Abstract: A process for producing 1,3-butadiene (BD) from ethanol in a single step by s7passing a mixture containing ethanol in a gas phase over a multifunctional catalyst having a transition metal dispersion of at least 30% on a silica metal oxide support. In some examples the multifunctional catalyst comprises a silica metal oxide having a surface area of at least 200 m{circumflex over (?)}2/g. The multifunctional catalyst can include a transition metal oxide, a silica metal oxide made from a high purity silica gel, mesoporous silica and fumed silica, such as high purity SBA16, SBA15, or Davisil grade 646.

Abstract: A simplified processes for producing desired chemicals such as butenes from feedstock mixtures containing ethanol. In one set of embodiments this is performed in a single step, wherein a feed containing ethanol in a gas phase is passed over an acidic metal oxide catalyst having a transition metal dispersion of at least 5% on a metal oxide support. The ethanol content of the feedstock mixture may vary from 10 to 100 percent of the feed and in those non-eat applications the ethanol feed may contain water.

Abstract: In one aspect, the disclosure relates to relates to heterogeneous catalysts useful for the synthesis of ammonia under microwave irradiation, processes for preparing the disclosed heterogeneous catalysts, and processes for synthesizing ammonia using the heterogeneous catalysts with microwave irradiation. In various aspects, the disclosed heterogeneous catalysts comprise: a metal selected from Group 7, Group 8, Group 9, Group 10, Group 11, or combinations thereof; a metal oxide support; and optionally a promoter material. This abstract is intended as a scanning tool for purposes of searching in the particular art and is not intended to be limiting of the present disclosure.

Abstract: A system and process for processing biologically-derived compounds or a complex bio-oil by converting cyclic compounds in a complex bio-oil or biologically-derived compounds to desired materials such as high molecular weight paraffins with minimal carbon loss by using a ring-contraction catalyst to selectively produce C5 ring containing compounds; and then reacting the C5 ring containing compounds with a C5 ring opening catalyst in a second reactor to minimize carbon loss via cracking reactions.

Abstract: A solar thermochemical processing system is disclosed. The system includes a first unit operation for receiving concentrated solar energy. Heat from the solar energy is used to drive the first unit operation. The first unit operation also receives a first set of reactants and produces a first set of products. A second unit operation receives the first set of products from the first unit operation and produces a second set of products. A third unit operation receives heat from the second unit operation to produce a portion of the first set of reactants.

Abstract: A process for producing 1,3-butadiene (BD) from ethanol in a single step by s7 passing a mixture containing ethanol in a gas phase over a multifunctional catalyst having a transition metal dispersion of at least 30% on a silica metal oxide support. In some examples the multifunctional catalyst comprises a silica metal oxide having a surface area of at least 200 m?2/g. The multifunctional catalyst can include a transition metal oxide, a silica metal oxide made from a high purity silica gel, mesoporous silica and fumed silica, such as high purity SBA16, SBA15, or Davisil grade 646.

Abstract: A solar thermochemical processing system is disclosed. The system includes a first unit operation for receiving concentrated solar energy. Heat from the solar energy is used to drive the first unit operation. The first unit operation also receives a first set of reactants and produces a first set of products. A second unit operation receives the first set of products from the first unit operation and produces a second set of products. A third unit operation receives heat from the second unit operation to produce a portion of the first set of reactants.

Abstract: A method for generating desired platform chemicals from feedstocks such as cellulosic biomass feedstocks containing levulinic acid by decarboxylating a feed stock comprising levulinic acid to generate ketones. This is done by passing a feed stock comprising levulinic acid in a gas phase over a non-precious metal catalyst on a neutral support.

Abstract: Disclosed are methods for producing dimethyl ether (DME) from methanol and for producing DME directly from syngas, such as syngas from biomass. Also disclosed are apparatus for DME production. The disclosed processes generally function at higher temperatures with lower contact times and at lower pressures than conventional processes so as to produce higher DME yields than do conventional processes. Certain embodiments of the processes are carried out in reactors providing greater surface to volume ratios than the presently used DME reactors. Certain embodiments of the processes are carried out in systems comprising multiple microchannel reactors.

Abstract: Carbon monoxide (CO) is selectively reacted with hydrogen (H2) over a ruthenium (Ru) on alumina catalyst at a temperature of about 210 to about 290° C. To be a viable option for micro catalytic fuel processing devices, highly active, selective, and stable catalysts must be demonstrated with as large a temperature window for feasible operation as possible. We have studied the effects of metal loading, preparation method, pretreatment conditions, and choice of support on the performance of Ru-based catalysts for such applications. Catalyst testing results and catalyst characterization using XRD and BET are discussed. In one example, operating at a gas hourly space velocity (GHSV) of 13,500 hr?1, a 3% Ru/Al2O3 catalyst yielded CO outputs less than 100 ppm in a temperature range from 240° C. to 285° C., while not exceeding a hydrogen consumption of 10%. This catalyst was further successfully demonstrated in a microchannel device.

Abstract: A compact integrated combustion reactor is described. In a preferred embodiment, the combustion catalyst is disposed in a staggered configuration such that the hot spot in an adjacent endothermic reaction chamber is substantially less than would occur with a conventional, unstaggered configuration. The integrated reactor may also include a methanation chamber for methanation of a reformate product. Systems containing reactant and product streams, and methods of conducting integrated combustion reactions are also described. A staggered catalyst conformation can be used more broadly for thermal chemical reactions requiring heat transfer in a layered device.

Abstract: A new regeneration method has been developed which can effectively and efficiently remove sulfur from Ni-based steam reforming catalysts. In its simplest form the present invention comprises the steps of oxidizing a catalyst with a dilute O2 stream; decomposing the nickel sulfate under inert gas stream and removing sub-surface sulfur under steam reforming conditions. In some embodiments these steps can all be accomplished and the regenerated catalyst be reintroduced to a steam reforming operation in a matter of eight hours or less.

Abstract: Methods for producing alcohols from CO or CO2 and H2 utilizing a palladium-zinc on alumina catalyst are described. Methods of synthesizing alcohols over various catalysts in microchannels are also described. Ethanol, higher alcohols, and other C2+ oxygenates can produced utilizing Rh—Mn or a Fisher-Tropsch catalyst.

Abstract: Methods for producing hydrogen via the water-gas shift reaction utilizing a palladium-zinc on alumina catalyst are described.

Abstract: The invention describes combustors and steam reformers and methods of combustion and steam reforming. For example, integrated combustion reactors are described in which heat from combustion is transferred to an endothermic reaction. Thermally efficient reactors and methods of alcohol steam reforming are also described. Also described is an integrated combustor/reformer containing a methanation catalyst.

Abstract: The present invention provides catalysts, reactors, and methods of steam reforming alcohols over a catalyst. Surprisingly superior results and properties obtained in methods and catalysts of the present invention are also described.

Abstract: The invention describes combustors and steam reformers and methods of combustion and steam reforming. For example, integrated combustion reactors are described in which heat from combustion is transferred to an endothermic reaction. Thermally efficient reactors and methods of alcohol steam reforming are also described. Also described is an integrated combustor/reformer containing a methanation catalyst.

Abstract: The present invention provides steam reforming catalyst compositions containing Pd and Zn, and methods of steam reforming alcohols over a catalyst. Surprisingly superior results and properties of the present invention, including low temperature activity and/or low carbon monoxide output, are also described. Methods of making a steam reforming catalyst are also provided.

Abstract: The present invention provides catalysts, reactors, and methods of steam reforming alcohols over a catalyst. Surprisingly superior results and properties obtained in methods and catalysts of the present invention are also described.

Abstract: Carbon monoxide (CO) is selectively reacted with hydrogen (H2) over a ruthenium (Ru) on alumina catalyst at a temperature of about 210 to about 290° C. To be a viable option for micro catalytic fuel processing devices, highly active, selective, and stable catalysts must be demonstrated with as large a temperature window for feasible operation as possible. We have studied the effects of metal loading, preparation method, pretreatment conditions, and choice of support on the performance of Ru-based catalysts for such applications. Catalyst testing results and catalyst characterization using XRD and BET are discussed. In one example, operating at a gas hourly space velocity (GHSV) of 13,500 hr?1, a 3% Ru/Al2O3 catalyst yielded CO outputs less than 100 ppm in a temperature range from 240° C. to 285° C., while not exceeding a hydrogen consumption of 10%. This catalyst was further successfully demonstrated in a microchannel device.