Abstract: For recovering hydrogen with a high recovery from a reformed gas and contributing to downsizing and cost reduction of facilities, a high-purity hydrogen E is obtained by reforming a reformable raw material A through a reforming unit 1 to yield a hydrogen-rich reformed gas B, compressing the hydrogen-rich reformed gas B with a compressor 2, allowing the compressed gas to pass through a PSA unit 3 to remove unnecessary gases other than carbon monoxide by adsorption, and allowing the resulting gas to pass through a carbon monoxide remover 4 packed with a carbon monoxide adsorbent supporting a copper halide to remove carbon monoxide by adsorption.

Abstract: A PSA apparatus for high-purity hydrogen gas production is provided which can recover high purity hydrogen gas at a high recovery rate from a reformed gas (hydrogen-containing gas) produced by a reforming process, for example an autothermal reforming process, and containing, as impurity components, at least CO, CO2, N2 and/or Ar, and can contribute to reducing the equipment size, hence reducing the equipment cost. The PSA apparatus for high-purity hydrogen gas B production by removing CO, CO2 and N2 by adsorption from a hydrogen containing gas A, comprises an adsorption tower 1; and an adsorbent bed 2 in the adsorption tower, wherein, on the occasion of regeneration of the adsorbent bed 2, a purge gas C is passed through in the direction opposite to the direction of passage of the hydrogen-containing gas A.

Abstract: A PSA apparatus for high-purity hydrogen gas production is provided which can recover high-purity hydrogen gas at a high recovery rate from a reformed gas (hydrogen-containing gas) produced by a reforming process, for example an autothermal reforming process, and containing, as impurity components, at least CO, CO2, N2 and/or Ar, and can contribute to reducing the equipment size, hence reducing the equipment cost.

Abstract: For recovering hydrogen with a high recovery from a reformed gas and contributing to downsizing and cost reduction of facilities, a high-purity hydrogen E is obtained by reforming a reformable raw material A through a reforming unit 1 to yield a hydrogen-rich reformed gas B, compressing the hydrogen-rich reformed gas B with a compressor 2, allowing the compressed gas to pass through a PSA unit 3 to remove unnecessary gases other than carbon monoxide by adsorption, and allowing the resulting gas to pass through a carbon monoxide remover 4 packed with a carbon monoxide adsorbent supporting a copper halide to remove carbon monoxide by adsorption.

Abstract: Disclosed herein is a hydrogen permeable member composed of a metal porous body and a hydrogen permeable membrane placed thereon, with a diffusion preventing layer interposed between them, wherein the metal porous body has those parts on which the diffusion preventing layer is absent and such parts are filled with metal oxide particles and/or porous metal oxide. This structure prevents direct contact between the metal porous body and the hydrogen permeable membrane, thereby relieving the latter from deterioration by diffusion of metal from the former.

Abstract: A method for concentrating 2,6-dimethylnaphthalene in a dimethylnaphthalene isomer mixture includes supplying the dimethylnaphthalene isomer mixture to an adsorption column packed with Y-type zeolite. In this instance, by setting the value derived from the expression (u1/3/&egr;)d−5/3 at 14 (m5/3 s−1/3 kg−1) or more, the concentration ratio of 2,6-dimethylnaphthalene to 2,7-dimethylnaphthalene can be 2.0 or more. u here represents the linear velocity (m/s) of the dimethylnaphthalene isomer mixture supplied to an adsorption column, &egr; represents the packing density (kg/m3) of Y-type zeolite, and d represents the grain size (m) of the Y-type zeolite.

Abstract: A method for concentrating 2,6-dimethylnaphthalene in a dimethylnaphthalene isomer mixture includes supplying the dimethylnaphthalene isomer mixture to an adsorption column packed with Y-type zeolite. In this instance, by setting the value derived from the expression (u⅓/&egr;)d−5/3 at 14 (m5/3 s−⅓kg−1) or more, the concentration ratio of 2,6-dimethylnaphthalene to 2,7-dimethylnaphthalene can be 2.0 or more. u here represents the linear velocity (m/s) of the dimethylnaphthalene isomer mixture supplied to an adsorption column, &egr; represents the packing density (kg/m3) of Y-type zeolite, and d represents the grain size (m) of the Y-type zeolite.

Abstract: A method comprising the steps of: allowing the directions of a magnetic field, an electric current and the liquid metal flow to perpendicularly intersect to one another; and varying at least one of the magnetic field and the electric current in intensity in response to the temperature of the liquid metal. A force acting on the liquid metal flow is increased and decreased by the interaction between the magnetic field and the electric current. An apparatus for performing the method comprising material varying in electric property with the temperature of the liquid metal. The material is installed in at least one of a path of the magnetic field, a path of the electric current and means for generating the magnetic field. Variation of the electric property of the material allows one of the magnetic field and the electric current to be automatically increased or decreased in intensity in response to the temperature of the liquid metal, so that the force acting on the liquid metal flow is controlled.