Abstract: Provided is an internal combustion engine system (1) capable of obtaining sufficient quantity of ethanol by separating a gasoline-ethanol composite fuel to gasoline and ethanol without being affected by components of gasoline. The internal combustion engine system (1) includes a composite fuel storing tank (2), a separation membrane (3) configured to separate a composite fuel to a gasoline component and an ethanol component, and a supplying unit (9) configured to supply the gasoline component and the ethanol component to an internal combustion engine respectively according to operation conditions. The separation membrane (3) is prepared to permeate aromatic hydrocarbons together with ethanol.

Abstract: A selectively permeable membrane type reactor including a catalyst for promoting a chemical reaction, a selectively permeable membrane which selectively allows a specific component to pass therethrough, and a carrier for disposing the catalyst and the selectively permeable membrane the carrier being a tubular body having two or more gas passage cells partitioned and formed by a partition wall formed of a porous body, the catalyst being individually disposed in some of the cells of the carrier, the selectively permeable membrane being individually disposed in the remainder of the cells, and the cell in which the catalyst is disposed and the cell in which the selectively permeable membrane is disposed being adjacently disposed with the partition wall positioned therebetween.

Abstract: A permselective membrane reactor is provided, including a reactor tube having a gas inlet at one end and a gas outlet at the other end thereof. A separator tube is disposed in the reactor tube and has a permselective membrane selectively permeable to hydrogen on a surface thereof and a discharge outlet for passing separated gas through the permselective membrane. The permselective membrane reactor also includes a layer comprising a reforming catalyst that promotes reforming of ethanol, so that ?, defined by the following equation, is in a range of 0.05 to 20: ?=a/b wherein a denotes the volume of the reforming catalyst layer [cm3], and b denotes the area of the permselective membrane [cm2].

Abstract: A selectively permeable membrane reactor includes a reaction tube including a supply port as an inlet port for a raw material gas and a discharge port as an outlet port for an unseparated gas, and a separation tube inserted into the reaction tube. The separation tube includes a selectively permeable membrane exhibiting selective permeability for a specific component on a surface facing the internal space of the reaction tube, and a process port as an outlet port for a separated gas which has passed through the selectively permeable membrane, and a catalyst for promoting a chemical reaction is provided in the reaction tube excluding the separation tube. A catalyst is carried by a foamed body having porous structure to form a foam-molded product and suppresses physical and chemical deterioration in the selectively permeable membrane and allows a mixed gas produced by a catalytic reaction to be efficiently separated.

Abstract: It is disclosed a plasma discharging electrode device generating non-equilibrium plasma for treating a gas. The device has a substrate comprising an integrated sintered ceramic body; an electrode embedded in said substrate; and a catalyst supported by said substrate and accelerating the reaction of the gas. The substrate has a surface portion whose porosity is higher than that of a portion in the vicinity of the electrode in the substrate.

Abstract: There is disclosed a permselective membrane type reactor which efficiently forms hydrogen by use of a water-gas shift reaction and which is excellent in an aspect of manufacturing cost. In a permselective membrane type reactor 100, a permselective membrane 3 is a Pd membrane or a Pd alloy membrane, and a catalyst layer 4 includes a first catalyst layer 4a on the side of the permselective membrane 3 and a second catalyst layer 4b disposed apart from the permselective membrane 3. The first catalyst layer 4a has a noble metal-based catalyst, and the second catalyst layer 4b has an iron-based catalyst.

Abstract: A method for producing hydrogen including the steps of supplying a raw material gas from a gas inlet of a reactor tube; producing a gas mixture containing hydrogen, carbon monoxide, and carbon dioxide by a reforming reaction and a shift reaction; recovering, from a discharge outlet of a separator tube, hydrogen being isolated by passing through a permselective membrane into the separator tube from the gas mixture; and discharging other gas components incapable of passing through the permselective membrane from a gas outlet of the reactor. Hydrogen is produced under conditions where ? defined by the following equation is in the range of 0.4 to 100: ?={(CO2)/(CO)2}/K wherein (CO2) and (CO) denote the partial pressures of carbon dioxide and carbon monoxide at the gas outlet and K denotes the equilibrium constant of the disproportionation reaction of carbon monoxide at the internal temperature of the reactor tube.

Abstract: A permselective membrane type reactor 100 comprises: a cylindrical reaction tube 1 having a gas inlet 11 at one end and a gas outlet 12 at the other end, a cylindrical, bottomed, separation tube 2 inserted into the reaction tube 1, which is made of a porous material and has a permselective membrane 3 at the surface, and a catalyst layer 4 provided between the reaction tube 1 and the separation tube 2, for promotion of chemical reaction. The reactor 100 further comprises, at a location apart from the permselective membrane 3, an oxygen-containing gas feeding section 20 which extends in the gas-flowing direction of the reaction tube 1 and feeds an oxygen-containing gas from multiple positions to the catalyst layer 4 in the gas-flowing direction.

Abstract: There is disclosed a membrane reactor 100 for a shift reaction including a selectively permeable membrane 3 having an H2-selective permeation ability and a catalyst 4 which promotes a chemical reaction, the selectively permeable membrane 3 is a Pd membrane or a Pd alloy membrane, the catalyst 4 is a precious metal catalyst, and the selectively permeable membrane preferably has a thickness of 20 ?m or less. The membrane reactor 100 for the shift reaction simultaneously performs inhibition of a methanation reaction and progression of a shift reaction while preventing deterioration of a thinly formed selectively permeable membrane, whereby hydrogen can efficiently be collected.

Abstract: In a process for producing hydrogen according to the present invention, hydrogen is produced under conditions where hydrogen recovery rate defined by the following equation is in the range of 60% to 99%: Hydrogen recovery rate=100×{A/(A+B)} wherein A denotes the amount of hydrogen that passes through the permselective membrane (the amount of permeated hydrogen) [ml/min], and B denotes the amount of hydrogen that does not pass through the permselective membrane (the amount of non-permeated hydrogen) [ml/min], and where ? defined by the following equation is at least 0.6: ?={(CO2)/(CO)2}/K wherein (CO2) denotes the partial pressure of carbon dioxide at the gas outlet of the reactor tube, (CO) denotes the partial pressure of carbon monoxide, and K denotes the equilibrium constant of the disproportionation reaction of carbon monoxide at the internal temperature of the reactor.

Abstract: There are disclosed a selective permeation membrane reactor which includes a selective permeation membrane having an excellent permeation performance and a separation performance with suppresses of methanation reaction of CO2 contained in hydrogen-containing gas to efficiently perform CO methanation reaction and manufacture highly pure hydrogen, and a method of manufacturing a hydrogen gas. The selective permeation membrane reactor includes a CO reducing unit for reducing carbon monoxide contained in concentrated hydrogen-containing gas; and the unit having a methanation catalyst layer which performs a methanation reaction to reduce carbon monoxide contained in the concentrated hydrogen-containing gas, and a reaction temperature control section for controlling temperature of the catalyst layer at 250° C. or more and 350° C. or less, thereby selectively treating carbon monoxide. As the methanation catalyst, Ru carried by a carrier made of alumina may be used.

Abstract: A process is provided for reforming a hydrocarbon with carbon dioxide using a selectively permeable membrane reactor including a catalyst for accelerating a chemical reaction and a selectively permeable membrane exhibiting selective permeability, wherein a carbon dioxide reforming reaction of the hydrocarbon is accelerated by the catalyst to produce reaction products, and a specific component among the reaction products is allowed to pass through the selectively permeable membrane so specific component is selectively separated. The process includes the steps of adding steam to a raw material gas containing the hydrocarbon and the carbon dioxide and supplying the raw material gas mixture to the selectively permeable membrane reactor.

Abstract: A selectively permeable membrane reactor 100 includes a reaction tube 1 including an internal space 24 having a supply port 22 as an inlet port for a raw material gas 11 and a discharge port 23 as an outlet port for an unseparated gas 12, and a separation tube 4 inserted into the internal space 24 of the reaction tube 1. The separation tube 4 includes a selectively permeable membrane 5 exhibiting selective permeability for a specific component on a surface facing the internal space 24 of the reaction tube 1, and a process port 25 as an outlet port for a separated gas 13 which has passed through the selectively permeable membrane 5, and a catalyst for promoting a chemical reaction is provided in the internal space 24 of the reaction tube 1 excluding the separation tube 4.

Abstract: A laminated zeolite composite is provided, including a MFI membrane constituted by a MFI type zeolite having a SiO2/Al2O3 (molar ratio) of 40 to 100, and a porous substrate constituted by a MFI type zeolite having a SiO2/Al2O3 (molar ratio) of 20 to 400, wherein the MFI membrane is formed on the porous substrate. The composite has high separation characteristics and high permeability.

Abstract: A laminated zeolite composite is provided, including a MFI membrane constituted by a MFI type zeolite having a SiO2/Al2O3 (molar ratio) of 40 to 100, and a porous substrate constituted by a MFI type zeolite having a SiO2/Al2O3 (molar ratio) of 20 to 400, wherein the MFI membrane is formed on the porous substrate. The composite has high separation characteristics and high permeability.

Abstract: A selectively permeable membrane type reactor 20 including a catalyst 6 for promoting a chemical reaction, a selectively permeable membrane 8 which selectively allows a specific component to pass therethrough, and a carrier 22 for disposing the catalyst 6 and the selectively permeable membrane 8, the carrier 22 being a tubular body having two or more gas passages (cells 26) partitioned and formed by a partition wall 24 formed of a porous body, the catalyst 6 being individually disposed in some of the cells 26 of the carrier 22, the selectively permeable membrane 8 being individually disposed in the remainder of the cells 26, and the cell (reaction cell 40, 42) in which the catalyst 6 is disposed and the cell (recovery cell 38) in which the selectively permeable membrane 8 is disposed being adjacently disposed.

Abstract: A process for reforming a hydrocarbon with carbon dioxide using a selectively permeable membrane reactor including a catalyst 1 for accelerating a chemical reaction and a selectively permeable membrane 3 exhibiting selective permeability, wherein a carbon dioxide reforming reaction of the hydrocarbon is accelerated by the catalyst 1 and a specific component among reaction products produced by the reaction is selectively separated by allowing the specific component to pass through the selectively permeable membrane 3, the process including adding steam to a raw material gas containing the hydrocarbon and the carbon dioxide and supplying the mixture to the selectively permeable membrane reactor. According to the present invention, inactivation of the catalyst due to coking can be prevented when carrying out the carbon dioxide reforming reaction of the hydrocarbon using the permeable membrane reactor, whereby the reaction can be efficiently and stably carried out over a long time.

Abstract: A zeolite laminated composite of the present invention is characterized in that it has a separation membrane being constituted by a zeolite, and a porous substrate being constituted by a zeolite and having a catalyst function, and that the separation membrane is formed on the porous substrate. The composite shows a small pressure loss and hardly generates defects such as cracks in the separation membrane even under a high temperature condition.

Abstract: The laminated zeolite composite of the present invention is characterized in that it comprises a MFI membrane being constituted by a MFI type zeolite and having a SiO2/Al2O3 (molar ratio) of 40 to 100, and a porous substrate being constituted by a MFI type zeolite and having a SiO2/Al2O3 (molar ratio) of 20 to 400, and that the MFI membrane is formed on the porous substrate. The composite has high separation characteristic and high permeability.

Abstract: A zeolite laminated composite of the present invention is characterized in that it has a separation membrane being constituted by a zeolite, and a porous substrate being constituted by a zeolite and having a catalyst function, and that the separation membrane is formed on the porous substrate. The composite shows a small pressure loss and hardly generates defects such as cracks in the separation membrane even under a high temperature condition.