Chiyoda Corporation

Cosmo Oil Co., Ltd.

Japan Oil, Gas and Metals National Corporation

Inpex Corporation

Jx Nippon Oil Energy Corporation

Japan Petroleum Exploration Co., Ltd.

Nippon Steel & Sumikin Engineering Co., Ltd.

Nippon Steel Corporation

Nippon Furnace Co., Ltd.

Sekiyushigen Kamatsu Kabushiki Kaisha

Tomoyuki Mikuriya

Shuhei Wakamatsu

Yasuhiro Onishi

Fuyuki Yagi

Kenichi Kawazuishi

Osamu Ikeda

Eiji Watanabe

Kazuhiko Tasaka

Nobuhiro Onda

Yasumasa Morita

Kenichi Imagawa

Susumu Mochida

Kiyoshi Inaba

Toshio Shimizu

Hironori Kawai

Osamu Iwamoto

Toshiaki Yoshioka

Yusuke Nakajima

Ryuichiro Kajiyama

Masaru Ihara

Yoshifumi Suehiro

Ryoichi Kawabata

Takeo Nikkuni

Yuhi Ozaki

Tadahiro Araake

Takenori Kanda

Ken-ichiro Fujimoto

Toshiki Furukawa

Provided is a system and a method which allow hydrogen to be produced both efficiently and in a stable manner when using exhaust gas produced by power generation as a heat source for the dehydrogenation reaction, controlling the temperature of the dehydrogenation reaction within an appropriate range. The system () for producing hydrogen comprises a dehydrogenation reaction unit () for producing hydrogen from an organic hydride by a dehydrogenation reaction in presence of a dehydrogenation catalyst; a first power generation unit () for generating electric power from energy of combustion gas produced by combustion of fuel; a waste heat recovery unit () for receiving heat from exhaust gas expelled from the first power generation unit; a heat exchanger () provided in the waste heat recovery unit for exchanging heat between the exhaust gas and a heat medium; and a circulation line (L-L) for introducing the heat medium heated in the heat exchanger to the dehydrogenation reaction unit in liquid form, and returning the heat medium expelled from the dehydrogenation reaction unit to the heat exchanger; wherein the heat medium is introduced into the dehydrogenation reaction unit at an introduction temperature ranging between 352&#xb0; C. and 392&#xb0; C., the heat medium is expelled from the dehydrogenation reaction unit at an expulsion temperature ranging between 337 &#xb0; C. and 367 &#xb0; C., and a difference between the introduction temperature and the expulsion temperature ranges between 10&#xb0; C. and 50&#xb0; C.

System and method for producing hydrogen

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.

A synthesis gas production apparatus (reformer) to be used for a synthesis gas production step in a GTL (gas-to-liquid) process is prevented from being contaminated by metal components. A method of suppressing metal contamination of a synthesis gas production apparatus operating for a GTL process that includes a synthesis gas production step of producing synthesis gas by causing natural gas and gas containing steam and/or carbon dioxide to react with each other for reforming in a synthesis gas production apparatus in which, at the time of separating and collecting a carbon dioxide contained in the synthesis gas produced in the synthesis gas production step and recycling the separated and collected carbon dioxide as source gas for the reforming reaction in the synthesis gas production step, a nickel concentration in the recycled carbon dioxide is not higher than 0.05 ppmv.

Method of suppressing metal contamination of synthesis gas production apparatus

The hydrocarbon synthesis reaction apparatus is provided with a synthesis gas supply line in which a synthesis gas is compressed and supplied by a first compressor, a reactor configured to accommodate a catalyst slurry, a gas-liquid separator configured to separate an unreacted synthesis gas and hydrocarbons discharged from the reactor into a gas and a liquid, a first recycle line in which the unreacted synthesis gas after separation into a gas and a liquid is compressed and recycled into the reactor by a second compressor, and a second recycle line configured to recycle a residual unreacted synthesis gas after separation into a gas and a liquid into the inlet side of the first compressor at the time of start-up operation when the synthesis gas is gradually increased in the amount to be introduced.

Hydrocarbon synthesis reaction apparatus, start-up process thereof, and hydrocarbon synthesis reaction system

A combustion air supply apparatusof alternating heat exchange type supplies combustion air and discharges combustion exhaust gas at a flow velocity of 80 to 200 m/sec. A burner assemblyis configured in such a manner that low-caloric fuel gas is pre-heated with heat of pre-combusting high-caloric fuel gas before the low-caloric fuel gas reaches a mixing starting space CA in the combustion chamber where the pre-combusting high-caloric fuel gas and the low-caloric fuel gas come to burn together in a full scale in the mixing starting space CA. When an air amount of the combustion air supplied through the high-temperature air supply ports of the plurality of fuel gas combustion apparatuses is defined as Qand an air amount of the pre-combustion air to be mixed with the high-caloric fuel gas, supplied from the fuel gas combustion apparatuses, is defined as Q, a total air amount (Q+Q) is 1.02 to 1.10 times more than a theoretical air amount QS required for combustion, and a ratio of Q/(Q+Q) is 0.011 to 0.047.

Reactor employing high-temperature air combustion technology

Synthesis gas for FT synthesis is produced using a producing apparatus including an active carbon adsorbing vessel for adsorbing impurities in a natural gas, a hydro-desulfurizer for hydrogenating and desulfurizing sulfur content in the natural gas under a condition of a partial pressure of hydrogen of 100 to 200 kPa, a second hydrogen supplying line for supplying hydrogen to the natural gas between the hydro-desulfurizer and a reactor, the reactor for obtaining synthesis gas by reacting the natural gas, carbon dioxide and steam in the presence of a catalyst for reforming, and a heat recovering boiler for cooling the synthesis gas at a cooling rate of 2000 to 4000&#xb0; C./second.

Process for producing synthesis gas for the fischer-tropsch synthesis and producing apparatus thereof

Growing community of inventors

Yokohama, Japan

Tomoyuki Mikuriya