JPH0747131B2 - How to recover performance of water electrolyzer - Google Patents
How to recover performance of water electrolyzerInfo
- Publication number
- JPH0747131B2 JPH0747131B2 JP4266743A JP26674392A JPH0747131B2 JP H0747131 B2 JPH0747131 B2 JP H0747131B2 JP 4266743 A JP4266743 A JP 4266743A JP 26674392 A JP26674392 A JP 26674392A JP H0747131 B2 JPH0747131 B2 JP H0747131B2
- Authority
- JP
- Japan
- Prior art keywords
- exchange membrane
- water electrolysis
- performance
- cation exchange
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 40
- 238000005868 electrolysis reaction Methods 0.000 claims description 44
- 238000005341 cation exchange Methods 0.000 claims description 27
- 239000012528 membrane Substances 0.000 claims description 27
- 239000012535 impurity Substances 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 7
- 230000000717 retained effect Effects 0.000 claims 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000011575 calcium Substances 0.000 description 6
- 239000011777 magnesium Substances 0.000 description 6
- 229910000000 metal hydroxide Inorganic materials 0.000 description 6
- 150000004692 metal hydroxides Chemical class 0.000 description 6
- 229910021645 metal ion Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000004140 cleaning Methods 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 239000003014 ion exchange membrane Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 239000002800 charge carrier Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000007772 electroless plating Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 125000000542 sulfonic acid group Chemical group 0.000 description 1
- TXEYQDLBPFQVAA-UHFFFAOYSA-N tetrafluoromethane Chemical compound FC(F)(F)F TXEYQDLBPFQVAA-UHFFFAOYSA-N 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、電解質である陽イオン
交換膜の両面に陽極と陰極とを接合させた水電解槽の性
能が水の汚染等で劣化した際、定格以上の電解電流で電
解することにより陽イオン交換膜に滞留した金属イオン
や金属イオン化合物等を陰極側へ排出することによって
水電解槽の性能を回復させる効果的な方法を提案するも
のである。BACKGROUND OF THE INVENTION The present invention relates to a cation exchange membrane, which is an electrolyte, having a positive electrode and a negative electrode bonded to both sides of the electrolyte. It proposes an effective method for recovering the performance of a water electrolysis cell by discharging metal ions, metal ion compounds, etc. accumulated in a cation exchange membrane by electrolysis to the cathode side.
【０００２】[0002]
【従来の技術】陽イオン交換膜水電解法とは、陽イオン
交換膜の両面に白金族金属からなる陽極と陰極とが接合
された触媒電極接合体を有する水電解槽の陽極側に水を
供給し、両極間に電圧をかけて、陽極より酸素を、陰極
より水素を得る方法である。2. Description of the Related Art The cation exchange membrane water electrolysis method is a method of supplying water to the anode side of a water electrolysis cell having a catalyst electrode assembly in which an anode and a cathode made of a platinum group metal are joined to both sides of a cation exchange membrane. Then, a voltage is applied between both electrodes to obtain oxygen from the anode and hydrogen from the cathode.
【０００３】この場合、水電解槽内では、下記の反応に
より、陽極から酸素［Ｏ2 ］が発生し、同時に生成した
プロトン［Ｈ+ ］はイオン交換膜中を通って陰極に向か
い、電子を得て水素［Ｈ2 ］となる。 陽極 ２Ｈ2 Ｏ→Ｏ2 ＋４Ｈ+ ＋４ｅ 陰極 ４Ｈ+ ＋４ｅ→２Ｈ2 In this case, in the water electrolysis tank, oxygen [O 2 ] is generated from the anode due to the following reaction, and the proton [H + ] simultaneously generated passes through the ion exchange membrane toward the cathode to generate electrons. It becomes hydrogen [H 2 ]. Anode 2H 2 O → O 2 + 4H + + 4e Cathode 4H + + 4e → 2H 2
【０００４】ここにイオン交換膜にカルシュウムイオン
［Ｃａ2+］、マグネシュウムイオン［Ｍｇ2+］などの金
属イオンが混入すると、それら金属イオンが一部プロト
ンに代わり電荷のキャリアとして働くため、下記の反応
により、陰極側の膜面あるいは膜内部に水酸化カルシュ
ウム［Ｃａ（ＯＨ）2 ］，水酸化マグネシュウム［Ｍｇ
（ＯＨ）2 ］などの金属水酸化物が析出する。 陽極 ２Ｈ2 Ｏ→Ｏ2 ＋４Ｈ+ ＋４ｅ 陰極 ４Ｈ2 Ｏ＋２Ｃａ2+→２Ｃａ（ＯＨ）2 ＋４Ｈ+ ４Ｈ+ ＋４ｅ→２Ｈ2 When metal ions such as calcium ions [Ca 2+ ] and magnesium ions [Mg 2+ ] are mixed in the ion exchange membrane, some of these metal ions act as charge carriers instead of protons. Depending on the reaction, calcium hydroxide [Ca (OH) 2 ], magnesium hydroxide [Mg]
A metal hydroxide such as (OH) 2 ] is deposited. Anode 2H 2 O → O 2 + 4H + + 4e Cathode 4H 2 O + 2Ca 2+ → 2Ca (OH) 2 + 4H + 4H + + 4e → 2H 2
【０００５】これら金属水酸化物が多量にイオン交換膜
中に析出すると、プロトンの動きが悪くなり濃度分極が
生じ水電解電圧の上昇によるエネルギー効率の低下や、
陽イオン交換膜の破損に伴う電流効率の低下、またはガ
ス濃度の低下等の性能の劣化等が生じる。When a large amount of these metal hydroxides are deposited in the ion exchange membrane, the movement of protons becomes poor and concentration polarization occurs, resulting in a decrease in energy efficiency due to an increase in water electrolysis voltage.
Due to the damage of the cation exchange membrane, the current efficiency is reduced, or the performance is deteriorated such as the gas concentration is reduced.
【０００６】そこで従来は、水電解槽内部を塩酸［ＨＣ
ｌ］により洗浄することによって、Ｃａ（ＯＨ）2 、Ｍ
ｇ（ＯＨ）2 などの金属水酸化物やＣａ2+、Ｍｇ2+など
の金属イオンを系外に溶出し、性能の回復を図ってい
た。Therefore, conventionally, hydrochloric acid [HC
l] to wash Ca (OH) 2 , M
Metal hydroxides such as g (OH) 2 and metal ions such as Ca 2+ and Mg 2+ were eluted out of the system to recover the performance.
【０００７】[0007]
【発明が解決しようとす課題】ところが、塩酸により水
電解槽内部を洗浄するという従来の方法には、実用に当
たっては水電解槽に塩酸洗浄用の経路および洗浄後の廃
液の排出経路を設ける必要があり、水電解槽の構造が大
変複雑になるという問題がある。また、塩酸洗浄後の廃
液の排出が不十分だと、水電解による酸素ガスとともに
残留塩酸の分解による塩素ガスも発生し、酸素濃度の低
下はもちろんのこと、電解によって生成される酸素の使
用目的によっては危険を伴うことさえある。さらに、塩
酸廃液は強酸でありその処理にも相当の注意が必要とな
るなど、多くの問題がある。However, in the conventional method of cleaning the inside of the water electrolysis tank with hydrochloric acid, in practical use, it is necessary to provide the water electrolysis tank with a path for cleaning hydrochloric acid and a path for discharging the waste liquid after cleaning. However, there is a problem that the structure of the water electrolyzer becomes very complicated. In addition, if the discharge of the waste liquid after cleaning with hydrochloric acid is insufficient, chlorine gas is generated due to the decomposition of residual hydrochloric acid together with oxygen gas due to water electrolysis, which not only lowers the oxygen concentration but also the purpose of use of oxygen generated by electrolysis. It can even be dangerous in some cases. Further, the hydrochloric acid waste liquid is a strong acid and requires considerable care in its treatment.
【０００８】本発明はこのような課題を解決するために
なされたものであり、その目的とするところは、塩酸を
使用せず、安全で、かつ容易に陽イオン交換膜水電解槽
の電解性能を回復させる方法を提供することである。The present invention has been made to solve the above problems, and an object of the present invention is to use a hydrochloric acid-free, safe and easy electrolytic performance of a cation-exchange membrane water electrolysis cell. Is to provide a way to recover.
【０００９】[0009]
【課題を解決しようとするための手段】そこで、陽イオ
ン交換膜に不純物が滞留して電解性能が劣化した陽イオ
ン交換膜水電解槽を、定格以上の電解電流で電解して陽
イオン交換膜から不純物を除去するすることにより電解
性能を回復させることを特徴とする水電解槽の性能回復
方法により、前記課題を解決するものである。[Problems to be Solved by the Invention] Then, a cation-exchange membrane water electrolysis tank in which impurities are accumulated in the cation-exchange membrane and electrolysis performance is deteriorated is electrolyzed with an electrolysis current higher than the rated value. The above problem is solved by a method for recovering the performance of a water electrolysis cell, which is characterized in that the electrolytic performance is recovered by removing impurities from the solution.
【００１０】[0010]
【作用】陽イオン交換膜水電解法では、陽極で酸素と同
時に生成されたプロトンが、陽イオン交換膜を通って陰
極に移動する際、プロトン１個当り６〜７分子の水を伴
って移動する。そこで、水電解槽の性能が水の汚染等に
よって劣化した際、水電解槽を定格以上の電解電流によ
り水電解すると、このプロトンの移動が通常より激しく
なり、それに伴いなう水の移動量も多くなる。そのた
め、陽イオン交換膜内部のＣａ（ＯＨ）2 ，Ｍｇ（Ｏ
Ｈ）2 などの金属水酸化物は、その水に除々に溶解し陰
極側へ排出される。また陽イオン交換膜内部のＣａ2+，
Ｍｇ2+などの金属イオンもプロトン同様一部電荷の移動
に関与しており、電解電流が定格以上になることでその
関与の度合いが急激に高くなるため、これら金属イオン
は陰極でＣａ（ＯＨ）2 ，Ｍｇ（ＯＨ）2 などの金属水
酸化物としてやはり陰極側へ排出される。その陰極の水
を系外へ排出するか、またはイオン交換器を通して脱イ
オンすれば、水電解槽内部の不純物を取り除き、電解性
能を回復させることができる。尚、定格電流とは、長時
間連続使用する際、流すことの出来る最大電流を意味し
ている。In the cation-exchange membrane water electrolysis method, when the protons produced simultaneously with oxygen at the anode move to the cathode through the cation-exchange membrane, they move with 6 to 7 molecules of water per proton. . Therefore, when the performance of the water electrolysis cell deteriorates due to water pollution, etc., if the water electrolysis is performed in the water electrolysis cell with an electrolysis current higher than the rated value, the movement of these protons becomes stronger than usual, and the amount of water movement accompanying it also increases. Will increase. Therefore, Ca (OH) 2 , Mg (O) inside the cation exchange membrane
H) 2 and other metal hydroxides gradually dissolve in the water and are discharged to the cathode side. In addition, Ca 2+ inside the cation exchange membrane,
Similar to protons, metal ions such as Mg 2+ are also involved in the transfer of some electric charges, and the degree of involvement increases sharply when the electrolytic current exceeds the rated value. ) 2 , Mg (OH) 2 and other metal hydroxides are also discharged to the cathode side. If the water of the cathode is discharged to the outside of the system or deionized through an ion exchanger, impurities inside the water electrolysis tank can be removed and the electrolytic performance can be restored. The rated current means the maximum current that can be flowed during continuous use for a long time.
【００１１】プロトンの移動に伴って移動する水の量は
通電電気量に比例するため、定格電流を長時間流す方法
もあるが、これによると再生に時間がかかることや金属
水酸化物の除去効率が悪い等の問題がある。従って、本
発明のように、定格電流以上で電解するのがより効果的
である。Since the amount of water that moves with the movement of protons is proportional to the amount of electricity supplied, there is also a method in which a rated current is passed for a long time, but this method takes time for regeneration and removal of metal hydroxide. There are problems such as inefficiency. Therefore, it is more effective to electrolyze at a rated current or more as in the present invention.
【００１２】[0012]
【実施例】本発明を実施例により説明する。図１は、陽
イオン交換膜を電解質とし、その両面に陽極と陰極とを
接合させた水電解槽の概要図である。１は陽イオン交換
膜、２は正極、３は負極である。陽イオン交換膜１はパ
ーフロロカーボンをベースにしスルホン酸基が導入され
たものである。この陽イオン交換膜の両面に、無電解メ
ッキ法により、触媒電極としての白金２ｍｇ／ｃｍ2 が
接合されている。また、集電体として、白金メッキした
チタンのエキスパンドメタルが触媒電極に圧接されてい
る。このような水電解槽の構造自体は周知のものであ
り、本発明の要旨とは無関係であるので、詳細な説明を
省略する。EXAMPLES The present invention will be described with reference to examples. FIG. 1 is a schematic diagram of a water electrolysis cell in which a cation exchange membrane is used as an electrolyte and an anode and a cathode are joined to both surfaces thereof. 1 is a cation exchange membrane, 2 is a positive electrode, and 3 is a negative electrode. The cation exchange membrane 1 is based on perfluorocarbon and has sulfonic acid groups introduced therein. Platinum 2 mg / cm 2 as a catalyst electrode is bonded to both surfaces of this cation exchange membrane by electroless plating. Further, an expanded metal of platinum-plated titanium is pressed against the catalyst electrode as a current collector. The structure itself of such a water electrolysis cell is well known and has nothing to do with the gist of the present invention, and thus detailed description thereof will be omitted.
【００１３】この水電解槽の陽イオン交換膜にイオン交
換容量の５０％のＣａを含ませた場合の電圧−電流特性
を図２（Ａ）に示す。ここで比較のため、正常な水電解
槽の電流−電圧特性（Ｄ）を合せて示す。同図に示され
るように、（Ａ）は水電解電圧が相当高くなっており、
正常品（Ｄ）に比べてエネルギー効率が低下しているの
が分かる。FIG. 2 (A) shows the voltage-current characteristics when the cation exchange membrane of this water electrolysis cell contains 50% of the ion exchange capacity of Ca. For comparison, the current-voltage characteristics (D) of a normal water electrolysis cell are also shown here. As shown in the figure, in (A), the water electrolysis voltage is considerably high,
It can be seen that the energy efficiency is lower than that of the normal product (D).
【００１４】この水電解槽を、電解電流を変えて性能の
回復を試みた。定格電解電流密度０．７Ａ／ｃｍ
2 （Ｂ）と定格以上の電解電流密度である１．０Ａ／ｃ
ｍ2 （Ｃ）とで、それぞれ４時間、陰極より生ずる水を
系外に排出しながら、電解した後の電解−電流特性を図
２中の（Ｂ）、（Ｃ）で示す。定格電解電流密度以上
（１．０Ａ／ｃｍ2 ）にて性能の回復を試みた場合
（Ｃ）は、全電解電流密度において正常品と同程度まで
回復しているのが分かる。しかし定格電解電流密度によ
る場合（Ｂ）は、完全に回復させるまでには至らなかっ
た。これより、定格以上の電解電流で電解して陽イオン
交換膜から不純物を除去することにより、不純物の混入
により性能が劣化した水電解槽の性能が良好に回復され
ることが分かる。An attempt was made to recover the performance of this water electrolysis cell by changing the electrolysis current. Rated electrolysis current density 0.7A / cm
2 (B) and 1.0A / c, which is the electrolytic current density above the rating
m 2 (C) and electrolysis-current characteristics after electrolysis while discharging water generated from the cathode to the outside of the system for 4 hours are shown by (B) and (C) in FIG. 2. It can be seen that when the recovery of the performance is attempted at the rated electrolytic current density or more (1.0 A / cm 2 ) (C), the total electrolytic current density is recovered to the same level as the normal product. However, in the case of the rated electrolytic current density (B), it was not possible to completely recover it. From this, it can be seen that the performance of the water electrolysis cell in which the performance has deteriorated due to the mixing of impurities is favorably restored by electrolyzing with an electrolysis current of the rated value or more to remove the impurities from the cation exchange membrane.
【００１５】[0015]
【発明の効果】本発明にかかる水電解槽の性能回復方法
は、陽イオン交換膜に不純物が滞留して電解性能が劣化
した陽イオン交換膜水電解槽を、定格以上の電解電流で
電解して陽イオン交換膜から不純物を除去するすること
により電解性能を回復させることを特徴とするものであ
る。従って、従来のようには塩酸を使うことがないの
で、残留塩酸による酸素濃度の低下や塩素混入による危
険性が無い。しかも、複雑な水電解槽構造やイオン交換
器を必要とせず、簡単容易に電解性能を回復させること
ができる。本発明の価値は大きい。The method for recovering the performance of the water electrolysis cell according to the present invention is to electrolyze a cation exchange membrane water electrolysis cell in which impurities have accumulated in the cation exchange membrane and the electrolysis performance has deteriorated, with an electrolysis current higher than the rated value. The electrolytic performance is recovered by removing impurities from the cation exchange membrane. Therefore, since hydrochloric acid is not used as in the prior art, there is no risk of a decrease in oxygen concentration due to residual hydrochloric acid or chlorine contamination. Moreover, the electrolytic performance can be easily and easily restored without the need for a complicated water electrolysis cell structure or an ion exchanger. The value of the present invention is great.
【図１】陽イオン交換膜水電解槽をしめす概略図であ
る。FIG. 1 is a schematic view showing a cation exchange membrane water electrolysis cell.
【図２】水電解の電流密度−電圧特性を示す図である。FIG. 2 is a diagram showing current density-voltage characteristics of water electrolysis.
１ 陽イオン交換膜 ２ 陽極 ３ 陰極 1 Cation exchange membrane 2 Anode 3 Cathode
Claims (1)
性能が劣化した陽イオン交換膜水電解槽を、定格以上の
電解電流で電解して陽イオン交換膜から不純物を除去す
ることにより電解性能を回復させること、 を特徴とする水電解槽の性能回復方法。1. A cation exchange membrane water electrolysis cell in which impurities are retained in the cation exchange membrane and electrolysis performance is deteriorated, and electrolysis is performed by removing the impurities from the cation exchange membrane by electrolyzing the cation exchange membrane water electrolysis cell with an electrolytic current higher than the rated value. A method for recovering performance of a water electrolysis cell, which comprises recovering performance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4266743A JPH0747131B2 (en) | 1992-09-08 | 1992-09-08 | How to recover performance of water electrolyzer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4266743A JPH0747131B2 (en) | 1992-09-08 | 1992-09-08 | How to recover performance of water electrolyzer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0686939A JPH0686939A (en) | 1994-03-29 |
| JPH0747131B2 true JPH0747131B2 (en) | 1995-05-24 |
Family
ID=17435093
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4266743A Expired - Lifetime JPH0747131B2 (en) | 1992-09-08 | 1992-09-08 | How to recover performance of water electrolyzer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0747131B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7129941B2 (en) * | 2019-04-12 | 2022-09-02 | 日立造船株式会社 | Water electrolysis device performance recovery method and water electrolysis device |
| CN117926341B (en) * | 2024-01-19 | 2024-09-10 | 华北电力大学 | A performance recovery method and system for PEM electrolyzer |
-
1992
- 1992-09-08 JP JP4266743A patent/JPH0747131B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0686939A (en) | 1994-03-29 |
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