Chiyoda Corporation

Chiyoda Chemical Engineering Construction Co., Ltd.

Nippon Steel Chemical Co., Ltd.

The Nisshin Oil Mills, Ltd.

Nkk Corporation

Sachio Asaoka

Yoshimi Shiroto

Nobuo Moriya

Kouji Sakashita

Tetsuo Maejima

Noriyuki Yoneda

Hiroaki Nishijima

Makoto Yasui

Fuyuki Yagi

Munekazu Nakamura

Shuhei Wakamatsu

Nobuhiro Onda

Akio Shindo

Tsuneo Watanabe

Mitsunori Shimura

Takeo Ono

Ryuichi Inaba

Takashi Imazeki

Susumu Yamamoto

Atsuro Nagumo

Yukitaka Wada

Athumi Kukidome

Kaoru Shimogawara

Kazushige Kawamura

Takeshi Minami

Dai Takeda

Haruto Kobayashi

Shinya Hodoshima

Tadasu Fujita

Osamu Togari

Katsuhiko Sakura

Yuzo Ikuta

Azusa Motomiya

Satoshi Tashiro

Keiji Shimoda

Yoshiyuki Hatano

Takashi Sendo

Noboru Andoh

Toshihiko Furukawa

Nobuyuki Suda

Minoru Uchida

Hiroaki Taniguchi

Yoshimi Okada

Yoichi Umehara

Yoshio Fukui

Yakudo Tachibana

Kazuhiko Tate

Hideki Sugiyama

Kazuhiko Hamato

Kenji Shimokawa

Makoto Nomura

Ryuichi Kanai

Fumiaki Tanaka

Takao Kameda

Takeshi Kouzaki

Hiroto Tajima

Nobuaki Egashira

Kazuaki Ueda

Tadami Kondoh

Naonori Sonehara

Athumi Kukudome

Karou Shimogawara

Mamoru Iwasaki

Hiroshi Yanai

Tadayoshi Matsuo

Tsohikazu Maruyama

Yoshiaki Matsui

Masanori Nagase

Takamasa Minami

Kiyoshi Hashimoto

Provided are zeolite catalysts that allow reactions to proceed at temperatures as low as possible when lower olefins are produced from hydrocarbon feedstocks with low boiling points such as light naphtha, make it possible to make propylene yield higher than ethylene yield in the production of lower olefins, and have long lifetime. The zeolite catalysts are used in the production of lower olefins from hydrocarbon feedstocks with low boiling points such as light naphtha. The zeolite catalysts are MFI-type crystalline aluminosilicates containing iron atoms and have molar ratios of iron atoms to total moles of iron atoms and aluminum atoms in the range from 0.4 to 0.7. The use of the zeolite catalysts make it possible to increase propylene yield, to lower reaction temperatures, and to extend catalyst lifetime.

Zeolite catalysts, methods for producing zeolite catalysts, and methods for producing lower olefins

Active carbon catalyst for recovering and removing sulfur oxides contained in flue gas by turning them into sulfuric acid by a catalytic desulfurization reaction. Powdery active carbon and fluororesin are kneaded by shearing force before being molded to a desired profile so that the inter-particulate gaps of powdery active carbon particles are made water-repellent. Flue gas preferably flows downwardly through a tower filled with such an active carbon catalyst, which is made to show a honeycomb structure having surfaces running only in a direction parallel to the flow. The activity of the catalyst maintains an enhanced level if dilute sulfuric acid or water is introduced into the active carbon from the top of the tower to cleanse the surface of the active carbon catalyst so that the catalyst layer is prevented from being clogged and contaminated by ashes and soot contained in flue gas.

Desulfurization of exhaust gases using activated carbon catalyst

Disclosed are a catalyst for producing a synthesis gas using a carbon-containing organic compound as a raw material and a process for producing carbon monoxide. The catalyst for producing a synthesis gas is composed of a carrier formed of a metal oxide and at least one catalytic metal selected from rhodium, ruthenium, iridium, palladium and platinum and supported on the carrier and is characterized in that the catalyst has a specific surface area of 25 m /g or less, in that the electronegativity of the metal ion of the carrier metal oxide is 13.0 or less and in that the amount of the supported catalytic metal is 0.0005-0.1 mole %, in terms of a metal, based on the carrier metal oxide. The process for producing carbon monoxide includes a step of reacting a carbon-containing organic compound with carbon dioxide in a pressurized condition to produce a synthesis gas, and a step of concentrating carbon monoxide in the thus obtained synthesis gas and is characterized in that the above-described catalyst is used as a catalyst in the synthesis gas producing step.

Catalyst for preparation of synthesis gas and process for preparing carbon monoxide

Disclosed is a process for producing a synthesis gas by an autothermal reforming method including a step of partially oxidizing a carbon-containing organic compound to produce a high temperature mixed gas, and a synthesis producing step of reacting the unreacted carbon-containing organic compound contained in the high temperature mixed gas with carbon dioxide and/or steam, wherein a catalyst having a considerably suppressed carbon deposition activity is used as a catalyst for the synthesis gas producing step. The catalyst is characterized in that the catalyst comprises a carrier formed of a metal oxide, and at least one catalytic metal selected from rhodium, ruthenium, iridium, palladium and platinum and supported on the carrier, in that the catalyst has a specific surface area of 25 m /g or less, in that metal ion of the carrier metal oxide has electronegativity of 13.0 or less, and in that the amount of the catalytic metal supported is 0.0005-0.1 mole %, in terms of a metal, based on the carrier metal oxide.

Process for preparing synthesis gas by autothermal reforming

A process for the wet processing of a dioxin-containing material, wherein the material is contacted with an aqueous solution, acidified with hydrochloric acid and containing a catalyst dissolved therein, at a temperature lower than 100&deg; C. to decompose the dioxins into harmless substances with a decomposition rate of at least 60%.

Wet type method of rendering dioxins innoxious

Disclosed is a process for producing a synthesis gas by reacting a carbon-containing organic compound with steam and/or carbon dioxide using a catalyst whose carbon deposition activity is considerably suppressed. The catalyst is characterized in that it comprises a carrier formed of a metal oxide, and at least one catalytic metal selected from rhodium, ruthenium, iridium, palladium and platinum and supported on the carrier, in that the catalyst has a specific surface area of 25 m,/g or less, in that the electronegativity of the metal ion of the carrier metal oxide is 13.0 or less and in that the amount of the catalytic metal is 0.0005-0.1 mole %, in terms of metal, based on the carrier metal oxide.

Process for preparing synthesis gas

Transesterification involving a fat, or a fat and fatty acid, or a phospholipid is carried out with a lipase or phospholipase immobilized on a polymer carrier. The transesterification is preferably carried out in a system containing a very small amount of water such as 50 to 2,000 ppm. The phospholipase can be phospholipase A.sub.2. In a first embodiment, lipase from a microorganism of the genus Rhizopus, Mucor, Alcaligenes or Candida is immobilized on the surface of a hydrophobic, insoluble organic polymer carrier having pores of an average diameter of 10 nm or larger and having on the surface epoxy groups capable of covalently binding lipase. The immobilized lipase is dried under reduced pressure. In a second embodiment, lipase is immobilized on the surface of a polymer carrier such as a hydrophobic, insoluble organic polymer carrier having a pore diameter of 5 to 1,000 nm and having on the surface a functional group capable of binding lipase and an anion-exchange group. Preferably, the functional group is an epoxy group and the anion-exchange group is a tertiary amino group. The lipase may be obtained from the same microorganism as in the first embodiment or from another lipase-producing microorganism. Iramobilization can be carried out as in the first embodiment. It is preferred to contact a solution of lipase with the polymer carrier in the presence of a fatty acid or derivative thereof for 10 minutes to 10 hours to covalently bond the lipase to the polymer carrier.

Transesterification with lipase immobilized on a polymer containing

An immobilized lipase is prepared for transesterification of oils, fats or phospholipids in a reaction system containing a very small amount of water such as 50 to 2,000 ppm. The lipase may be a phospholipase such as phospholipase A.sub.2. In a first embodiment, lipase from a microorganism of the genus Rhizopus, Mucor, Alcaligenes or Candida is immobilized on the surface of a hydrophobic, insoluble organic polymer carrier having pores of an average diameter of 10 nm or larger. A solution of lipase is contacted with the polymer carrier for 10 minutes to 40 hours to covalently bond the lipase to the carrier. The immobilized lipase is dried under reduced pressure to a water content of 0.5 to 30 wt %. In a second embodiment, lipase is immobilized on the surface of a polymer carrier such as a hydrophobic, insoluble organic polymer carrier having a pore diameter of 5 to 1,000 nm and having a functional group capable of binding lipase in a aqueous solution and an anion-exchange group on the surface. Preferably, the functional group is an epoxy group and the anion-exchange group is a tertiary amino group. The lipase may be obtained from the same microorganism as in the first embodiment or from another lipase-producing microorganism. Immobilization can be carried out as in the first embodiment. It is preferred to contact a solution of lipase with the polymer carrier in the presence of a fatty acid or derivative thereof for 10 minutes to 10 hours to covalently bond the lipase to the polymer carrier.

Immobilization of lipase on a polymer carrier containing epoxy and

In a method of producing dialkylcarbonate, alcoholic compound and cyclo-carbonate are subjected to a catalytic reaction each other at a reaction temperature of 20.degree. to 200.degree. C. and under a pressure of 0 to 40 kg/cm.sup.2 G, which keeps the reaction system liquid, in the presence of ion exchanged zeolite which is ion-exchanged with alkali metal ion and/or alkaline earth metal ion.

Method of producing dialkylcarbonate

A high quality bisphenol A with a high purity and an excellent hue is produced from a crystalline adduct of bisphenol A and phenol by washing the adduct with specifically purified phenol, followed by decomposition of the washed adduct to separate bisphenol A. The purification is performed by a method including contacting raw material phenol with a strong-acid ion exchange resin to obtain treated phenol, and distilling the treated phenol.

Process for the production of bisphenol A

High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005 % by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

Process for the production of bishenol A

High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005% by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

The invention relates to a process for preparing prilled bisphenol A by granulation which comprises adding compounds soluble in molten bisphenol A, not affecting adversely the melt color of bisphenol A to any significant extent, and have a melting point of 60.degree. C. or more to bisphenol A and granulating and also to a process which comprises adding the reaction mother liquor or cyrstallization mother liquor produced in the manufacturing step of bisphenol A to bisphenol A or the adduct of bispheol A and phenol or a mixture of bispheol A and phenol, removing the phenol, and granulating. The processes yield prilled bispheol A which have high strength and resist powdering.

Process for preparing prilled bisphenol A

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Yokohama, Japan

Sachio Asaoka