JPS62247884A - Treatment of iron ion-containing liquid - Google Patents
Treatment of iron ion-containing liquidInfo
- Publication number
- JPS62247884A JPS62247884A JP8955286A JP8955286A JPS62247884A JP S62247884 A JPS62247884 A JP S62247884A JP 8955286 A JP8955286 A JP 8955286A JP 8955286 A JP8955286 A JP 8955286A JP S62247884 A JPS62247884 A JP S62247884A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- iron
- extraction
- contg
- extractant
- 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.)
- Pending
Links
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 65
- 239000007788 liquid Substances 0.000 title claims abstract description 50
- -1 polytetrafluoroethylene Polymers 0.000 claims abstract description 57
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 24
- 239000007787 solid Substances 0.000 claims abstract description 19
- 150000001412 amines Chemical group 0.000 claims abstract description 13
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 12
- GRWZHXKQBITJKP-UHFFFAOYSA-L dithionite(2-) Chemical compound [O-]S(=O)S([O-])=O GRWZHXKQBITJKP-UHFFFAOYSA-L 0.000 claims abstract description 7
- 238000000034 method Methods 0.000 claims description 33
- 239000012528 membrane Substances 0.000 claims description 29
- 238000000605 extraction Methods 0.000 abstract description 54
- 229920001343 polytetrafluoroethylene Polymers 0.000 abstract description 7
- 239000004810 polytetrafluoroethylene Substances 0.000 abstract description 7
- 239000002699 waste material Substances 0.000 abstract description 7
- 238000009825 accumulation Methods 0.000 abstract description 4
- 150000002500 ions Chemical class 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 20
- 238000007747 plating Methods 0.000 description 18
- 238000005246 galvanizing Methods 0.000 description 7
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 6
- 239000011701 zinc Substances 0.000 description 6
- 229910052725 zinc Inorganic materials 0.000 description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 5
- 239000003456 ion exchange resin Substances 0.000 description 5
- 229920003303 ion-exchange polymer Polymers 0.000 description 5
- 238000004945 emulsification Methods 0.000 description 4
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 229910001447 ferric ion Inorganic materials 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- XTAZYLNFDRKIHJ-UHFFFAOYSA-N n,n-dioctyloctan-1-amine Chemical compound CCCCCCCCN(CCCCCCCC)CCCCCCCC XTAZYLNFDRKIHJ-UHFFFAOYSA-N 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 3
- 229960001763 zinc sulfate Drugs 0.000 description 3
- 229910000368 zinc sulfate Inorganic materials 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910001448 ferrous ion Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000010979 pH adjustment Methods 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- VBCJJAZGEJSVTL-UHFFFAOYSA-N (Z)-18-methylnonadec-9-en-1-amine Chemical compound CC(CCCCCCCC=C/CCCCCCCCN)C VBCJJAZGEJSVTL-UHFFFAOYSA-N 0.000 description 1
- UAMXXKRCPLMMPO-UHFFFAOYSA-N 2,3,3-trimethylpentan-2-amine Chemical compound CCC(C)(C)C(C)(C)N UAMXXKRCPLMMPO-UHFFFAOYSA-N 0.000 description 1
- OHNIDNZHXZEIAL-UHFFFAOYSA-N 3,9-diethyltridecan-6-amine Chemical compound CCCCC(CC)CCC(N)CCC(CC)CC OHNIDNZHXZEIAL-UHFFFAOYSA-N 0.000 description 1
- YKGBNAGNNUEZQC-UHFFFAOYSA-N 6-methyl-n,n-bis(6-methylheptyl)heptan-1-amine Chemical compound CC(C)CCCCCN(CCCCCC(C)C)CCCCCC(C)C YKGBNAGNNUEZQC-UHFFFAOYSA-N 0.000 description 1
- SAIKULLUBZKPDA-UHFFFAOYSA-N Bis(2-ethylhexyl) amine Chemical compound CCCCC(CC)CNCC(CC)CCCC SAIKULLUBZKPDA-UHFFFAOYSA-N 0.000 description 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- FCMYSEXCLRFWBP-UHFFFAOYSA-N [NH4+].[NH4+].[O-]S(=O)S([O-])=O Chemical compound [NH4+].[NH4+].[O-]S(=O)S([O-])=O FCMYSEXCLRFWBP-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- HXWGXXDEYMNGCT-UHFFFAOYSA-M decyl(trimethyl)azanium;chloride Chemical compound [Cl-].CCCCCCCCCC[N+](C)(C)C HXWGXXDEYMNGCT-UHFFFAOYSA-M 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- WLCFKPHMRNPAFZ-UHFFFAOYSA-M didodecyl(dimethyl)azanium;chloride Chemical compound [Cl-].CCCCCCCCCCCC[N+](C)(C)CCCCCCCCCCCC WLCFKPHMRNPAFZ-UHFFFAOYSA-M 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- JRBPAEWTRLWTQC-UHFFFAOYSA-N dodecylamine Chemical compound CCCCCCCCCCCCN JRBPAEWTRLWTQC-UHFFFAOYSA-N 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- YWFWDNVOPHGWMX-UHFFFAOYSA-N n,n-dimethyldodecan-1-amine Chemical compound CCCCCCCCCCCCN(C)C YWFWDNVOPHGWMX-UHFFFAOYSA-N 0.000 description 1
- NHLUVTZJQOJKCC-UHFFFAOYSA-N n,n-dimethylhexadecan-1-amine Chemical compound CCCCCCCCCCCCCCCCN(C)C NHLUVTZJQOJKCC-UHFFFAOYSA-N 0.000 description 1
- MJCJUDJQDGGKOX-UHFFFAOYSA-N n-dodecyldodecan-1-amine Chemical compound CCCCCCCCCCCCNCCCCCCCCCCCC MJCJUDJQDGGKOX-UHFFFAOYSA-N 0.000 description 1
- FILZIXBTUOHUIC-UHFFFAOYSA-N n-methyl-n-tridecyltridecan-1-amine Chemical compound CCCCCCCCCCCCCN(C)CCCCCCCCCCCCC FILZIXBTUOHUIC-UHFFFAOYSA-N 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- HEZHYQDYRPUXNJ-UHFFFAOYSA-L potassium dithionite Chemical compound [K+].[K+].[O-]S(=O)S([O-])=O HEZHYQDYRPUXNJ-UHFFFAOYSA-L 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 150000003335 secondary amines Chemical class 0.000 description 1
- JVBXVOWTABLYPX-UHFFFAOYSA-L sodium dithionite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])=O JVBXVOWTABLYPX-UHFFFAOYSA-L 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical class [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- RJSZFSOFYVMDIC-UHFFFAOYSA-N tert-butyl n,n-dimethylcarbamate Chemical compound CN(C)C(=O)OC(C)(C)C RJSZFSOFYVMDIC-UHFFFAOYSA-N 0.000 description 1
- ABVVEAHYODGCLZ-UHFFFAOYSA-N tridecan-1-amine Chemical compound CCCCCCCCCCCCCN ABVVEAHYODGCLZ-UHFFFAOYSA-N 0.000 description 1
- SWZDQOUHBYYPJD-UHFFFAOYSA-N tridodecylamine Chemical compound CCCCCCCCCCCCN(CCCCCCCCCCCC)CCCCCCCCCCCC SWZDQOUHBYYPJD-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
- 150000003751 zinc Chemical class 0.000 description 1
Landscapes
- Physical Water Treatments (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
Description
【発明の詳細な説明】
[産業上の利用分野]
本発明は鉄イオン含有液の処理方法に係り、特に電気亜
鉛メッキ浴液等の鉄イオン含有液から鉄イオンを効率的
に除去することができる鉄イオン含有液の処理方法に関
する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for treating iron ion-containing liquids, and in particular to a method for efficiently removing iron ions from iron ion-containing liquids such as electrogalvanizing bath liquids. This invention relates to a method for treating a liquid containing iron ions.
[従来の技術]
電気亜鉛メッキ鉄板の製造に用いられる電気亜鉛メッキ
浴としては、従来より硫酸亜鉛浴、塩化物浴、ホウフッ
化物浴、シアン化物のアルカリ性浴、ビロリン酸浴等が
知られているが、これらのうち、メッキ液の管理が容易
であることから、硫酸亜鉛浴が最もよく用いられている
。 。[Prior Art] As electrogalvanizing baths used in the production of electrogalvanized iron sheets, zinc sulfate baths, chloride baths, borofluoride baths, alkaline cyanide baths, birophosphoric acid baths, etc. are conventionally known. However, among these, the zinc sulfate bath is most commonly used because the plating solution is easy to manage. .
ところで、硫酸亜鉛メッキ浴のpHは、通常、亜鉛を溶
解させるために低くしている。そのため、被メツキ鉄板
、電解タンク等から鉄が溶出して、該メッキ浴の鉄イオ
ン濃度が増し各種の問題が起きる。例えば、得られる電
気亜鉛メッキ鉄板の製品表面特性を劣化させたり、電解
タンク、配管、ポンプ等の金属の溶損な早めたりするの
である。Incidentally, the pH of the zinc sulfate plating bath is usually kept low in order to dissolve zinc. Therefore, iron is leached from the plated iron plate, electrolytic tank, etc., and the iron ion concentration in the plating bath increases, causing various problems. For example, it may deteriorate the surface properties of the resulting electrogalvanized iron plate, or it may accelerate the erosion of metals in electrolytic tanks, piping, pumps, etc.
従来、電気亜鉛メッキ浴液から鉄イオンを除去する方法
として、電気亜鉛メッキ浴液をキレート性イオン交換樹
脂を充填した交換塔に通液し、鉄イオンを吸着除去する
方法(特公昭57−27960)が提案されている。こ
の方法によれば、電気亜鉛メッキ浴液から鉄イオンを選
択的に除去することが可能である。Conventionally, as a method for removing iron ions from an electrogalvanizing bath solution, the electrolytic galvanizing bath solution is passed through an exchange column filled with a chelating ion exchange resin, and iron ions are adsorbed and removed (Japanese Patent Publication No. 57-27960). ) has been proposed. According to this method, it is possible to selectively remove iron ions from the electrogalvanizing bath solution.
[発明が解決しようとする問題点]
しかしながら、キレート性イオン交換樹脂による方法で
は、原水である電気亜鉛メッキ浴液中の鉄イオン濃度(
1000〜lO100OOpp及びイオン交換樹脂の吸
着量(0,2〜0.8モル/見−樹脂)から考えて、原
水と同量程度の再生廃液が発生し、その処理が必要とな
る。また、吸着速度が遅い(SV=1hr ’程度)た
め、多量の樹脂を必要とし、装置が大型化する等の欠点
もある。[Problems to be solved by the invention] However, in the method using chelating ion exchange resin, the iron ion concentration (
Considering the amount of adsorption of the ion exchange resin (0.2 to 0.8 moles/resin), approximately the same amount of recycled waste liquid as the raw water is generated and must be treated. Furthermore, since the adsorption rate is slow (SV=about 1 hr'), a large amount of resin is required, and the apparatus has disadvantages such as an increase in size.
[問題点を解決するための手段]
本発明は、電気亜鉛メッキ浴液等の鉄イオン含有液から
、鉄イオンを効率的に除去する方法を提供するものであ
って、
鉄イオン含有液と、一級〜四級アミンの少なくとも1種
を含む抽出剤とを接触させた後、抽出剤をpH3,5以
下で還元剤を含む逆抽出剤と接触させて鉄イオンを逆抽
出することを特徴とする鉄イオン含有液の処理方法、
を要旨とするものである。[Means for Solving the Problems] The present invention provides a method for efficiently removing iron ions from an iron ion-containing solution such as an electrogalvanizing bath solution, comprising: an iron ion-containing solution; It is characterized by contacting with an extractant containing at least one of primary to quaternary amines, and then contacting the extractant with a back-extracting agent containing a reducing agent at a pH of 3.5 or less to back-extract iron ions. The gist is a method for treating iron ion-containing liquids.
即ち、本出願人は、鉄イオン含有液から鉄イオンを効率
的に除去する方法として、「鉄イオン含有液と、一級〜
四級アミンの少なくとも1種を含む抽出剤とを接触させ
た後、抽出剤を亜二チオン酸塩と接触させて鉄イオンを
逆抽出することを特徴とする鉄イオン含有液の処理方法
。」を先に特許出願した(特願昭60−168340、
以下「先願」という。)。That is, as a method for efficiently removing iron ions from an iron ion-containing liquid, the applicant has developed a method for efficiently removing iron ions from an iron ion-containing liquid.
A method for treating a liquid containing iron ions, which comprises contacting the liquid with an extractant containing at least one type of quaternary amine, and then contacting the extractant with a dithionite salt to back-extract iron ions. ” (Japanese Patent Application No. 168340-1983)
Hereinafter referred to as "prior application". ).
上記先願の方法によれば、鉄イオン含有液から、鉄イオ
ンを極めて高効率で除去することが可能とされるが、抽
出を長時間継続して行うと、抽出剤中に鉄を含むSSが
蓄積し、膜を介した抽出の場合には、膜にそのSSが付
着することが判明した。また、膜を介さない場合につい
ても、エマルジョン化により抽出効率が悪くなるおそれ
があった。According to the method of the above-mentioned prior application, iron ions can be removed from iron ion-containing liquids with extremely high efficiency. However, if extraction is continued for a long time, SS containing iron in the extractant may It was found that the SS accumulates and, in the case of extraction through the membrane, the SS is deposited on the membrane. Furthermore, even in the case where no membrane is used, there is a risk that the extraction efficiency will deteriorate due to emulsification.
木発明者らは、このような問題点を解決すべく、逆抽出
剤のpHについて主に検討を重ねた結果、Fe”c7)
溶解するpH1即ち、pH3,5以下にするとSSの蓄
積が殆どなく、膜への付着もないことを知見し、本発明
を完成させた。In order to solve these problems, the wood inventors mainly studied the pH of the back-extracting agent, and found that
The present invention was completed based on the finding that when the pH at which SS is dissolved is 1, that is, pH 3.5 or lower, there is almost no accumulation of SS and no adhesion to the membrane.
以下に本発明を図面を参照して詳細に説明する。The present invention will be explained in detail below with reference to the drawings.
第1図は本発明の処理方法に従って、鉄イオン含有液と
して電気亜鉛メッキ浴液の抽出及び逆抽出を各々独立し
た装置で行う例を示す系統図である。FIG. 1 is a system diagram showing an example in which extraction and back-extraction of an electrolytic galvanizing bath solution as an iron ion-containing solution are performed using independent devices, respectively, according to the treatment method of the present invention.
本例においては、まず電解亜鉛メッキ浴1から排出され
る鉄イオンを含むメッキ浴液を、配管6により固体膜2
で仕切られた抽出装置3の抽料室3aに送給し、抽出剤
室3bの一級〜四級アミンの少なくとも1種を含む抽出
剤と固体膜2を介して接触させる。In this example, the plating bath solution containing iron ions discharged from the electrolytic galvanizing bath 1 is first transferred to the solid film 2 through the pipe 6.
The extractant is fed to the extraction chamber 3a of the extraction device 3 partitioned by 1, and brought into contact with the extractant containing at least one of primary to quaternary amines in the extractant chamber 3b via the solid membrane 2.
この抽出処理において、抽料であるメッキ浴液のpHが
3以上であると沈殿物が析出して固体膜に付着し抽出効
率を低下させることがある。このため、処理するメッキ
浴液のpHは3未満とするのが好ましい。In this extraction process, if the pH of the plating bath solution, which is the extraction material, is 3 or higher, precipitates may precipitate and adhere to the solid membrane, reducing extraction efficiency. For this reason, the pH of the plating bath solution to be treated is preferably less than 3.
本発明において、用いる抽出剤は、第一級〜第四級アミ
ンの少なくとも1種を石油系炭化水素等の希釈剤で、ア
ミン濃度1〜80重量%程度に調整したものが好適であ
る。In the present invention, the extractant used is preferably one in which at least one of primary to quaternary amines is adjusted to an amine concentration of about 1 to 80% by weight using a diluent such as a petroleum hydrocarbon.
使用される第一級〜第四級アミンの好適な具体例として
は、tert−アイコシルアミン、1−(3−エチルペ
ンチル)−4−エチルオクチルアミン、1,1,3.3
−テトラメチルブチルアミン、ラウリルアミン等の一級
アミン;ジー(2−エチルヘキシル)アミン、ジラウリ
ルアミン、3.3,5,5,7.7−へキサメチルオク
チルアミン等の二級アミンニトリヘキシルアミン、トリ
オクチルアミン、トリイソオクチルアミン、トリラウリ
ルアミン、ジメチルラウリルアミン、ジメチルヘキサデ
シルアミン、メチルジ(トリデシル)アミン、ジメチル
オレイルアミン、ジメチルココアミン、トリカプリリル
アミン、トリデシルアミン、ジラウリルベンジルアミン
等の三級アミン;メチルトリオクチルアミンモニウムク
ロライド、ジメチルジラウリルアンモニウムクロライド
、トリメチルデシルアンモニウムクロライド等の四級ア
ミンが挙げられる。Preferred specific examples of primary to quaternary amines used include tert-icosylamine, 1-(3-ethylpentyl)-4-ethyloctylamine, 1,1,3.3
- Primary amines such as tetramethylbutylamine and laurylamine; secondary amines such as di(2-ethylhexyl)amine, dilaurylamine, 3.3,5,5,7.7-hexamethyloctylamine, nitrihexylamine, Trioctylamine, triisooctylamine, trilaurylamine, dimethyllaurylamine, dimethylhexadecylamine, methyldi(tridecyl)amine, dimethyloleylamine, dimethylcocoamine, tricaprylylamine, tridecylamine, dilaurylbenzylamine, etc. Quaternary amines include quaternary amines such as methyltrioctylaminemonium chloride, dimethyldilauryl ammonium chloride, and trimethyldecylammonium chloride.
メッキ浴液中の鉄イオンは、抽出装置3における抽出に
より、抽出剤に抽出されて除去される。The iron ions in the plating bath liquid are extracted by the extractant and removed by the extraction device 3.
鉄イオンが除去されたメッキ浴液(抽残液)は、配管7
により電解亜鉛メッキ浴lに返送され、再使用される。The plating bath liquid (raffinate liquid) from which iron ions have been removed is transferred to piping 7.
It is returned to the electrolytic galvanizing bath 1 and reused.
即ち、抽出処理されたメッキ浴液を電解亜鉛メッキ浴で
再使用する場合、メッキ浴中に抽出剤が混入して含有さ
れていると不都合が起こる。しかるに、第1図に示す装
置においては、抽出剤損失の少ない固体膜接触方式で抽
出を行うため、抽残液のメッキ浴液中への抽出剤の混入
が殆どなく、′メッキ浴液の再使用が可能となる。That is, when an extracted plating bath solution is reused in an electrolytic galvanizing bath, problems may occur if the plating bath contains an extractant. However, in the apparatus shown in Figure 1, extraction is carried out using a solid membrane contact method with little loss of extractant, so there is almost no extraction agent mixed into the plating bath liquid from the raffinate solution, and the plating bath liquid is not recycled. It becomes possible to use it.
抽出装置3の固体膜2としては、平膜型、チューブラ−
型、ホロファイバー型等、各種の形態のものが用いられ
る。The solid membrane 2 of the extraction device 3 may be a flat membrane type or a tubular type.
Various forms are used, such as a mold and a holofiber type.
また、固体膜は多孔質のものであれば良く、例えばポリ
テトラフルオロエチレン(以下rPTFE」という)、
酢酸セルロース、ポリスルホン、ポリ塩化ビニル、ポリ
プロピレン、ポリアミド等の半透膜が挙げられるが、特
にPTFEが好ましい。一般にPTFEは耐薬品性、疎
水性に優れ、また抽出速度も極めて高く、固体膜として
採用するに好適な性質を備える。多孔質PTFE膜は、
使用する抽出剤等によって、その膜厚、孔径等を選定す
る。The solid membrane may be porous, such as polytetrafluoroethylene (hereinafter referred to as "rPTFE"),
Semipermeable membranes such as cellulose acetate, polysulfone, polyvinyl chloride, polypropylene, and polyamide may be used, but PTFE is particularly preferred. In general, PTFE has excellent chemical resistance and hydrophobicity, and also has an extremely high extraction rate, making it suitable for use as a solid membrane. Porous PTFE membrane is
The membrane thickness, pore size, etc. are selected depending on the extractant used.
なお、PTFE固体膜の抽出速度が速い理由は明らかで
ないが、その網目状構造や極端な疎水性(親油性)によ
り、抽料と抽剤との接触部が孔だけでなく、膜面全体に
わたることとなり、膜内における拡散も速いためと推定
される。It is not clear why the extraction rate of the PTFE solid membrane is so fast, but due to its network structure and extreme hydrophobicity (lipophilicity), the contact area between the extractant and the extraction agent is not limited to the pores, but covers the entire membrane surface. This is presumed to be due to fast diffusion within the film.
第1図においては、抽料(即ち、メッキ浴液)と抽出剤
とを固体膜を介して接触させる方式の抽出装置を示した
が、本発明においては、ミキサー・セトラー型、スプレ
ー塔等の抽料と抽出剤が直接接触する抽出方式を採用し
ても良い。しかしながら、前述の如く、抽残液の再使用
の面からは、固体膜接触方式とするのが好ましい。Although FIG. 1 shows an extraction device in which the extraction material (i.e., plating bath liquid) and the extractant are brought into contact with each other through a solid membrane, in the present invention, a mixer-settler type, a spray tower, etc. An extraction method in which the extraction material and the extractant are brought into direct contact may also be adopted. However, as mentioned above, from the viewpoint of reusing the raffinate, it is preferable to use the solid membrane contact method.
抽出装置3において鉄イオンを抽出した抽出剤は、これ
を配管8により逆抽出装置4に送給し、還元剤を含む逆
抽出剤とpH3,5以下で接触させて逆抽出を行う。The extractant from which iron ions have been extracted in the extraction device 3 is sent to the back extraction device 4 through a pipe 8, and brought into contact with a back extraction agent containing a reducing agent at a pH of 3.5 or lower to perform back extraction.
本発明において、還元剤としては、亜二チオン酸ナトリ
ウム、亜二チオン酸カリウム、亜二チオン酸アンモニウ
ム等の亜二チオン酸塩等が還元力が強いことが好ましい
が、その他亜硫酸塩等の他の還元剤も使用可能である。In the present invention, as the reducing agent, it is preferable that dithionite salts such as sodium dithionite, potassium dithionite, and ammonium dithionite have a strong reducing power, but other salts such as sulfites, etc. Reducing agents can also be used.
なお、還元剤として、亜二チオン酸塩を用いる場合、亜
二チオン酸塩は低PHで分解し易いことから、これを逆
抽出初期に逆抽出剤中に高濃度添加しておくのは好まし
くなく、ORP制御あるいは定量注入方式で定期的に少
量ずつ添加するのが好ましい。In addition, when dithionite is used as a reducing agent, it is preferable to add it at a high concentration to the back-extracting agent at the beginning of back-extraction because dithionite is easily decomposed at low pH. Rather, it is preferable to periodically add small amounts using ORP control or a metered injection method.
逆抽出装置4における逆抽出剤と抽出剤との接触は、固
体膜を介して行っても良く、固体膜を介さず直接接触さ
せても良い。一般に固体膜を介して接触させればエマル
ジョン化等が防止され良好な抽出が実施でき、また固体
膜を介さずに直接接触させる場合には抽出速度が速く、
固体膜への結晶付着等の可能性がないという利点がある
。The back extractant and the extractant may be brought into contact with each other in the back extraction device 4 through a solid membrane, or may be brought into direct contact without going through a solid membrane. In general, if the contact is made through a solid membrane, emulsification etc. can be prevented and good extraction can be carried out, and if the contact is made directly without going through a solid membrane, the extraction speed is fast.
There is an advantage that there is no possibility of crystal attachment to the solid film.
逆抽出後の抽出剤は、廃液処理又は省資源の面から、可
能な限り循環再使用するのが好ましいが、本発明の方法
においては、逆抽出後の抽出剤は、配管9より必要に応
じてアルカリ洗浄塔5で処理し、配管11を経て抽出装
置3に直接循環して再使′用することができる。It is preferable to recycle and reuse the extractant after back extraction as much as possible from the viewpoint of waste liquid treatment or resource saving. It can then be treated in the alkaline washing tower 5, and then directly circulated to the extraction device 3 via piping 11 for reuse.
一方、逆抽出剤を配管13により循環使用することによ
り、逆抽出された鉄イオンは逆抽出剤中に高濃縮される
。この場合、鉄イオンは第1鉄塩の結晶物として、逆抽
出剤中から晶析回収することも可能である(第1図の配
管15)。このようにすることにより、特公昭57−2
7960に開示されているイオン交換樹脂による処理方
法における、イオン交換樹脂の厚生廃液に相当する、逆
抽出剤液量は極めて少量で足り、廃液処理等の問題も解
消される。On the other hand, by circulating the back-extracting agent through the pipe 13, the back-extracted iron ions are highly concentrated in the back-extracting agent. In this case, iron ions can be crystallized and recovered from the back-extracting agent as ferrous salt crystals (piping 15 in FIG. 1). By doing this, the Tokuko Sho 57-2
In the treatment method using an ion exchange resin disclosed in No. 7960, an extremely small amount of the back extractant liquid corresponding to the welfare waste liquid of the ion exchange resin is sufficient, and problems such as waste liquid treatment are also solved.
なお、前述の如く、本発明において、逆抽出はpH3,
5以下で行うが、このpH調整には通常の酸あるいは場
合によりアルカリが使用できる。In addition, as mentioned above, in the present invention, back extraction is performed at pH 3,
This pH adjustment is carried out at a pH of 5 or less, and a common acid or, if necessary, an alkali can be used for this pH adjustment.
また、逆抽出剤中に亜鉛を共存させた場合には、逆抽出
された鉄が亜鉛と反応して沈殿を生成し、逆抽出剤から
の鉄分の晶析回収がより容易となることから、本発明の
方法は電気亜鉛メッキ浴液のように鉄分と亜鉛分との両
方を含む液の処理の特に有効である。しかしながら、亜
鉛分を含有しない液であっても、逆抽出剤中に別途亜鉛
塩を添加することにより、晶析回収を有利に行うことが
可能である。In addition, when zinc is present in the back-extracting agent, the back-extracted iron reacts with the zinc to form a precipitate, making it easier to crystallize and recover iron from the back-extracting agent. The method of the present invention is particularly effective in treating solutions containing both iron and zinc, such as electrogalvanizing bath solutions. However, even if the liquid does not contain zinc, it is possible to advantageously perform crystallization and recovery by separately adding a zinc salt to the back-extracting agent.
本発明の方法で処理対象となる鉄イオン含有液としては
、ステンレス酸洗廃水、鋼板製造廃水、電気予熱器洗浄
廃水等が挙げられる。また、鉄イオン及び亜鉛イオンを
含有する液としては、前記した電気亜鉛メッキ浴液の他
、亜鉛調湿式冶金廃液等が挙げられる。Examples of the iron ion-containing liquid to be treated in the method of the present invention include stainless steel pickling wastewater, steel plate manufacturing wastewater, electric preheater cleaning wastewater, and the like. In addition, examples of the liquid containing iron ions and zinc ions include the electrolytic galvanizing bath liquid described above, a zinc moisture control type metallurgical waste liquid, and the like.
以上は、本発明の方法を、独立した別個の抽出装置及び
逆抽出装置を用いて実施する場合について説明したが、
本発明の方法は、抽出機能及び逆抽出機能を兼備した三
液層タイプの装置を用いても、容易に実施し得る。The above describes the case where the method of the present invention is implemented using an independent and separate extractor and back-extractor.
The method of the present invention can be easily carried out using a three-liquid layer type device that has both an extraction function and a back extraction function.
[作用]
鉄イオン含有液を一級〜四級アミンの少なくとも1種を
含む抽出剤で抽出処理することにより、液中の鉄イオン
を効率良く除去することができる。[Function] By extracting the iron ion-containing liquid with an extractant containing at least one of primary to quaternary amines, iron ions in the liquid can be efficiently removed.
また、抽出剤を亜二千オン酸塩等の還元剤により逆抽出
することにより、抽出剤中の第2鉄イオンは還元されて
第1鉄イオンとなり、逆抽出が容易となるため高い逆抽
出速度で逆抽出される。In addition, by back-extracting the extractant with a reducing agent such as dithionite, the ferric ions in the extractant are reduced to ferrous ions, making back-extraction easier and increasing the back-extraction rate. Back-extracted at speed.
しかして、この逆抽出剤のpHが3.5以下であると、
鉄イオンは第2鉄イオンになり難く、第2鉄イオンとな
っても、溶解するためSS源とならないので、抽出剤中
の鉄を含むSSの蓄積が防止され、SSの膜への付着、
エマルジョン化等により長期運転が阻害されることがな
い。However, if the pH of this back extractant is 3.5 or less,
Iron ions are difficult to turn into ferric ions, and even if they become ferric ions, they dissolve and do not become a source of SS. This prevents the accumulation of iron-containing SS in the extractant, and prevents SS from adhering to the membrane.
Long-term operation is not hindered by emulsification etc.
このため、抽出剤を再び抽出工程に循環使用して長期間
安定に継続処理することが可能となる。Therefore, it is possible to recirculate the extractant in the extraction process and continue the process stably for a long period of time.
逆抽出剤中に逆抽出された第1鉄イオンは容易に晶析回
収することが可能である。The ferrous ions back-extracted into the back-extracting agent can be easily crystallized and recovered.
[実施例コ
以下に本発明を実施例及び比較例により更に具体的に説
明するが、本発明はその要旨を超えない限り、以下の実
施例に限定されるものではない。[Examples] The present invention will be explained in more detail below using Examples and Comparative Examples, but the present invention is not limited to the following Examples unless the gist thereof is exceeded.
実施例I
lFe3250pp、ZZn37400ppを含むpH
2,1の電気亜鉛メッキ浴液を、第1図に示す装置を用
いて、本発明の方法に従って、抽出処理した。Example I pH containing 3250pp of lFe, 37400pp of ZZn
EXAMPLE 2.1 Electrolytic galvanizing bath liquid was subjected to extraction treatment according to the method of the present invention using the apparatus shown in FIG.
抽出装置3の固体膜2としては、面積150cm’のポ
リテトラフルオロエチレン製膜を用い、この固体膜2を
介して、抽料室3aにメッキ浴1のメッキ浴液を配管6
を経て1500m見/m i nで通液し、抽出剤室3
bにトリーn−オクチルアミンを40vou%含むケロ
シン液1.05文を3000’m文/ m i nで通
液させた。抽出剤は配管8により逆抽出剤1.6文が循
環通液されている逆抽出装置4に200mu/minの
流量で送給した。A polytetrafluoroethylene membrane with an area of 150 cm' is used as the solid membrane 2 of the extraction device 3, and the plating bath liquid of the plating bath 1 is supplied to the extraction chamber 3a through the piping 6.
The liquid is passed through the extractant chamber 3 at a rate of 1,500m/min.
1.05 ml of kerosene solution containing 40 vol% of tri-n-octylamine was passed through b at a rate of 3000 m ml/min. The extractant was fed at a flow rate of 200 mu/min to the back extractor 4 through which 1.6 mt of back extractant was circulated through a pipe 8.
なお、この逆抽出剤は蒸留水にNA35204 、Na
OH及びH2SO4を添加すルコトニより、pH3,0
〜3.5.0RP−280〜−320mVに調節制御し
て、処理を行った。Note that this back-extracting agent contains NA35204 and Na in distilled water.
From Rucotoni adding OH and H2SO4, pH 3,0
The treatment was carried out under adjustment control at ~3.5.0 RP -280 to -320 mV.
その結果、メッキ浴液からの鉄イオンの抽出速度は8.
9g−Fe/m’−hr程度に維持され、50時間継続
処理後においても膜へのSSの析出付着は生じなかった
。As a result, the extraction rate of iron ions from the plating bath solution was 8.
The temperature was maintained at about 9 g-Fe/m'-hr, and no SS deposition occurred on the membrane even after continuous treatment for 50 hours.
実施例2
逆抽出剤の還元剤としてN a 2 S O3を用い、
0RP300〜310mV (実施例1におけるN a
2 S 204の添加重量とほぼ同程度の添加量とな
る値)に調節したこと以外は、実施例1と同様にして処
理を行った。Example 2 Using N a 2 S O3 as the reducing agent of the back extractant,
0RP300-310mV (Na in Example 1
The treatment was carried out in the same manner as in Example 1, except that the added amount was adjusted to a value that was approximately the same as the added weight of 2S 204.
その結果、メッキ浴液からの鉄イオンの抽出速度は8.
8g−Fe/rn’・hr程度に維持され、50時間継
続処理後においても膜へのSSの析出付着は生じなかづ
た。As a result, the extraction rate of iron ions from the plating bath solution was 8.
The temperature was maintained at approximately 8 g-Fe/rn'·hr, and no SS precipitation adhered to the film even after continuous treatment for 50 hours.
比較例1
逆抽出剤トL テ100 g / l N a 2 S
204を用い、pH5,8〜5.9に調節したこと以
外は、実施例1と同様にして処理を行った。Comparative Example 1 Reverse extractant 100 g/l Na2S
The treatment was carried out in the same manner as in Example 1, except that 204 was used and the pH was adjusted to 5.8 to 5.9.
その結果、メッキ浴液からの鉄イオンの初期抽出速度は
、8.8g−Fe/ゴ・hr程度であったが、抽出開始
20時間後あたりから膜にSSが付着し始め、徐々に抽
出速度が低下した。As a result, the initial extraction rate of iron ions from the plating bath solution was approximately 8.8 g-Fe/g-hr, but from around 20 hours after the start of extraction, SS began to adhere to the membrane, and the extraction rate gradually increased. decreased.
上記実施例及び比較例の結果から、本発明の方法によれ
ば、長期間安定かつ高効率で継続処理を行うことができ
ることが明らかである。From the results of the above Examples and Comparative Examples, it is clear that according to the method of the present invention, continuous treatment can be performed stably and with high efficiency over a long period of time.
[発明の効果]
以上詳述した通り、本発明の鉄イオン含有液の処理方法
は、鉄イオン含有液を一級〜四級アミンの少なくとも1
種を含む抽出剤と接触させ、また抽出後の抽出剤をpH
3,5以下で還元剤を含む逆抽出剤で逆抽出するもので
あって、
■ 鉄イオン含有液中の鉄イオンを極めて効率良く除去
することができる。[Effects of the Invention] As detailed above, the method for treating an iron ion-containing liquid of the present invention provides a method for treating an iron ion-containing liquid by treating the iron ion-containing liquid with at least one of primary to quaternary amines.
contact with an extractant containing seeds, and also adjust the pH of the extractant after extraction.
This method performs back extraction with a back extraction agent containing a reducing agent with a molecular weight of 3.5 or less, and (1) iron ions in an iron ion-containing liquid can be removed extremely efficiently.
■ 高い逆抽出効率で鉄イオンを逆抽出することができ
る。■ Iron ions can be back-extracted with high back-extraction efficiency.
■ このため抽出剤を循環使用することが可能となる。■ This makes it possible to recycle the extractant.
■ 廃液処理すべき廃液量が極めて少ない。■ The amount of waste liquid to be treated is extremely small.
等の利点を有する上に、
■ 抽出剤中のSSの蓄積が防止されるため、膜へのS
S付着あるいはエマルジョン化が生起することがなく、
効率的な抽出を長期間安定に継続して行うことが可能と
なる。In addition, it has the following advantages: ■ It prevents the accumulation of SS in the extractant, reducing the amount of S on the membrane.
No S adhesion or emulsification occurs,
It becomes possible to perform efficient extraction stably and continuously for a long period of time.
という効果が奏され、工業的、経済的に極めて有利であ
る。This effect is produced and it is extremely advantageous industrially and economically.
第1図は本発明方法を説明する系統図である。
■・・・電気亜鉛メッキ浴、 2・・・固体膜、3・・
・抽出装置、 4・・・逆抽出装置。FIG. 1 is a system diagram illustrating the method of the present invention. ■...Electrogalvanizing bath, 2...Solid film, 3...
・Extraction device, 4... Reverse extraction device.
Claims (4)
も1種を含む抽出剤とを接触させた後、抽出剤をpH3
.5以下で還元剤を含む逆抽出剤と接触させて鉄イオン
を逆抽出することを特徴とする鉄イオン含有液の処理方
法。(1) After bringing the iron ion-containing liquid into contact with an extractant containing at least one of primary to quaternary amines, the extractant is adjusted to pH 3.
.. A method for treating an iron ion-containing liquid, the method comprising back-extracting iron ions by bringing the liquid into contact with a back-extracting agent containing a reducing agent at a concentration of 5 or less.
て行うことを特徴とする特許請求の範囲第1項に記載の
処理方法。(2) The treatment method according to claim 1, wherein the iron ion-containing liquid and the extractant are brought into contact through a solid membrane.
を特徴とする特許請求の範囲第1項又は第2項に記載の
処理方法。(3) The treatment method according to claim 1 or 2, wherein the iron ion-containing liquid is an electrogalvanizing bath liquid.
特許請求の範囲第1項ないし第3項のいずれか1項に記
載の処理方法。(4) The treatment method according to any one of claims 1 to 3, wherein the reducing agent is a dithionite salt.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP8955286A JPS62247884A (en) | 1986-04-18 | 1986-04-18 | Treatment of iron ion-containing liquid |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP8955286A JPS62247884A (en) | 1986-04-18 | 1986-04-18 | Treatment of iron ion-containing liquid |
Publications (1)
Publication Number | Publication Date |
---|---|
JPS62247884A true JPS62247884A (en) | 1987-10-28 |
Family
ID=13973985
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP8955286A Pending JPS62247884A (en) | 1986-04-18 | 1986-04-18 | Treatment of iron ion-containing liquid |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS62247884A (en) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10507406A (en) * | 1994-10-22 | 1998-07-21 | セントラル リサーチ ラボラトリーズ リミティド | Method and apparatus for diffusion transfer between immiscible fluids |
JPH10507962A (en) * | 1994-10-22 | 1998-08-04 | セントラル リサーチ ラボラトリーズ リミティド | Method and apparatus for diffusion transfer between immiscible fluids |
JP2005007352A (en) * | 2003-06-20 | 2005-01-13 | Sharp Corp | Separation method, separation device and detection device for particle |
JP2008070121A (en) * | 2006-09-12 | 2008-03-27 | Miura Co Ltd | Quantitative determination method of iron |
CN103922528A (en) * | 2014-03-21 | 2014-07-16 | 浙江华海药业股份有限公司 | Method for processing valsartan waste water |
CN115231647A (en) * | 2022-07-27 | 2022-10-25 | 赣州步莱铽新资源有限公司 | Recovery method of back extraction waste acid |
-
1986
- 1986-04-18 JP JP8955286A patent/JPS62247884A/en active Pending
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10507406A (en) * | 1994-10-22 | 1998-07-21 | セントラル リサーチ ラボラトリーズ リミティド | Method and apparatus for diffusion transfer between immiscible fluids |
JPH10507962A (en) * | 1994-10-22 | 1998-08-04 | セントラル リサーチ ラボラトリーズ リミティド | Method and apparatus for diffusion transfer between immiscible fluids |
JP2005007352A (en) * | 2003-06-20 | 2005-01-13 | Sharp Corp | Separation method, separation device and detection device for particle |
JP2008070121A (en) * | 2006-09-12 | 2008-03-27 | Miura Co Ltd | Quantitative determination method of iron |
CN103922528A (en) * | 2014-03-21 | 2014-07-16 | 浙江华海药业股份有限公司 | Method for processing valsartan waste water |
CN103922528B (en) * | 2014-03-21 | 2019-07-02 | 浙江华海药业股份有限公司 | A kind of method of Valsartan wastewater treatment |
CN115231647A (en) * | 2022-07-27 | 2022-10-25 | 赣州步莱铽新资源有限公司 | Recovery method of back extraction waste acid |
CN115231647B (en) * | 2022-07-27 | 2023-08-15 | 赣州步莱铽新资源有限公司 | Method for recycling back-extraction waste acid |
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