Abstract: Methods are provided for synthesizing ZSM-58 crystals with an improved morphology and/or an improved size distribution. By controlling the conditions during synthesis of the ZSM-58 crystals, crystals of a useful size with a narrow size distribution can be generated. Steaming the H-form DDR framework type crystals at a temperature from 426±° C. to 1100±° C. for a time period from about 30 minutes to about 48 hours can attain one or more of the following properties: a CH4 diffusivity of no more than 95% of the CH4 diffusivity of the unsteamed H-form DDR framework type crystals; an N2 BET surface area from 85% to 110% of the surface area of unsteamed H-form DDR framework type crystals; and an equilibrium CO2 sorption capacity from 80% to 105% of the equilibrium CO2 sorption capacity of unsteamed H-form DDR framework type crystals.

Abstract: Methods are provided for removing CO2 and/or H2S from a gas phase stream, such as a refinery flue gas stream, a coal-fired or petroleum-burning power plant, or a natural gas stream. A gas phase stream containing CO2 and/or H2S can be contacted under effective conditions with an aqueous slurry of supported amine particles. The CO2 and/or H2S can react with the supported amines to form bicarbonates, carbonates, carbamates, sulfide salts, or other species. Because the amine is part of, bonded to, or otherwise supported on a particulate substrate, the reaction product from the amine reaction can also remain bound to the particle. After reacting supported amines with CO2 and/or H2S captured from a gas stream, the supported amines particles can be separated from the aqueous slurry environment for regeneration of the supported amine and release of the CO2 and/or H2S.

Abstract: Methods are provided for synthesizing ZSM-58 crystals with an improved morphology and/or an improved size distribution. By controlling the conditions during synthesis of the ZSM-58 crystals, crystals of a useful size with a narrow size distribution can be generated. Additionally, by controlling the ratio of water content to silica content in the synthesis mixture, it has unexpectedly been found that ZSM-58 crystals can be formed with an improved morphology. The improved morphology can result in ZSM-58 crystals with a more uniform size across the various dimensions of the crystal, which allows for more uniform diffusion within the crystal. This is in contrast to conventionally synthesized crystals, where the size of the crystal can vary along different axes of the crystals.

Abstract: A cyclic process for selectively separating hydrogen sulfide from a gas mixture including CO2 is operated by contacting the gas mixture under sorption conditions with a non-aqueous sorbent comprising a basic non-protogenic nitrogenous compound to react the H2S with the basic compound so that the H2S can be sorbed by the compound. The compound containing the sorbed H2S can then be subjected to desorption conditions by which the H2S is desorbed and the sorbent readied for another sorption step in the cycle. The basic nitrogenous compound can be carried on a porous solid sorbent, e.g., a solid oxide such as alumina, silica, silica-alumina, zeolites, or a mesoporous and/or macroporous solid oxide. The process may be operated using a pressure swing, temperature swing, partial pressure swing, purge displacement, or a combination thereof between the sorption and desorption portions of the cycle, preferably in a rapid cycle operation.

Abstract: Methods are provided for removing CO2 and/or H2S from a gas phase stream, such as a refinery flue gas stream, a coal-fired or petroleum-burning power plant, or a natural gas stream. A gas phase stream containing CO2 and/or H2S can be contacted under effective conditions with an aqueous slurry of supported amine particles. The CO2 and/or H2S can react with the supported amines to form bicarbonates, carbonates, carbamates, sulfide salts, or other species. Because the amine is part of, bonded to, or otherwise supported on a particulate substrate, the reaction product from the amine reaction can also remain bound to the particle. After reacting supported amines with CO2 and/or H2S captured from a gas stream, the supported amines particles can be separated from the aqueous slurry environment for regeneration of the supported amine and release of the CO2 and/or H2S.

Abstract: A cyclic process for selectively separating hydrogen sulfide from a gas mixture including CO2 is operated by contacting the gas mixture under sorption conditions with a non-aqueous sorbent comprising a basic non-protogenic nitrogenous compound to react the H2S with the basic compound so that the H2S can be sorbed by the compound. The compound containing the sorbed H2S can then be subjected to desorption conditions by which the H2S is desorbed and the sorbent readied for another sorption step in the cycle. The basic nitrogenous compound can be carried on a porous solid sorbent, e.g., a solid oxide such as alumina, silica, silica-alumina, zeolites, or a mesoporous and/or macroporous solid oxide. The process may be operated using a pressure swing, temperature swing, partial pressure swing, purge displacement, or a combination thereof between the sorption and desorption portions of the cycle, preferably in a rapid cycle operation.

Abstract: The invention provides low metal content molecular sieve catalyst compositions, processes for making such catalysts, and processes for using such catalysts in the conversion of an oxygenate into one or more light olefins. Preferably, the catalyst composition comprises a matrix material having a low metal content. By utilizing matrix materials having low metal contents, the amount of metal-catalyzed side reaction byproducts formed in a reaction system, particularly in an oxygenate-to-olefin reaction system, can be advantageously reduced.

Abstract: This invention relates to supported activators comprising the product of the combination of an ion-exchange layered silicate, an organoaluminum compound, and a heterocyclic compound, which may be substituted or unsubstituted. This invention further relates to catalyst systems comprising catalyst compounds and such activators, as well as processes to polymerize unsaturated monomers using the supported activators. For the purposes of this patent specification and the claims thereto, the term “activator” is used interchangeably with the term “co-catalyst”, the term “catalyst” refers to a metal compound that when combined with an activator polymerizes olefins, and the term “catalyst system” refers to the combination of a catalyst and an activator with or without a support. The terms “support” or “carrier”, for purposes of this patent specification, are used interchangeably and are any ion-exchange layered silicates.

Abstract: The invention provides low metal content molecular sieve catalyst compositions, processes for making such catalysts, and processes for using such catalysts in the conversion of an oxygenate into one or more light olefins. Preferably, the catalyst composition comprises a matrix material having a low metal content. By utilizing matrix materials having low metal contents, the amount of metal-catalyzed side reaction byproducts formed in a reaction system, particularly in an oxygenate-to-olefin reaction system, can be advantageously reduced.

Abstract: The present invention includes a fuel cell system and a method to operate a fuel cell. The fuel cell system includes a source of a fuel and water emulsion, receiving the emulsion and. a reformer for receiving the emulsion and producing hydrogen, a hydrogen-oxygen fuel cell connected to the reformer and able to receive hydrogen from the reformer. The method for operating a fuel cell system including a hydrogen gas oxygen fuel cell includes producing the hydrogen gas from a fuel and water emulsion.

Abstract: The present invention includes a fuel cell system and a method to operate a fuel cell. The fuel cell system includes a source of a fuel and water emulsion, receiving the emulsion and a reformer for receiving the emulsion and producing hydrogen, a hydrogen-oxygen fuel cell connected to the reformer and able to receive hydrogen from the reformer. The method for operating a fuel cell system including a hydrogen gas oxygen fuel cell includes producing the hydrogen gas from a fuel and water emulsion.

Abstract: A process for dewaxing waxy hydrocarbonaceous materials, such as hydrocarbon fuel and lubricating oil fractions to reduce their cloud and pour points comprises reacting the material with hydrogen in the presence of a dewaxing catalyst comprising at least one metal catalytic component and ferrierite in which at least a portion of its cation exchange positions are occupied by one or more trivalent rare earth metal cations. The rare earth ion exchanged ferrierite catalyst has good selectivity for lubricating oil production, particularly when dewaxing a Fischer-Tropsch wax hydroisomerate. Preferably at least 10% and more preferably at least 15% of the ferreirite cation exchange capacity is occupied by one or more trivalent rare earth metal cations.

Abstract: Pillared clays composited with Group VIII metals or Group VI metals may be used for the hydroconversion with excellent activity maintenance, of Fischer Tropsch waxes, boiling above about 700.degree. F.

Abstract: A process for dewaxing waxy hydrocarbonaceous materials, such as hydrocarbon fuel and lubricating oil fractions to reduce their cloud and pour points comprises reacting the material with hydrogen in the presence of a dewaxing catalyst comprising at least one metal catalytic component and ferrierite in which at least a portion of its cation exchange positions are occupied by one or more trivalent rare earth metal cations. The rare earth ion exchanged ferrierite catalyst has good selectivity for lubricating oil production, particularly when dewaxing a Fischer-Tropsch wax hydroisomerate. Preferably at least 10% and more preferably at least 15% of the ferreirite cation exchange capacity is occupied by one or more trivalent rare earth metal cations.

Abstract: Ferrierite is ion exchanged with trivalent rare earth metals by a hydrothermal ion exchange method. The ion exchange is carried out by contacting ferrierite, in which its cation exchange positions are occupied by hydrogen or a hydrogen precursor, with an aqueous solution of one or more rare earth metal cations at a temperature above the boiling point of the solution. After the ion exchange, preferably at least 10% and more preferably at least 15% of the ferrierite cation exchange capacity is occupied by a trivalent rare earth metal cation. When combined with a catalytic metal, such as a Group VIII noble metal, the trivalent rare earth metal ion exchanged ferrierite is useful as a dewaxing catalyst having good selectivity for lubricating oil fractions, particularly when dewaxing a Fischer-Tropsch wax hydroisomerate.

Abstract: Hydroconversion of paraffin containing hydrocarbon feeds is effected over a supported Group VIII and Group VI metal containing catalyst also containing a hydrocracking suppressant such as a Group IB metal, wherein the catalyst is preferably prepared by fixing the Group IB metal on to the support prior to incorporating the Group VI metal on to the support.

Abstract: Hydroconversion of paraffin containing hydrocarbon feeds is effected over a supported Group VIII and Group VI metal containing catalyst also containing a hydrocracking suppressant such as a Group IB metal, wherein the catalyst is preferably prepared by fixing the Group IB metal on to the support prior to incorporating the Group VI metal on to the support.

Abstract: The present invention provides for microporous ceramic materials having a surface area in excess of 50 m.sup.2 /gm and an open microporous cell structure wherein the micropores have a mean width of less than 20 Angstroms and wherein said microporous structure comprises a volume of greater than about 0.015 cm.sup.3 /gm of the ceramic. The invention also provides for a preceramic composite intermediate composition comprising a mixture of a ceramic precursor and finely divided particles comprising a non-silicon containing ceramic, carbon, or an inorganic compound having a decomposition temperature in excess of 400.degree. C., whose pyrolysis product in inert atmosphere or in an ammonia atmosphere at temperatures of up to less than about 1100.degree. C. gives rise to the microporous ceramics of the invention.

Abstract: The present invention is directed to a novel catalyst composition and its use in the dehydrogenation of paraffins to olefins. The catalyst comprises an alloy of a Group VIII noble metal and a metal selected from the group consisting of zinc and gallium on a support selected from the group consisting of silica, zinc oxide modified silica and zinc oxide modified silica-pillared clays when said alloy is a zinc alloy, and silica, gallium oxide modified silica and gallium oxide modified silica-pillared clays when said alloy is a gallium alloy. The instant catalyst is an active and selective catalyst for the catalytic dehydrogenation of paraffins to olefins, especially gaseous paraffins, having the added benefit of retaining high activity and selectivity even following repeated regeneration by calcination in oxygen containing gas at temperatures of 450.degree. C. to 650.degree. C., preferably 450.degree. C. to 500.degree. C.

Abstract: The present invention is directed to a novel catalyst composition and its use in the dehydrogenation of paraffins to olefins. The catalyst comprises an alloy of a Group VIII noble metal and a metal selected from the group consisting of zinc and gallium on a support selected from the group consisting of silica, zinc oxide modified silica and zinc oxide modified silica-pillared clays when said alloy is a zinc alloy, and silica, gallium oxide modified silica and gallium oxide modified silica-pillared clays when said alloy is a gallium alloy. The instant catalyst is an active and selective catalyst for the catalytic dehydrogenation of paraffins to olefins, especially gaseous paraffins, having the added benefit of retaining high activity and selectivity even following repeated regeneration by calcination in oxygen containing gas at temperatures of 450.degree. C. to 650.degree. C., preferably 450.degree. C. to 500.degree. C.