JP2010043301A - Method for regenerating adsorption device in hydrogen production system - Google Patents

Method for regenerating adsorption device in hydrogen production system Download PDF

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JP2010043301A
JP2010043301A JP2008206693A JP2008206693A JP2010043301A JP 2010043301 A JP2010043301 A JP 2010043301A JP 2008206693 A JP2008206693 A JP 2008206693A JP 2008206693 A JP2008206693 A JP 2008206693A JP 2010043301 A JP2010043301 A JP 2010043301A
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hydrogen
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pressure
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JP5220511B2 (en
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Masanori Okabe
昌規 岡部
Koji Nakazawa
孝治 中沢
Kenji Taruie
憲司 樽家
Eiji Hario
栄次 針生
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Honda Motor Co Ltd
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

<P>PROBLEM TO BE SOLVED: To simply regenerate an adsorption section and adequately reduce an amount of hydrogen to be disposed. <P>SOLUTION: A method for regenerating the adsorption device in a hydrogen production system comprises the steps of: moving a high-pressure hydrogen gas in a first adsorption column 40a to a second adsorption column 40b to equalize the pressure in the inside of the first adsorption column 40a to that of the second adsorption column 40b, when regenerating the first adsorption column 40a; releasing the gas remaining in the first adsorption column 40a to a disposing section; and using the high-pressure hydrogen gas which has been moved to the second adsorption column 40b as a product gas. The high-pressure hydrogen gas that has been moved to the second adsorption column 40b is used as the product gas, which accordingly reduces the amount of hydrogen gas to be wastefully disposed. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

本発明は、水を電気分解して高圧水素を生成する水電解部と、生成された水素から水分を除去する気液分離部と、前記気液分離部から導出される前記水素に含まれる水分を吸着して除去する吸着装置とを備える水素生成システムの吸着装置再生方法に関する。   The present invention includes a water electrolysis unit that electrolyzes water to generate high-pressure hydrogen, a gas-liquid separation unit that removes moisture from the generated hydrogen, and moisture contained in the hydrogen derived from the gas-liquid separation unit The present invention relates to an adsorption device regeneration method for a hydrogen generation system including an adsorption device that adsorbs and removes water.

近年、水素を燃料として電力又は動力を供給するシステム、例えば、燃料電池システムが提案されている。燃料である水素を製造するために、水を電気分解して水素（及び酸素）を発生させる水電解装置が用いられている。   In recent years, a system for supplying electric power or power using hydrogen as a fuel, for example, a fuel cell system has been proposed. In order to produce hydrogen as a fuel, a water electrolysis apparatus that generates hydrogen (and oxygen) by electrolyzing water is used.

この水電解装置では、水分を含んだ水素が製造されており、製品ガスとして乾燥状態の水素（以下、ドライ水素ともいう）を得るためには、前記水素から水分を除去する必要がある。そこで、例えば、特許文献１に開示されている装置が知られている。   In this water electrolysis apparatus, hydrogen containing moisture is produced, and in order to obtain dry hydrogen (hereinafter also referred to as dry hydrogen) as a product gas, it is necessary to remove moisture from the hydrogen. Therefore, for example, an apparatus disclosed in Patent Document 1 is known.

この装置は、図７に示すように、純水製造手段（図示せず）により製造された純水中のガスを脱気する膜脱気モジュール１と、前記膜脱気モジュール１により脱気処理された純水を膜電解する水電解セル２と、前記水電解セル２の陽極から発生する酸素及び陰極から発生する水素を個別に除湿するモレキュラーシーブス３ａ〜３ｄとを有している。このため、水電解セル２から発生される高純度の水素及び酸素は、除湿手段であるモレキュラーシーブス３ａ、３ｂ及び３ｃ、３ｄにより除湿されている。   As shown in FIG. 7, this apparatus includes a membrane deaeration module 1 for degassing a gas in pure water produced by pure water production means (not shown), and a deaeration treatment by the membrane deaeration module 1. A water electrolysis cell 2 for membrane electrolyzing the purified water, and molecular sieves 3a to 3d for dehumidifying oxygen generated from the anode of the water electrolysis cell 2 and hydrogen generated from the cathode individually. For this reason, the high purity hydrogen and oxygen generated from the water electrolysis cell 2 are dehumidified by the molecular sieves 3a, 3b and 3c, 3d which are dehumidifying means.

特開平５−２８７５７０号公報Japanese Patent Laid-Open No. 5-287570

しかしながら、上記の特許文献１では、例えば、水素の除湿を行うために２つのモレキュラーシーブス３ａ、３ｂを備えているが、このモレキュラーシーブス３ａ、３ｂによる吸水量が所定量を超えると、前記モレキュラーシーブス３ａ、３ｂを再生させるために活性化する作業が必要となっている。   However, in the above-mentioned Patent Document 1, for example, two molecular sieves 3a and 3b are provided to perform dehumidification of hydrogen. Work to activate in order to regenerate 3a, 3b is necessary.

このため、モレキュラーシーブス３ａ、３ｂを所定の減圧下で比較的長時間にわたって加熱処理する必要がある。これにより、活性化に相当な時間がかかるとともに、この活性化を行っている間、装置全体の稼働が停止されてしまい、効率的ではないという問題がある。   For this reason, it is necessary to heat-treat the molecular sieves 3a and 3b for a relatively long time under a predetermined reduced pressure. Accordingly, there is a problem that it takes a considerable time for activation, and the operation of the entire apparatus is stopped during the activation, which is not efficient.

本発明はこの種の問題を解決するものであり、吸着部の再生処理を簡単に行うとともに、廃棄される水素量を良好に削減することが可能な水素生成システムの吸着装置再生方法を提供することを目的とする。   The present invention solves this type of problem, and provides an adsorption device regeneration method for a hydrogen generation system capable of easily reducing the amount of hydrogen to be discarded while easily performing regeneration processing of the adsorption unit. For the purpose.

本発明は、水を電気分解して高圧水素を生成する水電解部と、生成された前記高圧水素から水分を除去する気液分離部と、前記気液分離部から導出される前記高圧水素に含まれる水分を吸着して除去する吸着装置とを備えるとともに、前記吸着装置は、前記気液分離部に選択的に接続される少なくとも第１吸着部及び第２吸着部を設ける水素生成システムの吸着装置再生方法に関するものである。   The present invention includes a water electrolysis unit that electrolyzes water to generate high-pressure hydrogen, a gas-liquid separation unit that removes moisture from the generated high-pressure hydrogen, and the high-pressure hydrogen that is derived from the gas-liquid separation unit. An adsorption device that adsorbs and removes moisture contained therein, and the adsorption device adsorbs at least a first adsorption unit and a second adsorption unit that are selectively connected to the gas-liquid separation unit. The present invention relates to a device reproduction method.

この吸着装置再生方法は、第１吸着部を再生する際に、前記第１吸着部内の高圧ガスを第２吸着部に移動させ、前記第１吸着部内及び前記第２吸着部内を同圧にする工程と、前記第１吸着部内の残余のガスを、廃棄部に放出する工程と、前記第２吸着部に移動した前記高圧ガスを製品ガスとして使用する工程とを有している。   In this adsorption device regeneration method, when the first adsorption unit is regenerated, the high-pressure gas in the first adsorption unit is moved to the second adsorption unit so that the inside of the first adsorption unit and the inside of the second adsorption unit have the same pressure. A step, a step of discharging the remaining gas in the first adsorption unit to a disposal unit, and a step of using the high-pressure gas moved to the second adsorption unit as a product gas.

また、この吸着装置再生方法は、第１吸着部内及び第２吸着部内が同圧になった後、前記第２吸着部を気液分離部に接続することが好ましい。   Further, in this adsorption device regeneration method, it is preferable that the second adsorption unit is connected to the gas-liquid separation unit after the inside of the first adsorption unit and the second adsorption unit become the same pressure.

さらに、この吸着装置再生方法は、第１吸着部内及び第２吸着部内が同圧になった際の圧力が、５ＭＰａ以上であることが好ましい。   Furthermore, in this adsorption device regeneration method, it is preferable that the pressure when the inside of the first adsorption unit and the second adsorption unit become the same pressure is 5 MPa or more.

さらにまた、この吸着装置再生方法は、第１吸着部及び第２吸着部が、吸着剤として活性炭を有することが好ましい。   Furthermore, in this adsorption apparatus regeneration method, it is preferable that the first adsorption unit and the second adsorption unit have activated carbon as an adsorbent.

本発明によれば、第１吸着部の再生時に、この第１吸着部内に残存する高圧ガスが第２吸着部に移動されるため、前記第１吸着部内の全てのガスを放出することがない。従って、第２吸着部では、第１吸着部内の高圧ガスの一部（第１吸着部内及び第２吸着部内が同圧になるガス量）を、製品ガスとして利用することができ、無駄に廃棄されるガス量を良好に低減することが可能になる。これにより、簡単な制御で、経済的な再生処理が遂行されるとともに、再生に必要なエネルギの削減が容易に図られる。   According to the present invention, when the first adsorption unit is regenerated, the high-pressure gas remaining in the first adsorption unit is moved to the second adsorption unit, so that all the gas in the first adsorption unit is not released. . Therefore, in the second adsorption unit, a part of the high-pressure gas in the first adsorption unit (the amount of gas in which the first adsorption unit and the second adsorption unit have the same pressure) can be used as product gas, and is wasted. It is possible to reduce the amount of gas to be favorably reduced. As a result, economical regeneration processing is performed with simple control, and energy required for regeneration can be easily reduced.

図１は、本発明の実施形態に係る吸着装置再生方法が適用される水素生成システム１０の概略構成説明図である。   FIG. 1 is a schematic configuration explanatory diagram of a hydrogen generation system 10 to which an adsorption device regeneration method according to an embodiment of the present invention is applied.

水素生成システム１０は、純水供給装置１２を介して市水から生成された純水が供給され、この純水を電気分解することによって高圧水素を製造する水電解装置（水電解部）１４と、前記水電解装置１４から水素導出路１６に導出される前記高圧水素に含まれる水分を除去する気液分離器（気液分離部）１８と、前記気液分離器１８から水素供給路２０に供給される水素に含まれる水分を吸着して除去する吸着装置２２と、前記吸着装置２２に連通するドライ水素供給路２４に導出される前記水素（ドライ水素）、すなわち、製品ガスを貯留可能な水素タンク２６とを備える。なお、水素タンク２６は、必要に応じて備えていればよく、この水素タンク２６を削除することも可能である。   The hydrogen generation system 10 is supplied with pure water generated from city water via a pure water supply device 12, and electrolyzes the pure water to produce high-pressure hydrogen and a water electrolysis device (water electrolysis unit) 14. A gas-liquid separator (gas-liquid separator) 18 that removes water contained in the high-pressure hydrogen led out from the water electrolysis device 14 to the hydrogen lead-out path 16, and a hydrogen supply path 20 from the gas-liquid separator 18. An adsorbing device 22 that adsorbs and removes moisture contained in supplied hydrogen, and the hydrogen (dry hydrogen) led out to a dry hydrogen supply path 24 communicating with the adsorbing device 22, that is, product gas can be stored. And a hydrogen tank 26. Note that the hydrogen tank 26 may be provided as necessary, and the hydrogen tank 26 may be deleted.

水電解装置１４は、複数の水分解セル２８が積層されており、前記水分解セル２８の積層方向一端には、配管３０ａ、３０ｂ及び３０ｃが接続される。配管３０ａ、３０ｂは、純水供給装置１２に連通して純水の循環が行われる一方、配管３０ｃは、水素導出路１６を介して気液分離器１８に接続される。水素導出路１６には、高圧水素を得るためのバルブ（背圧弁）３２が配設される。気液分離器１８には、純水循環路３４の一端が接続され、前記純水循環路３４は、純水供給装置１２を介装して水電解装置１４の配管３０ａに接続される。気液分離器１８の底部には、純水循環路３４に連通するドレンバルブ３６ａ、３６ｂが設けられる。   In the water electrolysis apparatus 14, a plurality of water decomposition cells 28 are stacked, and pipes 30 a, 30 b and 30 c are connected to one end of the water decomposition cell 28 in the stacking direction. The pipes 30 a and 30 b communicate with the pure water supply device 12 to circulate pure water, while the pipe 30 c is connected to the gas-liquid separator 18 through the hydrogen lead-out path 16. The hydrogen lead-out path 16 is provided with a valve (back pressure valve) 32 for obtaining high-pressure hydrogen. One end of a pure water circulation path 34 is connected to the gas-liquid separator 18, and the pure water circulation path 34 is connected to a pipe 30 a of the water electrolysis apparatus 14 via the pure water supply device 12. Drain valves 36 a and 36 b communicating with the pure water circulation path 34 are provided at the bottom of the gas-liquid separator 18.

吸着装置２２は、水素に含まれる水蒸気（水分）を物理的吸着作用で吸着するとともに、水分を外部に放出して再生される水分吸着剤を充填した少なくとも第１吸着塔（第１吸着部）４０ａ及び第２吸着塔（第２吸着部）４０ｂを備える。水分吸着剤としては、例えば、活性炭が用いられる。   The adsorption device 22 adsorbs water vapor (moisture) contained in hydrogen by a physical adsorption action, and at least a first adsorption tower (first adsorption unit) filled with a moisture adsorbent that is regenerated by releasing moisture to the outside. 40a and a second adsorption tower (second adsorption part) 40b. As the moisture adsorbent, for example, activated carbon is used.

水素供給路２０と第１吸着塔４０ａ及び第２吸着塔４０ｂの入口側とは、水素分岐路４４ａ、４４ｂを介して接続されるとともに、前記水素分岐路４４ａ、４４ｂは、連結路４６を介して放出路４８に接続される。第１吸着塔４０ａ及び第２吸着塔４０ｂの出口側には、ドライ水素供給路２４に合流するドライ水素分岐路５０ａ、５０ｂが設けられる。   The hydrogen supply path 20 and the inlet side of the first adsorption tower 40a and the second adsorption tower 40b are connected via hydrogen branch paths 44a and 44b, and the hydrogen branch paths 44a and 44b are connected via a connection path 46. And connected to the discharge path 48. Dry hydrogen branch paths 50a and 50b that join the dry hydrogen supply path 24 are provided on the outlet side of the first adsorption tower 40a and the second adsorption tower 40b.

水素分岐路４４ａ、４４ｂには、バルブ５２ａ、５２ｂが配設される一方、連結路４６には、バルブ５２ｃ、５２ｄが配設される。放出路４８には、バルブ５２ｅが配設される。ドライ水素分岐路５０ａ、５０ｂには、バルブ５４ａ、５４ｂが配設されるとともに、ドライ水素供給路２４には、バルブ５４ｃが配設される。   Valves 52a and 52b are disposed in the hydrogen branch paths 44a and 44b, while valves 52c and 52d are disposed in the connection path 46. A valve 52 e is disposed in the discharge path 48. Valves 54 a and 54 b are disposed in the dry hydrogen branch paths 50 a and 50 b, and a valve 54 c is disposed in the dry hydrogen supply path 24.

水素タンク２６には、燃料供給路５６がバルブ５８を介して接続される。この燃料供給路５６は、燃料電池車両６０の燃料タンクに直接、あるいは、図示しない貯留タンクを介して接続可能である。   A fuel supply path 56 is connected to the hydrogen tank 26 via a valve 58. The fuel supply path 56 can be connected to the fuel tank of the fuel cell vehicle 60 directly or via a storage tank (not shown).

このように構成される水素生成システム１０の動作について、以下に説明する。   The operation of the hydrogen generation system 10 configured as described above will be described below.

先ず、純水供給装置１２では、純水循環路３４に純水が導出されており、この純水は、配管３０ａから水電解装置１４内に供給される。水電解装置１４では、各水分解セル２８により水が電気により分解されて水素が得られるとともに、バルブ３２を介して高圧水素（１ＭＰａ〜６０ＭＰａ）が得られる。この高圧水素は、配管３０ｃを介して水電解装置１４の外部に取り出し可能となる。一方、反応により生成した酸素と、使用済みの水とは、配管３０ｂを介して純水供給装置１２に戻される。   First, in the pure water supply device 12, pure water is led to the pure water circulation path 34, and this pure water is supplied into the water electrolysis device 14 from the pipe 30a. In the water electrolysis apparatus 14, water is decomposed by electricity in each water splitting cell 28 to obtain hydrogen, and high pressure hydrogen (1 MPa to 60 MPa) is obtained via the valve 32. This high-pressure hydrogen can be taken out of the water electrolysis apparatus 14 through the pipe 30c. On the other hand, the oxygen produced by the reaction and the used water are returned to the pure water supply device 12 via the pipe 30b.

図２に示すように、水電解装置１４で生成された水蒸気を含む比較的高圧の水素は、水素導出路１６を介して気液分離器１８に送られる。この気液分離器１８では、水素に含まれる水蒸気が、この水素から分離されて純水循環路３４に戻される一方、前記水素は、水素供給路２０に供給される。   As shown in FIG. 2, relatively high-pressure hydrogen containing water vapor generated by the water electrolysis device 14 is sent to the gas-liquid separator 18 via the hydrogen lead-out path 16. In the gas-liquid separator 18, water vapor contained in hydrogen is separated from the hydrogen and returned to the pure water circulation path 34, while the hydrogen is supplied to the hydrogen supply path 20.

水素供給路２０に供給された水素は、吸着装置２２に送られる。吸着装置２２では、例えば、バルブ５２ａ、５４ａが開放されるとともに、バルブ５２ｂ〜５２ｅ及び５４ｂが閉塞されることにより、第１吸着塔４０ａに水素が導入される。この第１吸着塔４０ａ内では、水素に含まれる水蒸気が吸着されて乾燥状態の水素（ドライ水素）が得られ、このドライ水素がドライ水素分岐路５０ａからドライ水素供給路２４に導出される。ドライ水素は、例えば、圧力が３５ＭＰａで且つ露点が−５０℃である。   The hydrogen supplied to the hydrogen supply path 20 is sent to the adsorption device 22. In the adsorption device 22, for example, the valves 52a and 54a are opened, and the valves 52b to 52e and 54b are closed, whereby hydrogen is introduced into the first adsorption tower 40a. In the first adsorption tower 40a, water vapor contained in hydrogen is adsorbed to obtain dry hydrogen (dry hydrogen), and this dry hydrogen is led out from the dry hydrogen branch path 50a to the dry hydrogen supply path 24. For example, dry hydrogen has a pressure of 35 MPa and a dew point of −50 ° C.

ドライ水素供給路２４に導出されたドライ水素は、水素タンク２６に貯蔵される。この水素タンク２６に貯蔵されたドライ水素は、必要に応じてバルブ５８の開放作用下に、製品ガスとして燃料供給路５６を介して燃料電池車両６０に充填される。   The dry hydrogen led out to the dry hydrogen supply path 24 is stored in the hydrogen tank 26. The dry hydrogen stored in the hydrogen tank 26 is filled into the fuel cell vehicle 60 as a product gas through the fuel supply path 56 under the opening action of the valve 58 as necessary.

次いで、第１吸着塔４０ａが限界吸着量に達すると、水電解装置１４による純水の電気分解処理が一旦停止されるとともに、本発明に係る吸着装置再生方法が行われる。   Next, when the first adsorption tower 40a reaches the limit adsorption amount, the electrolysis process of pure water by the water electrolysis device 14 is temporarily stopped and the adsorption device regeneration method according to the present invention is performed.

先ず、図３に示すように、バルブ５２ａ、５４ａが閉塞される一方、バルブ５２ｃ、５２ｄが開放される。ここで、第１吸着塔４０ａ内は、高圧水素ガスによって、例えば、３５ＭＰａに昇圧されるとともに、第２吸着塔４０ｂ内は、大気圧に維持されている。従って、バルブ５２ｃ、５２ｄが開放されることにより、第１吸着塔４０ａ内の水素ガス（高圧ガス）は、連結路４６を通って第２吸着塔４０ｂ内に移動する。   First, as shown in FIG. 3, the valves 52a and 54a are closed, while the valves 52c and 52d are opened. Here, the inside of the first adsorption tower 40a is pressurized to, for example, 35 MPa by high-pressure hydrogen gas, and the inside of the second adsorption tower 40b is maintained at atmospheric pressure. Accordingly, when the valves 52c and 52d are opened, the hydrogen gas (high-pressure gas) in the first adsorption tower 40a moves into the second adsorption tower 40b through the connection path 46.

このため、第１吸着塔４０ａ内の水素ガスが所定量、例えば、半分の量だけ第２吸着塔４０ｂに移動されて、前記第１吸着塔４０ａ内の圧力と前記第２吸着塔４０ｂ内の圧力とが均等化される。これにより、第１吸着塔４０ａ内及び第２吸着塔４０ｂ内には、それぞれ約１７ＭＰａの水素ガスが充填されている。従って、第１吸着塔４０ａ内が減圧される一方、第２吸着塔４０ｂ内が昇圧されている。   Therefore, the hydrogen gas in the first adsorption tower 40a is moved to the second adsorption tower 40b by a predetermined amount, for example, half the amount, and the pressure in the first adsorption tower 40a and the second adsorption tower 40b The pressure is equalized. As a result, the first adsorption tower 40a and the second adsorption tower 40b are each filled with about 17 MPa of hydrogen gas. Accordingly, the pressure in the first adsorption tower 40a is reduced, while the pressure in the second adsorption tower 40b is increased.

その後、図４に示すように、バルブ５２ｄが閉塞されるとともに、バルブ５２ｂが開放されることにより、第２吸着塔４０ｂで精製作業が開始される。一方、バルブ５２ｅが開放されることにより、第１吸着塔４０ａ内に残存するガス（水素ガス及び水分）は、放出路４８から廃棄部、例えば、外部に放出される。これにより、第１吸着塔４０ａ内からガス及び水分が放出され、前記第１吸着塔４０ａ内が大気圧に降圧した時点で、バルブ５２ｃ、５２ｅが閉塞される（図５参照）。   Thereafter, as shown in FIG. 4, the valve 52d is closed and the valve 52b is opened, so that the purification operation is started in the second adsorption tower 40b. On the other hand, when the valve 52e is opened, the gas (hydrogen gas and moisture) remaining in the first adsorption tower 40a is discharged from the discharge path 48 to a waste part, for example, the outside. As a result, gas and moisture are released from the first adsorption tower 40a, and the valves 52c and 52e are closed when the pressure in the first adsorption tower 40a is reduced to atmospheric pressure (see FIG. 5).

第２吸着塔４０ｂでは、水素に含まれる水蒸気が吸着されて乾燥状態の水素（ドライ水素）が得られ、バルブ５４ｂの開放作用下に、このドライ水素がドライ水素分岐路５０ｂからドライ水素供給路２４に導出される。   In the second adsorption tower 40b, water vapor contained in hydrogen is adsorbed to obtain dry hydrogen (dry hydrogen), and the dry hydrogen is supplied from the dry hydrogen branch 50b to the dry hydrogen supply channel under the opening action of the valve 54b. 24.

この場合、本実施形態では、第１吸着塔４０ａの再生時に、この第１吸着塔４０ａ内に残存する高圧水素ガスが所定量、例えば、半分の量だけ第２吸着塔４０ｂに移動された後、前記第１吸着塔４０ａの再生処理が開始されている。このため、例えば、第１吸着塔４０ａに充填されている３５ＭＰａの水素ガスを再生のために全て排出する場合に比べ、この第１吸着塔４０ａ内に残存する水素ガスが増える。従って、第１吸着塔４０ａから排出される水素分のエネルギロスを有効に削減することができる。   In this case, in the present embodiment, after regeneration of the first adsorption tower 40a, the high-pressure hydrogen gas remaining in the first adsorption tower 40a is moved to the second adsorption tower 40b by a predetermined amount, for example, half the amount. The regeneration process of the first adsorption tower 40a is started. For this reason, for example, hydrogen gas remaining in the first adsorption tower 40a is increased as compared with the case where all of the 35 MPa hydrogen gas filled in the first adsorption tower 40a is discharged for regeneration. Therefore, it is possible to effectively reduce the energy loss of the hydrogen discharged from the first adsorption tower 40a.

しかも、第２吸着塔４０ｂには、第１吸着塔４０ａから水素ガスが供給されており、この第２吸着塔４０ｂ内が昇圧されている。これにより、第２吸着塔４０ｂを所望の圧力、例えば、３５ＭＰａに昇圧するためにかかる時間が一挙に短縮され、ドライ水素を迅速に送り出すことが可能になる。   Moreover, hydrogen gas is supplied from the first adsorption tower 40a to the second adsorption tower 40b, and the pressure in the second adsorption tower 40b is increased. As a result, the time taken to increase the pressure of the second adsorption tower 40b to a desired pressure, for example, 35 MPa, is shortened all at once, and dry hydrogen can be sent out quickly.

さらに、第２吸着塔４０ｂでは、第１吸着塔４０ａから移動された水素ガスを、製品ガスとして水素タンク２６に供給することができる。このため、無駄に廃棄される水素ガスを良好に低減することが可能になり、経済的であるという効果が得られる。   Furthermore, in the second adsorption tower 40b, the hydrogen gas moved from the first adsorption tower 40a can be supplied to the hydrogen tank 26 as a product gas. For this reason, it is possible to satisfactorily reduce the hydrogen gas that is wasted and is economical.

特に、本実施形態では、第１吸着塔４０ａ内に残存する高圧水素ガスが、半分の量だけ第２吸着塔４０ｂに移動された後、前記第１吸着塔４０ａ内及び前記第２吸着塔４０ｂ内の圧力は、５ＭＰａ以上に維持されている。   In particular, in the present embodiment, after the high-pressure hydrogen gas remaining in the first adsorption tower 40a is moved to the second adsorption tower 40b by a half amount, the inside of the first adsorption tower 40a and the second adsorption tower 40b. The internal pressure is maintained at 5 MPa or more.

ここで、高圧ガス中の水分濃度は、図６に示すように、前記高圧ガスの圧力が５ＭＰａ以上の圧力において、著しく減少している。従って、第１吸着塔４０ａから第２吸着塔４０ｂに移動する水分量が非常に少なくなり、前記第１吸着塔４０ａから前記第２吸着塔４０ｂに移動した水素ガスを、ドライ水素として有効且つ経済的に利用することができるという利点がある。   Here, as shown in FIG. 6, the moisture concentration in the high-pressure gas is significantly reduced when the pressure of the high-pressure gas is 5 MPa or more. Therefore, the amount of moisture moving from the first adsorption tower 40a to the second adsorption tower 40b is very small, and the hydrogen gas moved from the first adsorption tower 40a to the second adsorption tower 40b is effective and economical as dry hydrogen. There is an advantage that it can be utilized.

さらにまた、第１吸着塔４０ａは、水分吸着剤として活性炭を用いている。このため、例えば、モレキュラーシーブスに比較して水の吸着力が弱く、大気圧までのガス放出を行うだけで、第１吸着塔４０ａの再生処理が十分に行われる。この場合、高圧水素ガスは、飽和水分量が著しく少ないため、製品ガスに近似した状態で、外部に放出されてしまう。これにより、第１吸着塔４０ａから第２吸着塔４０ｂに移動した高圧水素は、製品ガスとして有効に利用することが可能になり、廃棄される水素ガス量を半減させることができる。   Furthermore, the first adsorption tower 40a uses activated carbon as a moisture adsorbent. For this reason, for example, the adsorption | suction ability of water is weak compared with a molecular sieve, and the reproduction | regeneration process of the 1st adsorption tower 40a is fully performed only by discharging | emitting gas to atmospheric pressure. In this case, the high-pressure hydrogen gas has an extremely small saturated water content, and thus is released to the outside in a state similar to the product gas. Thereby, the high-pressure hydrogen moved from the first adsorption tower 40a to the second adsorption tower 40b can be effectively used as the product gas, and the amount of discarded hydrogen gas can be halved.

なお、第２吸着塔４０ｂの再生処理は、上記の第１吸着塔４０ａの再生処理と同様であり、この説明は省略する。   The regeneration process of the second adsorption tower 40b is the same as the regeneration process of the first adsorption tower 40a, and the description thereof is omitted.

また、本実施形態では、吸着装置２２は、第１吸着塔４０ａ及び第２吸着塔４０ｂの２基の吸着塔を備えているが、これに限定されるものではなく、例えば、３以上の吸着塔を並列して構成してもよい。   Moreover, in this embodiment, although the adsorption | suction apparatus 22 is equipped with two adsorption towers, the 1st adsorption tower 40a and the 2nd adsorption tower 40b, it is not limited to this, For example, 3 or more adsorption | suction The towers may be configured in parallel.

本発明の実施形態に係る吸着装置再生方法が適用される水素生成システムの概略構成説明図である。1 is a schematic configuration explanatory diagram of a hydrogen generation system to which an adsorption device regeneration method according to an embodiment of the present invention is applied. 前記水素生成システムの動作説明図である。It is operation | movement explanatory drawing of the said hydrogen generation system. 前記水素生成システムの動作説明図である。It is operation | movement explanatory drawing of the said hydrogen generation system. 前記水素生成システムの動作説明図である。It is operation | movement explanatory drawing of the said hydrogen generation system. 前記水素生成システムの動作説明図である。It is operation | movement explanatory drawing of the said hydrogen generation system. ガス圧力と飽和水分濃度との関係説明図である。It is an explanatory view of the relationship between gas pressure and saturated water concentration. 特許文献１に開示されている装置の説明図である。It is explanatory drawing of the apparatus currently disclosed by patent document 1. FIG.

符号の説明Explanation of symbols

１０…水素生成システム １２…純水供給装置
１４…水電解装置 １６…水素導出路
１８…気液分離器 ２０…水素供給路
２２…吸着装置
３２、５２ａ〜５２ｅ、５４ａ〜５４ｃ、５８…バルブ
４０ａ、４０ｂ…吸着塔 ４４ａ、４４ｂ…水素分岐路
４６…連結路 ４８…放出路
５０ａ、５０ｂ…ドライ水素分岐路 ６０…燃料電池車両 DESCRIPTION OF SYMBOLS 10 ... Hydrogen production system 12 ... Pure water supply apparatus 14 ... Water electrolysis apparatus 16 ... Hydrogen lead-out path 18 ... Gas-liquid separator 20 ... Hydrogen supply path 22 ... Adsorption apparatus 32, 52a-52e, 54a-54c, 58 ... Valve 40a , 40b ... Adsorption towers 44a, 44b ... Hydrogen branch path 46 ... Connection path 48 ... Release path 50a, 50b ... Dry hydrogen branch path 60 ... Fuel cell vehicle

Claims (4)

水を電気分解して高圧水素を生成する水電解部と、生成された前記高圧水素から水分を除去する気液分離部と、前記気液分離部から導出される前記高圧水素に含まれる水分を吸着して除去する吸着装置とを備えるとともに、前記吸着装置は、前記気液分離部に選択的に接続される少なくとも第１吸着部及び第２吸着部を設ける水素生成システムの吸着装置再生方法であって、
前記第１吸着部を再生する際に、前記第１吸着部内の高圧ガスを前記第２吸着部に移動させ、前記第１吸着部内及び前記第２吸着部内を同圧にする工程と、
前記第１吸着部内の残余のガスを、廃棄部に放出する工程と、
前記第２吸着部に移動した前記高圧ガスを製品ガスとして使用する工程と、
を有することを特徴とする水素生成システムの吸着装置再生方法。 A water electrolysis unit that electrolyzes water to generate high-pressure hydrogen, a gas-liquid separation unit that removes moisture from the generated high-pressure hydrogen, and water contained in the high-pressure hydrogen derived from the gas-liquid separation unit An adsorption device that adsorbs and removes the adsorption device, and the adsorption device is an adsorption device regeneration method for a hydrogen generation system that includes at least a first adsorption unit and a second adsorption unit that are selectively connected to the gas-liquid separation unit. There,
When regenerating the first adsorbing unit, moving the high-pressure gas in the first adsorbing unit to the second adsorbing unit, and the same pressure in the first adsorbing unit and the second adsorbing unit;
Discharging the remaining gas in the first adsorption section to a disposal section;
Using the high-pressure gas moved to the second adsorption section as a product gas;
A method for regenerating an adsorption device for a hydrogen generation system, comprising: 請求項１記載の吸着装置再生方法において、前記第１吸着部内及び前記第２吸着部内が同圧になった後、前記第２吸着部を前記気液分離部に接続することを特徴とする水素生成システムの吸着装置再生方法。   2. The adsorption apparatus regeneration method according to claim 1, wherein the second adsorption unit is connected to the gas-liquid separation unit after the inside of the first adsorption unit and the second adsorption unit become the same pressure. Method for regenerating adsorption device of production system. 請求項１又は２記載の吸着装置再生方法において、前記第１吸着部内及び前記第２吸着部内が同圧になった際の圧力は、５ＭＰａ以上であることを特徴とする水素生成システムの吸着装置再生方法。   3. The adsorption apparatus for a hydrogen generation system according to claim 1, wherein the pressure when the pressure in the first adsorption section and the second adsorption section is the same is 5 MPa or more. Playback method. 請求項１〜３のいずれか１項に記載の吸着装置再生方法において、前記第１吸着部及び前記第２吸着部は、吸着剤として活性炭を有することを特徴とする水素生成システムの吸着装置再生方法。   The adsorption device regeneration method according to any one of claims 1 to 3, wherein the first adsorption unit and the second adsorption unit have activated carbon as an adsorbent. Method.
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JP2013023733A (en) * 2011-07-21 2013-02-04 Honda Motor Co Ltd Method for operating water electrolysis system
WO2014002988A1 (en) 2012-06-25 2014-01-03 日産自動車株式会社 Water electrolysis system

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Publication number Priority date Publication date Assignee Title
JP2008144254A (en) * 2006-12-13 2008-06-26 Honda Motor Co Ltd Hydrogen producing system and method of regenerating adsorption apparatus thereof

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JP2008144254A (en) * 2006-12-13 2008-06-26 Honda Motor Co Ltd Hydrogen producing system and method of regenerating adsorption apparatus thereof

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012096165A (en) * 2010-11-02 2012-05-24 Shinwa Controls Co Ltd Low dew-point air generator
JP2013023733A (en) * 2011-07-21 2013-02-04 Honda Motor Co Ltd Method for operating water electrolysis system
WO2014002988A1 (en) 2012-06-25 2014-01-03 日産自動車株式会社 Water electrolysis system
CN104428450A (en) * 2012-06-25 2015-03-18 日产自动车株式会社 Water electrolysis system
US9435040B2 (en) 2012-06-25 2016-09-06 Nissan Motor Co., Ltd. Water electrolysis system
CN104428450B (en) * 2012-06-25 2017-05-24 日产自动车株式会社 Water electrolysis system

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