JP6116658B2 - 気体溶解装置及び気体溶解方法 - Google Patents
気体溶解装置及び気体溶解方法 Download PDFInfo
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- JP6116658B2 JP6116658B2 JP2015255409A JP2015255409A JP6116658B2 JP 6116658 B2 JP6116658 B2 JP 6116658B2 JP 2015255409 A JP2015255409 A JP 2015255409A JP 2015255409 A JP2015255409 A JP 2015255409A JP 6116658 B2 JP6116658 B2 JP 6116658B2
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 192
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 183
- 239000001257 hydrogen Substances 0.000 claims description 177
- 229910052739 hydrogen Inorganic materials 0.000 claims description 177
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Description
前記溶存槽に加圧貯留された水素水を再度、前記加圧型気体溶解手段に送出し水素バブルと同時に加圧送水することを特徴としてもよい。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.6mのポリプロピレン製のものを使用した。圧力を0.41MPa、水素発生量を21cm3/min、水の流量を730cm3/minで行った。30分運転後の水中の水素濃度は、7℃で6.5ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を水道に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.6mのポリプロピレン製のものを使用した。圧力を0.25MPa、水素発生量を21cm3/min、水の流量を730cm3/minで行った。30分運転後の水中の水素濃度は、11℃で2.6ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.6mのポリプロピレン製のものを使用した。圧力を0.30MPa、水素発生量を21cm3/min、水の流量を730cm3/minで行った。30分運転後の水中の水素濃度は、7℃で5.9ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.5mのポリプロピレン製のものを使用した。圧力を0.35MPa、水素発生量を25cm3/min、水の流量を590cm3/minで行った。30分運転後の水中の水素濃度は、7℃で3.0ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.6mのポリプロピレン製のものを使用した。圧力を0.38MPa、水素発生量を25cm3/min、水の流量を560cm3/minで行った。30分運転後の水中の水素濃度は、7℃で3.8ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.8mのポリプロピレン製のものを使用した。圧力を0.40MPa、水素発生量を25cm3/min、水の流量を540cm3/minで行った。30分運転後の水中の水素濃度は、7℃で4.2ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.8mのポリプロピレン製のものを使用した。圧力を0.45MPa、水素発生量を20cm3/min、水の流量を560cm3/minで行った。30分運転後の水中の水素濃度は、7℃で4.5ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.8mのポリプロピレン製のものを使用した。圧力を0.50MPa、水素発生量を15cm3/min、水の流量を570cm3/minで行った。30分運転後の水中の水素濃度は、7℃で4.2ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ2.0mのポリプロピレン製のものを使用した。圧力を0.60MPa、水素発生量を15cm3/min、水の流量を460cm3/minで行った。30分運転後の水中の水素濃度は、7℃で3.4ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ1.4mのポリプロピレン製のものを使用した。圧力を0.20MPa、水素発生量を30cm3/min、水の流量を550cm3/minで行った。30分運転後の水中の水素濃度は、7℃で2.7ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ3mのポリプロピレン製のものを使用した。圧力を0.50MPa、水素発生量を20cm3/min、水の流量を550cm3/minで行った。30分運転後の水中の水素濃度は、7℃で2.4ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径3mmで長さ4mのポリプロピレン製のものを使用した。圧力を0.35MPa、水素発生量を20cm3/min、水の流量を650cm3/minで行った。30分運転後の水中の水素濃度は、7℃で3.5ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図3に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径3mmで長さ2.5mのポリプロピレン製のものを使用した。圧力を0.25MPa、水素発生量を20cm3/min、水の流量を700cm3/minで行った。30分運転後の水中の水素濃度は、7℃で3.0ppmの水素水となり、過飽和の状態を維持していた。
図1に示す気体溶解装置1を図2に示すように市販のウォーターサーバー100に接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径2mmで長さ0.4mのポリプロピレン製のものを使用した。圧力を0.05MPa、水素発生量を21cm3/min、水の流量を960cm3/minで行った。30分運転後の水中の水素濃度は、7℃で1.6ppmの水素水となり、過飽和の状態を維持できなかった。
図1に示す気体溶解装置1を図2に示すように市販のウォーターサーバーに接続して、4回循環して、水素水を生成した。降圧移送手段5の細管5aは、内径3mmで長さ0.8mのポリプロピレン製のものを使用した。圧力を0.08MPa、水素発生量を21cm3/min、水の流量を900cm3/minで行った。30分運転後の水中の水素濃度は、7℃で1.8ppmの水素水となり、過飽和の状態を維持できなかった。
2 気体発生手段
21 水素発生手段
22 イオン交換手段
23 水素発生手段用取入口
24 水素供給管
25 酸素排出口
3 加圧型気体溶解手段
4 溶存槽
41、42 溶存タンク
5 降圧移送手段
5a 細管
6 コントロール機構
7、8 液体吸入口
9、10 吐出口
100 ウォーターサーバー
Claims (4)
- 水に水素を溶解させて水素水を生成する気体溶解装置であって、
水槽と、
固体高分子膜(PEM)を挟んだ電気分解により水素を発生させる水素発生手段と、
前記水素発生手段からの水素を水素バブルとして前記水槽からの水に与えて加圧送水する加圧型気体溶解手段と、
前記加圧型気体溶解手段から水素水を導いて貯留する溶存槽と、
前記溶存槽に貯留された水素水を前記水槽中に導く降圧移送手段としての管状路と、を含み、
前記水槽中の水を前記加圧型気体溶解手段、前記溶存槽、前記管状路、前記水槽へと送水して循環させ前記水素バブルをナノバブルとするとともに、前記加圧型気体溶解手段から前記溶存槽へと送水される水の一部を前記水素発生手段に導き電気分解に供することを特徴とする気体溶解装置。 - 前記溶存槽は前記加圧型気体溶解手段からの水素水を加圧貯留することを特徴とする請求項1記載の気体溶解装置。
- 前記溶存槽は少なくともその一部にフィルターを与えられていることを特徴とする請求項2記載の気体溶解装置。
- 前記加圧型気体溶解手段はダイヤフラムポンプを含むことを特徴とする請求項1乃至3のうちの1つに記載の気体溶解装置。
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