removed forming a water electrolysis catalyst comprising the nano-sized inorganic oxide core having a substantially continuous thin shell layer of the PGM oxide. The water electrolysis catalyst comprises less than 30 wt% of the PGM oxide.

Abstract: A fluidized reforming process comprising a two stage fluidized reforming reactor is described. A naphtha stream flows upward through the two fluidized stages and contacts the catalyst forming a product stream and spent catalyst. The spent catalyst is separated from the product stream and the naphtha feed stream. Some of the spent catalyst is regenerated by contact with an oxygen-containing regeneration fluid to heat and reactivate the catalyst. The heated, regenerated catalyst forms at least a port of the catalyst stream for the process. A process for cyclizing paraffins or isomerizing cyclopentanes is also described. The process uses a chloride-free Pt/Ga-containing catalyst to form a cyclic aliphatic hydrocarbon or isomerizing a cyclopentane in the presence of the chloride-free Pt/Ga-containing catalyst to form a cyclohexane.

Abstract: A method for preparing high specific surface area activated carbon through rapid activation, comprises the following steps: 1) selecting biomass raw material with a particle size of 0.3-0.9 mm; immersing the biomass raw material in a chemical reagent for 3-6 hours; and drying the biomass raw material in a constant-temperature drying oven of 100° C.-150° C. after immersing is ended; 2) stirring or crushing the dried material to form granular material after drying is completed; and 3) adopting a fluidized bed or a spouted bed as an activation reactor; increasing the temperature of the activation reactor to 700-800° C.; introducing fluidized gas; placing quartz sand; placing the granular material obtained in step 2); activating for 1-10 min; immediately discharging the material after activation is ended; and washing the material with water until the material is neutral to obtain activated carbon with a specific surface area of 1267-1359 m2/g.

Abstract: A method for preparing high specific surface area activated carbon through rapid activation, comprises the following steps: 1) selecting biomass raw material with a particle size of 0.3-0.9 mm; immersing the biomass raw material in a chemical reagent for 3-6 hours; and drying the biomass raw material in a constant-temperature drying oven of 100° C.-150° C. after immersing is ended; 2) stirring or crushing the dried material to form granular material after drying is completed; and 3) adopting a fluidized bed or a spouted bed as an activation reactor; increasing the temperature of the activation reactor to 700-800° C.; introducing fluidized gas; placing quartz sand; placing the granular material obtained in step 2); activating for 1-10 min; immediately discharging the material after activation is ended; and washing the material with water until the material is neutral to obtain activated carbon with a specific surface area of 1267-1359 m2/g.