Chiyoda Corporation

Kenichi Imagawa

Hironori Kawai

Yoshimi Okada

Yusuke Nakajima

Masato Shiraga

Osamu Ikeda

Susumu Yamamoto

Takeshi Minami

Shinichi Inoue

Atsuro Nagumo

Haruto Kobayashi

Tomoyuki Mikuriya

Tetsuro Matsumura

Akihiro Muto

Tomohiko Shirasaki

Tatsuo Ishiyama

Takenori Kanda

Shinichi Nakata

A hydrogenation catalyst with a small amount of supported metal that is excellent in stability and inhibition of side reactions is provided. The catalyst hydrogenates an aromatic hydrocarbon compound into an alicyclic hydrocarbon compound, and a Group X metal represented by nickel is supported in a composite support including at least alumina and titania. The composite support preferably includes at least an alumina substrate coated with titania. It is also preferable that the Group X metal is prereduced by hydrogen. In the case that the Group X metal is nickel, the nickel content is preferably 5-35 wt % as nickel oxide in the catalyst. The substrate includes, for example, a porous structure formed by a plurality of needle-shaped or column-shaped intertwined three-dimensionally.

Hydrogenation catalyst for aromatic hydrocarbon and hydrotreatment method using the catalyst

To reduce the emission of carbon dioxide and improve the energy efficiency in a hydrogen supply system. The hydrogen supply system () comprises: a reformer () for performing steam reforming of a hydrocarbon; a shift reaction unit () for producing a gas containing hydrogen and carbon dioxide by causing a water gas shift reaction of a gas obtained from the reformer; a first absorber () for absorbing the carbon dioxide contained in the gas obtained from the shift reaction unit in an absorption liquid; a hydrogenation reaction unit () for producing a hydrogenated aromatic compound by causing a hydrogenation reaction of an aromatic compound with a gas that has passed through the first absorber; and a regenerator () for separating the carbon dioxide from the absorption liquid by re-circulating the absorption liquid from the first absorber and heating the absorption liquid with heat generated from the hydrogenation reaction.

Systems and methods for producing hydrogen from a hydrocarbon and using the produced hydrogen in a hydrogenation reaction

To allow hydrogen to be supplied to a dehydrogenation reaction unit for dehydrogenating an organic hydride by using a highly simple structure so that the activity of the dehydrogenation catalyst of the dehydrogenation reaction unit is prevented from being rapidly reduced. The hydrogen production system () comprises a first dehydrogenation reaction unit () for producing hydrogen by a dehydrogenation reaction of an organic hydride in presence of a first catalyst, and a second dehydrogenation reaction unit () for receiving a product of the first dehydrogenation reaction unit, and producing hydrogen by a dehydrogenation reaction of the organic hydride remaining in the product in presence of a second catalyst, wherein an amount of the first catalyst used in the first dehydrogenation reaction unit is equal to or less than an amount of the second catalyst used in the second dehydrogenation reaction unit, and an amount of hydrogen produced in the first dehydrogenation reaction unit is less than an amount of hydrogen produced in the second dehydrogenation reaction unit.

System and method for producing hydrogen

The energy is minimized that is required to lower the concentration of the high boiling point components (containing the poisoning substance for the dehydrogenation catalyst) contained in the hydrogenated aromatic compound produced by the hydrogenation of an aromatic compound. The hydrogenation system () for an aromatic compound comprises a hydrogenation reaction unit () for adding hydrogen to an aromatic compound by a hydrogenation reaction to produce a hydrogenated aromatic compound, a first separation unit () for separating a gas and a liquid component from a product of the hydrogenation reaction unit while maintaining a temperature of the product generally higher than a boiling point of the hydrogenated aromatic compound, and a second separation unit () for separating the hydrogenated aromatic compound from the gas component separated by the first separation unit.

Hydrogenation system for aromatic compound, hydrogen storage and transportation system equipped with same, and process for hydrogenation of aromatic compound

A catalyst for manufacturing synthesis gas has a carrier and a Group VIII metal carried by the carrier. The carrier contains a first ingredient, a second ingredient and a third ingredient. The first ingredient is an oxide of at least an alkaline earth metal selected from the group of magnesium, calcium, strontium and barium. The second ingredient is an oxide of at least an element selected from the group of scandium, yttrium and lanthanoids. The third ingredient is zirconia or a substance containing zirconia as principal ingredient and has a solid electrolytic property. The carrier may be formed by forming an overcoat film on a substrate by coating. Then, the overcoat film contains the above three ingredients. A catalyst according to the invention can remarkably reduce the dimensions of the reaction facility and improve the energy efficiency of the facility.

Catalyst for manufacturing synthesis gas and method of manufacturing synthesis gas using the same

A porous spinel type oxide shows a large surface area and a uniform micro-porous structure. The oxide is expressed by general formula MO&mdash;Al,O,and shows a surface area per unit weight of not less than 80 m,/g. Such a porous spinel type compound oxide is obtained by impregnating a specific &ggr;-alumina carrier with a solution of a compound of metal element M capable of taking a valence of 2, drying the impregnated carrier and calcining it at a temperature of 600&deg; C. or higher. The specific &ggr;-alumina carrier shows a surface area per unit weight of not less than 150 m,/g, a micro-pore volume per unit weight of not less than 0.55 cm,/g and an average micro-pore diameter between 90 and 200 angstroms. The micro-pores with a diameter between 90 and 200 angstroms occupy not less than 60% of the total micro-pore volume of the carrier.

Spinel type compound oxide and method of manufacturing the same

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Yokohama, Japan

Kenichi Imagawa