JP2001073172A - Electrolytic treating method for waste solution - Google Patents
Electrolytic treating method for waste solutionInfo
- Publication number
- JP2001073172A JP2001073172A JP24796099A JP24796099A JP2001073172A JP 2001073172 A JP2001073172 A JP 2001073172A JP 24796099 A JP24796099 A JP 24796099A JP 24796099 A JP24796099 A JP 24796099A JP 2001073172 A JP2001073172 A JP 2001073172A
- Authority
- JP
- Japan
- Prior art keywords
- exchange membrane
- cathode
- anion exchange
- anode
- membrane
- 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.)
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- ing And Chemical Polishing (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
(57)【要約】
【課題】 環境に有害な塩素ガスが発生することなく、
廃液から有価金属を回収する。
【解決手段】 金属を含有する酸性廃液を電解して金属
を回収する電解処理方法方法であって、カソード電極と
アノード電極との間に陰イオン交換膜と陽イオン交換膜
からなるバイポーラ膜を取り付けて、電解槽をカソード
部とアノード部とに分離し、前記カソード部には酸性廃
液を注入し、前記アノード部にはアルカリ性水溶液を注
入した後、電解を行うことを特徴とする廃液の電解処理
方法。
(57) [Abstract] [Problem] Without generating harmful chlorine gas to the environment,
Recover valuable metals from wastewater. SOLUTION: The electrolytic treatment method for recovering metal by electrolyzing an acidic waste liquid containing metal, wherein a bipolar membrane comprising an anion exchange membrane and a cation exchange membrane is attached between a cathode electrode and an anode electrode. Separating the electrolytic cell into a cathode portion and an anode portion, injecting an acidic waste liquid into the cathode portion, injecting an alkaline aqueous solution into the anode portion, and then performing electrolysis. Method.
Description
【０００１】[0001]
【産業上の利用分野】本発明は、廃液の電解処理方法に
関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for electrolytically treating waste liquid.
【０００２】[0002]
【従来技術】特開平３−３５２５６１号には、アンモニ
ア性銅塩化物エッチング液を電解し、カソード電極に銅
を析出させる技術が記載されている。また、アノード電
極には、炭素あるいは、インジウム、ルテニウム、白
金、パラジウム、金等で被覆したチタン電極を用いるこ
と、アノード部での塩素ガス発生が抑制できるとの記載
がされている。しかし、酸性の水溶液では、このような
電極を用いて電解すると塩素ガス発生が抑制できないと
いう問題がある。2. Description of the Related Art Japanese Patent Application Laid-Open No. 3-352561 discloses a technique in which an ammoniacal copper chloride etching solution is electrolyzed to deposit copper on a cathode electrode. Further, it is described that a titanium electrode coated with carbon or indium, ruthenium, platinum, palladium, gold, or the like is used as the anode electrode, and generation of chlorine gas at the anode part can be suppressed. However, in the case of an acidic aqueous solution, there is a problem that chlorine gas generation cannot be suppressed when electrolysis is performed using such an electrode.
【０００３】[0003]
【発明が解決しようとする課題】本発明者は、上述の通
り、通常の電解では、アノード側で有害な塩素ガスや、
亜硝酸ガスが発生するが、電極の間に陰イオン交換膜と
陽イオン交換膜を挟むとアノード側で有害な塩素ガスが
発生しないことを見出し、本発明に至った。As described above, the present inventor has found that in normal electrolysis, harmful chlorine gas or
Although nitrite gas is generated, it has been found that no harmful chlorine gas is generated on the anode side when an anion exchange membrane and a cation exchange membrane are interposed between electrodes, and the present invention has been accomplished.
【０００４】[0004]
【課題を解決するための手段】よって、本発明は、金属
を含有する酸性廃液を電解して金属を回収する電解処理
方法方法であって、カソード電極とアノード電極との間
に陰イオン交換膜と陽イオン交換膜からなるバイポーラ
膜を取り付けて、電解槽をカソード部とアノード部とに
分離し、前記カソード部には酸性廃液を注入し、前記ア
ノード部にはアルカリ性水溶液を注入した後、電解を行
うことを特徴とする廃液の電解処理方法である。SUMMARY OF THE INVENTION Accordingly, the present invention is an electrolytic treatment method for recovering a metal by electrolyzing an acidic waste liquid containing a metal, wherein an anion exchange membrane is provided between a cathode electrode and an anode electrode. And a bipolar membrane comprising a cation exchange membrane, and the electrolytic cell was separated into a cathode part and an anode part. An acidic waste liquid was injected into the cathode part, and an alkaline aqueous solution was injected into the anode part. And a method for electrolytically treating waste liquid.
【０００５】また、本発明は、金属を含有する酸性廃液
を電解して金属を回収する電解処理方法であって、カソ
ード電極の隣に陰イオン交換膜を、該陰イオン交換膜と
アノード電極との側に陰イオン交換膜と陽イオン交換膜
とからなるバイポーラ膜を配置し、電解槽をカソード部
とアノード部、及び前記陰イオン交換膜と前記バイポー
ラ膜との間の間隙部とに分離し、前記カソード部には酸
性廃液を注入し、前記アノード部にはアルカリ性水溶液
を注入し、前記陰イオン交換膜と陽イオン交換膜との間
の間隙部には水を注入した後、電解を行うことを特徴と
する廃液の電解処理方法である。また、本発明は、カソ
ード電極と陰イオン交換膜との間、及びアノード電極
と、陰イオン交換膜と陽イオン交換膜とからなるバイポ
ーラ膜との間に、隔膜を取り付けることを特徴とする前
記記載の廃液の電解処理方法である。[0005] The present invention also relates to an electrolytic treatment method for recovering metal by electrolyzing an acidic waste liquid containing metal, wherein an anion exchange membrane is provided next to the cathode electrode and the anion exchange membrane and the anode electrode are connected to each other. Side, a bipolar membrane comprising an anion exchange membrane and a cation exchange membrane is arranged, and the electrolytic cell is separated into a cathode section and an anode section, and a gap between the anion exchange membrane and the bipolar membrane. An acidic waste liquid is injected into the cathode, an alkaline aqueous solution is injected into the anode, water is injected into a gap between the anion exchange membrane and the cation exchange membrane, and then electrolysis is performed. This is a method for electrolytically treating a waste liquid. Further, the present invention is characterized in that a diaphragm is attached between a cathode electrode and an anion exchange membrane, and between an anode electrode and a bipolar membrane composed of an anion exchange membrane and a cation exchange membrane. An electrolytic treatment method for the waste liquid described above.
【０００６】[0006]
【実施例】実施例１ 図１に概略図として示すように、カソード電極１とアノ
ード電極２との間に、陰イオン交換膜３と、陽イオン交
換膜４とからなるバイポーラ膜（室町化学工業（株）製
MC-３４７０）を電解槽５に取り付けて電解を行った。
ここで、カソード電極１の材質はステンレスであり、ア
ノード電極２の材質はカーボンとした。カソード部６に
は約１モル／ｌの塩化第２銅溶液（６４ｇ／ｌ）を０．
１６ｌ、アノード部７には約０．０１モル／ｌのアンモ
ニア水溶液を０．１６ｌ入れ、０．５Ａで２４時間電解
を行い、カソード部６で１０．２ｇの金属銅が回収でき
た。カソード部６に残った溶液の銅イオン濃度は、０．
５４ｇ／ｌ、塩素イオン濃度は、６３ｇ／ｌであった。
また、電解中、アノード部７で塩素ガスの発生は認めら
れなかった。EXAMPLE 1 As schematically shown in FIG. 1, a bipolar membrane comprising an anion exchange membrane 3 and a cation exchange membrane 4 between a cathode electrode 1 and an anode electrode 2 (Muromachi Chemical Industry Co., Ltd.) Co., Ltd.
(MC-3470) was attached to the electrolytic cell 5 for electrolysis.
Here, the material of the cathode electrode 1 was stainless steel, and the material of the anode electrode 2 was carbon. About 1 mol / l of a cupric chloride solution (64 g / l) was added to the cathode section 6 at a concentration of 0.1 g / l.
16 l and 0.16 l of an aqueous solution of about 0.01 mol / l of ammonia were placed in the anode section 7, electrolysis was performed at 0.5 A for 24 hours, and 10.2 g of metallic copper could be recovered in the cathode section 6. The copper ion concentration of the solution remaining in the cathode section 6 is 0.1.
The concentration was 54 g / l, and the chloride ion concentration was 63 g / l.
During the electrolysis, generation of chlorine gas was not observed in the anode part 7.
【０００７】実施例２ 図２に示すように、カソード電極１とアノード電極２と
の間に、陰イオン交換膜３と、陽イオン交換膜４とから
なるバイポーラ膜（室町化学工業（株）製MC-３４７
０）を電解槽５に取り付けて電解を行った。ここで、カ
ソード電極１の材質はステンレスであり、アノード電極
２の材質はカーボンとした。また、カソード部６で発生
する金属銅粉によるバイポーラ膜の目詰まりを防止する
為に、カソード電極１とバイポーラ膜との間に隔膜８
（Ｎｏ．２ろ紙）を間に挟んで取り付けた。Embodiment 2 As shown in FIG. 2, a bipolar membrane comprising an anion exchange membrane 3 and a cation exchange membrane 4 (manufactured by Muromachi Chemical Co., Ltd.) is provided between a cathode electrode 1 and an anode electrode 2. MC-347
0) was attached to the electrolytic cell 5 to perform electrolysis. Here, the material of the cathode electrode 1 was stainless steel, and the material of the anode electrode 2 was carbon. Further, in order to prevent clogging of the bipolar film due to metallic copper powder generated in the cathode portion 6, a diaphragm 8 is provided between the cathode electrode 1 and the bipolar film.
(No. 2 filter paper).
【０００８】カソード部６には約１モル／ｌの塩化第２
銅溶液（６４ｇ／ｌ）を０．１６ｌ、アノード部７には
約０．０１モル／ｌのアンモニア水溶液を０．１６ｌ入
れ、０．５Ａで２４時間電解を行い、カソード部６で１
０．２ｇの金属銅が回収できた。カソード部６に残った
溶液の銅イオン濃度は、０．５４ｇ／ｌ、塩素イオン濃
度は、６３ｇ／ｌであった。また、電解中、アノード部
７で塩素ガスの発生は認められなかった。なお、隔膜８
を、アノード電極２とバイポーラ膜との間に設けると、
液中に混入したゴミ等の浮遊物によるバイポーラ膜の目
詰まりを防止できた。The cathode section 6 has about 1 mol / l of secondary chloride
0.16 l of a copper solution (64 g / l) and 0.16 l of an aqueous ammonia solution of about 0.01 mol / l in the anode section 7, electrolysis was performed at 0.5 A for 24 hours, and 1
0.2 g of metallic copper could be recovered. The solution remaining in the cathode section 6 had a copper ion concentration of 0.54 g / l and a chloride ion concentration of 63 g / l. During the electrolysis, generation of chlorine gas was not observed in the anode part 7. The diaphragm 8
Is provided between the anode electrode 2 and the bipolar film,
The clogging of the bipolar membrane due to suspended matter such as dust mixed in the liquid was prevented.
【０００９】実施例３ 図３に示すように、カソード電極１とアノード電極２と
の間に、陰イオン交換膜３と、陰イオン交換膜３と陽イ
オン交換膜４とからなるバイポーラ膜（室町化学工業
（株）製MC-３４７０）とを電解槽５に取り付けて電解
を行った。ここで、カソード電極１の材質はステンレス
であり、アノード電極２の材質はカーボンとした。カソ
ード部６には約１モル／ｌの塩化第２銅溶液（６４ｇ／
ｌ）を０．１６ｌ、アノード部７には約０．００５モル
／ｌの水酸化カルシウム水溶液を０．１６ｌ入れ、ま
た、陰イオン交換膜３とバイポーラ膜との間の酸回収部
９には０．０８ｌの水を入れた。０．５Ａで２４時間電
解を行い、カソード部６で１０．４ｇの金属銅が回収で
きた。カソード部６に残った溶液の銅イオン濃度は、
０．４８ｇ／ｌ、酸回収部９の銅イオン濃度は０．１１
ｇ／ｌ、塩素イオン濃度は、１２０ｇ／ｌであった。ま
た、電解中、アノード部７で塩素ガスの発生は認められ
なかった。Embodiment 3 As shown in FIG. 3, a bipolar membrane (Muromachi) comprising an anion exchange membrane 3 and an anion exchange membrane 3 and a cation exchange membrane 4 is provided between a cathode electrode 1 and an anode electrode 2. (MC-3470 manufactured by Chemical Industry Co., Ltd.) was attached to the electrolytic cell 5 for electrolysis. Here, the material of the cathode electrode 1 was stainless steel, and the material of the anode electrode 2 was carbon. About 1 mol / l cupric chloride solution (64 g /
0.16 l), 0.16 l of an aqueous solution of about 0.005 mol / l calcium hydroxide in the anode section 7, and the acid recovery section 9 between the anion exchange membrane 3 and the bipolar membrane 0.08 l of water was charged. Electrolysis was performed at 0.5 A for 24 hours, and 10.4 g of metallic copper could be recovered at the cathode 6. The copper ion concentration of the solution remaining in the cathode section 6 is
0.48 g / l, the concentration of copper ions in the acid recovery section 9 is 0.11
g / l and chloride ion concentration were 120 g / l. During the electrolysis, generation of chlorine gas was not observed in the anode part 7.
【００１０】また、図４に示すように、カソード電極１
と陰イオン交換膜３との間に隔膜８（Ｎｏ．２ろ紙）を
間に挟んで取り付けた場合、カソード部６で発生する金
属銅粉によるイオン交換膜の目詰まりを防止できた。ま
た、隔膜８を、アノード電極２とバイポーラ膜との間に
設けると、液中に混入したゴミ等の浮遊物によるバイポ
ーラ膜の目詰まりを防止できた。Further, as shown in FIG.
When the diaphragm 8 (No. 2 filter paper) was interposed between the ion exchange membrane and the anion exchange membrane 3, clogging of the ion exchange membrane due to metallic copper powder generated in the cathode part 6 could be prevented. Further, when the diaphragm 8 was provided between the anode electrode 2 and the bipolar membrane, clogging of the bipolar membrane due to suspended matter such as dust mixed in the liquid could be prevented.
【００１１】[0011]
【発明の効果】環境に有害な塩素ガスが発生することな
く、廃液から有価金属を回収できる。According to the present invention, valuable metals can be recovered from waste liquid without generating chlorine gas harmful to the environment.
【図１】本発明に関する電解槽。FIG. 1 shows an electrolytic cell according to the present invention.
【図２】本発明に関する電解槽。FIG. 2 is an electrolytic cell according to the present invention.
【図３】本発明に関する電解槽。FIG. 3 is an electrolytic cell according to the present invention.
【図４】本発明に関する電解槽。FIG. 4 is an electrolytic cell according to the present invention.
１…カソード電極、２…アノード電極、３…陰イオン交
換膜、４…陽イオン交換膜、５…電解槽、６…カソード
部、７…アノード部、８…隔膜、９…酸回収部。DESCRIPTION OF SYMBOLS 1 ... Cathode electrode, 2 ... Anode electrode, 3 ... Anion exchange membrane, 4 ... Cation exchange membrane, 5 ... Electrolyzer, 6 ... Cathode part, 7 ... Anode part, 8 ... Diaphragm, 9 ... Acid recovery part.
Claims (3)
回収する電解処理方法方法であって、カソード電極とア
ノード電極との間に陰イオン交換膜と陽イオン交換膜か
らなるバイポーラ膜を取り付けて、電解槽をカソード部
とアノード部とに分離し、前記カソード部には酸性廃液
を注入し、前記アノード部にはアルカリ性水溶液を注入
した後、電解を行うことを特徴とする廃液の電解処理方
法。An electrolytic treatment method for recovering a metal by electrolyzing an acidic waste liquid containing a metal, wherein a bipolar membrane comprising an anion exchange membrane and a cation exchange membrane is provided between a cathode electrode and an anode electrode. Attached, the electrolytic cell is separated into a cathode part and an anode part, an acidic waste liquid is injected into the cathode part, an alkaline aqueous solution is injected into the anode part, and then electrolysis is performed. Processing method.
回収する電解処理方法であって、カソード電極の隣に陰
イオン交換膜を、該陰イオン交換膜とアノード電極との
側に陰イオン交換膜と陽イオン交換膜とからなるバイポ
ーラ膜を配置し、電解槽をカソード部とアノード部、及
び前記陰イオン交換膜と前記バイポーラ膜との間の間隙
部とに分離し、前記カソード部には酸性廃液を注入し、
前記アノード部にはアルカリ性水溶液を注入し、前記陰
イオン交換膜と陽イオン交換膜との間の間隙部には水を
注入した後、電解を行うことを特徴とする廃液の電解処
理方法。2. An electrolytic treatment method for recovering a metal by electrolyzing an acidic waste liquid containing a metal, wherein an anion exchange membrane is provided next to the cathode electrode and an anion exchange membrane is provided on the side of the anion exchange membrane and the anode electrode. A bipolar membrane composed of an ion exchange membrane and a cation exchange membrane is arranged, and the electrolytic cell is separated into a cathode part and an anode part, and a gap between the anion exchange membrane and the bipolar membrane, and the cathode part is separated. Inject acidic wastewater into
A method for electrolytically treating a waste liquid, comprising: injecting an alkaline aqueous solution into the anode part, injecting water into a gap between the anion exchange membrane and the cation exchange membrane, and then performing electrolysis.
びアノード電極と、陰イオン交換膜と陽イオン交換膜と
からなるバイポーラ膜との間に、隔膜を取り付けること
を特徴とする請求項１または請求項２記載の廃液の電解
処理方法。3. A membrane is attached between a cathode electrode and an anion exchange membrane and between an anode electrode and a bipolar membrane comprising an anion exchange membrane and a cation exchange membrane. 3. The method for electrolytically treating waste liquid according to claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24796099A JP2001073172A (en) | 1999-09-01 | 1999-09-01 | Electrolytic treating method for waste solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24796099A JP2001073172A (en) | 1999-09-01 | 1999-09-01 | Electrolytic treating method for waste solution |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2001073172A true JP2001073172A (en) | 2001-03-21 |
Family
ID=17171123
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24796099A Pending JP2001073172A (en) | 1999-09-01 | 1999-09-01 | Electrolytic treating method for waste solution |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2001073172A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101528777B1 (en) * | 2013-09-25 | 2015-06-15 | (주) 시온텍 | Bipolar ion exchange sheet for recovering valuables, method of manufacturing the same and apparatus for recovering valuables |
| WO2025010355A1 (en) * | 2023-07-05 | 2025-01-09 | X Development Llc | Methods of remediating waste and systems thereof |
-
1999
- 1999-09-01 JP JP24796099A patent/JP2001073172A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101528777B1 (en) * | 2013-09-25 | 2015-06-15 | (주) 시온텍 | Bipolar ion exchange sheet for recovering valuables, method of manufacturing the same and apparatus for recovering valuables |
| WO2025010355A1 (en) * | 2023-07-05 | 2025-01-09 | X Development Llc | Methods of remediating waste and systems thereof |
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