JP2002266038A - Zinc separation method - Google Patents
Zinc separation methodInfo
- Publication number
- JP2002266038A JP2002266038A JP2001068119A JP2001068119A JP2002266038A JP 2002266038 A JP2002266038 A JP 2002266038A JP 2001068119 A JP2001068119 A JP 2001068119A JP 2001068119 A JP2001068119 A JP 2001068119A JP 2002266038 A JP2002266038 A JP 2002266038A
- Authority
- JP
- Japan
- Prior art keywords
- zinc
- copper
- halogen
- solution
- solvent extraction
- 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.)
- Granted
Links
- 239000011701 zinc Substances 0.000 title claims abstract description 60
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 57
- 238000000926 separation method Methods 0.000 title claims abstract 3
- 239000010949 copper Substances 0.000 claims abstract description 43
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 38
- 229910052802 copper Inorganic materials 0.000 claims abstract description 36
- 238000000034 method Methods 0.000 claims abstract description 29
- 229910052736 halogen Inorganic materials 0.000 claims abstract description 16
- 150000002367 halogens Chemical class 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000000638 solvent extraction Methods 0.000 claims abstract description 13
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 8
- 230000002378 acidificating effect Effects 0.000 claims abstract description 5
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 4
- 239000003960 organic solvent Substances 0.000 claims abstract description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 8
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 5
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 101100123313 Mus musculus H1.8 gene Proteins 0.000 abstract 1
- 238000000605 extraction Methods 0.000 description 13
- 239000000243 solution Substances 0.000 description 12
- 229910021591 Copper(I) chloride Inorganic materials 0.000 description 10
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 8
- 238000002386 leaching Methods 0.000 description 6
- 239000000460 chlorine Substances 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005363 electrowinning Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000012074 organic phase Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 2
- 229960001763 zinc sulfate Drugs 0.000 description 2
- 229910000368 zinc sulfate Inorganic materials 0.000 description 2
- ZDFBXXSHBTVQMB-UHFFFAOYSA-N 2-ethylhexoxy(2-ethylhexyl)phosphinic acid Chemical compound CCCCC(CC)COP(O)(=O)CC(CC)CCCC ZDFBXXSHBTVQMB-UHFFFAOYSA-N 0.000 description 1
- -1 2-ethylhexyl Chemical group 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- UTYSTRPOWXHXKX-UHFFFAOYSA-N didecan-2-yl hydrogen phosphate Chemical compound CCCCCCCCC(C)OP(O)(=O)OC(C)CCCCCCCC UTYSTRPOWXHXKX-UHFFFAOYSA-N 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000012085 test solution Substances 0.000 description 1
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Extraction Or Liquid Replacement (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
(57)【要約】
【課題】銅及び亜鉛を含んだハロゲン系液から亜鉛を分
離する方法を提供することを目的とする。
【解決手段】 銅、亜鉛を含むハロゲン系液と有機りん
酸系酸性抽出剤を接触させ溶媒抽出処理を行なう方法に
おいて、対象処理液中の２価の銅を予め１価に還元し、
その後還元処理液を不活性雰囲気下で、２５℃以上、ｐ
Ｈ１．８〜５．６の条件下で溶媒抽出することにより、
ハロゲン系液の亜鉛を有機溶媒中に移行させ銅と亜鉛を
分離する、亜鉛の分離方法。
(57) [Object] To provide a method for separating zinc from a halogen-based solution containing copper and zinc. SOLUTION: In a method of performing a solvent extraction treatment by bringing a halogen-based solution containing copper and zinc into contact with an organic phosphoric acid-based acidic extractant, divalent copper in a target treatment solution is reduced to monovalent in advance,
Then, the reduction treatment liquid is heated at 25 ° C.
By solvent extraction under the conditions of H1.8 to 5.6,
A zinc separation method in which zinc in a halogen-based liquid is transferred into an organic solvent to separate copper and zinc.
Description
【０００１】[0001]
【産業上の利用分野】本発明は、 主に銅、亜鉛を含む
ハロゲン系液から亜鉛を分離回収する方法に関するもの
であり、更に詳しく述べると有価物である亜鉛を銅等と
湿式処理により分離し回収する方法に関するものであ
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for separating and recovering zinc from a halogen-based liquid containing mainly copper and zinc. More specifically, the present invention relates to a method of separating valuable zinc from copper and the like by wet treatment. And methods for collecting.
【０００２】[0002]
【従来の技術】一般的に難溶性塩類の溶解度は、共存す
るイオンにより著しく変化する。例えば塩化物浴でのＣ
ｕＣｌの溶解度を考えると、その溶解度は塩素イオン濃
度により変化する。このとき塩素イオン濃度の増加と共
にＣｕＣｌ溶解度も増加する。これはＣｌ錯体を形成す
るためであり、例えばＣｕＣｌ２−、ＣｕＣｌ３ ２−の
ような錯体が形成される。2. Description of the Related Art Generally, the solubility of sparingly soluble salts is significantly changed by coexisting ions. For example, C in a chloride bath
Considering the solubility of uCl, its solubility varies depending on the chloride ion concentration. At this time, the solubility of CuCl increases with an increase in the chloride ion concentration. This is to form a Cl complex, for example, a complex such as CuCl 2− and CuCl 3 2− is formed.
【０００３】このように錯体を形成する場合、難溶性塩
類の溶解度が増加する場合があるため、この性質を利用
した浸出がしばしば行われる。しかしながら、浸出目的
成分以外の溶解度も増加する場合があり、浸出液中の不
純物濃度も増大する。このため、不純物成分を除去する
ことが望まれている。[0003] When a complex is formed in this manner, the solubility of a poorly soluble salt may increase, and leaching utilizing this property is often performed. However, the solubility other than the leaching target component may also increase, and the impurity concentration in the leaching solution also increases. For this reason, it is desired to remove impurity components.
【０００４】塩素濃度４から５モル／Lの塩化物浴で
は、銅（１価）はＣｕＣｌ２−やＣｕＣｌ３ ２−の形
で、亜鉛はＺｎＣｌ３ −やＺｎＣｌ４ ２−の形で存在し
ている考えられる。この液から亜鉛を除去する方法とし
て中和法や還元法が考えられるが、中和法では低いｐＨ
で銅が先に沈殿するため好ましくなく、還元法でも銅が
先に還元されるため、亜鉛のみの除去は困難である。し
たがって、新規な亜鉛除去法の開発が望まれている。In a chloride bath having a chlorine concentration of 4 to 5 mol / L, copper (monovalent) exists in the form of CuCl 2− and CuCl 3 2− , and zinc exists in the form of ZnCl 3 − and ZnCl 4 2−. I think it is. A neutralization method or a reduction method can be considered as a method for removing zinc from this solution.
However, it is not preferable because copper precipitates first, and it is difficult to remove only zinc because copper is reduced first even by a reduction method. Therefore, development of a new zinc removal method is desired.
【０００５】[0005]
【発明が解決しようとする課題】上記問題点を解決す
る、湿式法により銅と亜鉛とを分離する方法を提供する
ものである。SUMMARY OF THE INVENTION An object of the present invention is to provide a method for separating copper and zinc by a wet method, which solves the above problems.
【０００６】[0006]
【課題を解決するための手段】本発明者らは、銅、亜鉛
を含むハロゲン液性からの亜鉛除去の種々の検討を行っ
た結果、分離方法として、 （１）銅、亜鉛を含むハロゲン系液と有機りん酸系酸性
抽出剤を接触させ溶媒抽出処理を行なう方法において、
対象処理液中の２価の銅を予め１価に還元し、その後還
元処理液を不活性雰囲気下で、２５℃以上、ｐＨ１．８
〜５．６の条件下で溶媒抽出することにより、ハロゲン
系液の亜鉛を有機溶媒中に移行させ銅と亜鉛を分離す
る、亜鉛の分離方法。 （２）ハロゲン系液の組成が、塩化ナトリウム２００〜
３５０ｇ／Ｌ、臭化ナトリウム０〜５０ｇ／Ｌである上
記（１）記載の亜鉛の分離方法。を提供するものであ
る。The present inventors have conducted various studies on the removal of zinc from a halogen solution containing copper and zinc. In the method of performing a solvent extraction treatment by contacting the liquid and an organic phosphoric acid acidic extractant,
Divalent copper in the target processing solution is reduced to monovalent in advance, and then the reduced processing solution is subjected to an inert atmosphere at 25 ° C. or higher and pH 1.8.
A method for separating zinc, wherein zinc in a halogen-based liquid is transferred into an organic solvent to separate copper and zinc by solvent extraction under the conditions of ~ 5.6. (2) The composition of the halogen-based liquid is sodium chloride 200 to
The method for separating zinc according to the above (1), wherein 350 g / L and 0 to 50 g / L of sodium bromide are used. Is provided.
【作用】以下本発明の構成を詳しく説明する。なお構成
は例を挙げて説明しているが、本発明はこの例に制限さ
れるものではない。The structure of the present invention will be described below in detail. Although the configuration has been described using an example, the present invention is not limited to this example.
【０００７】一般的に難溶性塩類の溶解度は、共存する
イオンにより著しく変化する。例えば塩化物浴でのＣｕ
Ｃｌの溶解度を考えると、その溶解度は塩素イオン濃度
により変化する。このとき塩素イオン濃度の増加と共に
ＣｕＣｌ溶解度も増加する。これはＣｌ錯体を形成する
ためであり、例えばＣｕＣｌ２−、ＣｕＣｌ３ ２−のよ
うな錯体が形成される。[0007] In general, the solubility of poorly soluble salts is significantly changed by coexisting ions. For example, Cu in chloride bath
Considering the solubility of Cl, the solubility changes depending on the chloride ion concentration. At this time, the solubility of CuCl increases with an increase in the chloride ion concentration. This is to form a Cl complex, for example, a complex such as CuCl 2− and CuCl 3 2− is formed.
【０００８】このように錯体を形成する場合、難溶性塩
類の溶解度が増加する場合があるため、この性質を利用
した浸出がしばしば行われる。しかしながら、浸出目的
成分以外の溶解度も増加する場合があり、浸出液中の不
純物濃度も増大する。このため、不純物成分を除去する
ことが望まれる。[0008] In the case of forming a complex as described above, since the solubility of the hardly soluble salts may increase, leaching utilizing this property is often performed. However, the solubility other than the leaching target component may also increase, and the impurity concentration in the leaching solution also increases. For this reason, it is desired to remove impurity components.
【０００９】塩素濃度４から５モル／Lの塩化物浴で
は、銅はＣｕＣｌ２−やＣｕＣｌ３ ２−の形で、亜鉛は
ＺｎＣｌ３ −やＺｎＣｌ４ ２−の形で存在していると考
えられる。この液から亜鉛を除去する方法として中和法
や還元法が考えられが、中和法では低いｐＨで銅が先に
沈殿するため好ましくなく、還元法でも銅が先に還元さ
れるため、亜鉛のみの除去は困難である。したがって、
新規な亜鉛除去法の開発が望まれている。In a chloride bath having a chlorine concentration of 4 to 5 mol / L, it is considered that copper is present in the form of CuCl 2− or CuCl 3 2− and zinc is present in the form of ZnCl 3 − or ZnCl 4 2−. Can be As a method of removing zinc from this solution, a neutralization method or a reduction method is conceivable. However, the neutralization method is not preferable because copper is precipitated first at a low pH, and the reduction method also reduces copper first. It is difficult to remove only. Therefore,
Development of a new zinc removal method is desired.
【００１０】本発明者らは、銅、亜鉛を含むハロゲン液
性からの亜鉛除去の種々の検討を行った結果、溶媒抽出
法により銅と亜鉛との分離ができるとの知見を得た。The present inventors have conducted various studies on the removal of zinc from a halogen solution containing copper and zinc, and have found that copper and zinc can be separated by a solvent extraction method.
【００１１】即ち、銅（１価）、亜鉛を含むハロゲン系
液性の浸出液に対して、例えば有機りん酸系酸性抽出剤
である商品名ＤＰ−８Ｒ（bis(2-ethylhexyl)phosphori
c acid）、商品名ＤＰ−１０Ｒ（diisodecylphosphoric
acid）や商品名ＰＣ−８８Ａ（2-ethylhexylphosphoni
c acid mono-2-ethyl ester）等で溶媒抽出を行うとＣ
ｕ＋は抽出されず水相中に残り、亜鉛が抽出剤中に移行
する。銅がＣｕ２＋の場合は亜鉛と共に抽出剤中に抽出
されるため、銅と亜鉛の分離が困難となる。特に本発明
でのハロゲン系液の組成が、塩化ナトリウム２００〜３
５０ｇ／Ｌ、臭化ナトリウム０〜５０ｇ／Ｌである液組
成である場合に銅及び亜鉛を含む液の亜鉛の分離方法に
適する方法である。上記の問題を解決する為には、溶媒
抽出前に例えば、銅粉による還元を行い、銅（２価）を
銅（１価）に予め還元しておくこと、さらには溶媒抽出
処理中の銅（１価）から銅（２価）への酸化を防止する
ため、アルゴン等に代表される不活性ガスで封入するこ
とが肝要である。この亜鉛を除去した水相を例えば公知
の方法である電解採取法を適用することによって、高品
質の銅の回収が可能となる。That is, for a halogen-based leachate containing copper (monovalent) and zinc, for example, an organic phosphoric acid-based acidic extractant (trade name: DP-8R (bis (2-ethylhexyl) phosphori))
c acid), trade name DP-10R (diisodecylphosphoric)
acid) and PC-88A (2-ethylhexylphosphoni)
c acid mono-2-ethyl ester)
u + is not extracted and remains in the aqueous phase and zinc migrates into the extractant. When copper is Cu 2+ , it is extracted into the extractant together with zinc, so that it is difficult to separate copper and zinc. In particular, the composition of the halogen-based liquid in the present invention is sodium chloride 200 to 3
When the liquid composition is 50 g / L and sodium bromide is 0 to 50 g / L, this method is suitable for a method for separating zinc from a liquid containing copper and zinc. In order to solve the above-mentioned problem, for example, copper (divalent) is reduced to copper (monovalent) by performing reduction with copper powder before solvent extraction, and further, copper during the solvent extraction treatment is reduced. In order to prevent oxidation from (monovalent) to copper (divalent), it is important to fill with an inert gas represented by argon or the like. By applying, for example, a known method of electrowinning the aqueous phase from which zinc has been removed, high-quality copper can be recovered.
【００１２】抽出剤で抽出された亜鉛は、例えば希硫酸
で逆抽出され硫酸亜鉛溶液となり更に公知の方法である
電解採取等を行うことにより、金属亜鉛としての回収が
可能である。亜鉛を逆抽出した後の抽出剤は再び抽出工
程へ繰返される。The zinc extracted with the extractant is, for example, back-extracted with dilute sulfuric acid to form a zinc sulfate solution, which can be recovered as zinc metal by subjecting it to a known method such as electrowinning. After the zinc has been back-extracted, the extractant is repeated again in the extraction step.
【００１３】酸性抽出剤の溶媒抽出においては、液のｐ
Ｈにより抽出率が異なる。このｐＨを調整するために薬
剤が投入されるが、薬剤コストを最小にするため、表１
に示すように浸出液のｐＨ（０〜６）に近いところで抽
出することが望ましい。抽出ｐＨは１．８〜５．６、さ
らに詳細に述べると２．５から５．６が好ましい。ｐH
が１．８より小さいとZnの抽出率が低く、ｐHが５．６
を超えるとCuの抽出率が上昇してくる。In the solvent extraction of the acidic extractant, p
The extraction rate differs depending on H. Drugs are added to adjust the pH. To minimize the cost of the drugs, Table 1 was used.
It is desirable to extract near the pH (0 to 6) of the leachate as shown in FIG. The extraction pH is preferably from 1.8 to 5.6, more preferably from 2.5 to 5.6. pH
Is less than 1.8, the extraction rate of Zn is low, and the pH is 5.6.
Exceeding the temperature increases the extraction rate of Cu.
【表１】 供試液：Cu(+)75g/L、Zn15g/L、NaCl280g/L、NaBr28g/L 処理条件：25vol％DP-8R、相比＝１、25℃×1hr 雰囲気：Ａｒ封入[Table 1] Test solution: Cu (+) 75 g / L, Zn 15 g / L, NaCl 280 g / L, NaBr 28 g / L Treatment conditions: 25 vol% DP-8R, phase ratio = 1, 25 ° C. × 1 hr Atmosphere: Ar enclosed
【００１４】溶媒抽出の処理時間は、表２に示すように
２時間以内更に詳しく述べると１時間以内が好ましい。
亜鉛の抽出は短時間に行われるため、処理時間が長くて
も亜鉛の抽出率は向上しない。The processing time for the solvent extraction is preferably within 2 hours as shown in Table 2, more preferably within 1 hour.
Since the extraction of zinc is performed in a short time, the extraction rate of zinc does not improve even if the treatment time is long.
【表２】 [Table 2]
【００１５】溶媒抽出処理の液温は表３に示すように25
℃以上が好ましい。液温が高いと、亜鉛の抽出率は高く
なる傾向であるが、熱エネルギーコスト等を考慮する
と、より常温付近での抽出が好ましい。As shown in Table 3, the liquid temperature of the solvent extraction treatment was 25
C. or higher is preferred. If the liquid temperature is high, the extraction rate of zinc tends to be high, but in consideration of thermal energy costs and the like, extraction at around normal temperature is more preferable.
【表３】 [Table 3]
【００１６】抽出剤で抽出された亜鉛は、例えば希硫酸
で逆抽出され硫酸亜鉛溶液となり更に電解採取等を行う
ことにより、金属亜鉛としての回収が可能である。亜鉛
を逆抽出した後の抽出剤は再び抽出工程へ繰返される。The zinc extracted with the extractant is, for example, back-extracted with dilute sulfuric acid to form a zinc sulfate solution, which can be recovered as metallic zinc by subjecting it to electrolytic extraction and the like. After the zinc has been back-extracted, the extractant is repeated again in the extraction step.
【００１７】本発明により、銅、亜鉛を含むハロゲン系
液から、亜鉛を分離回収することが可能となった。According to the present invention, zinc can be separated and recovered from a halogen-based solution containing copper and zinc.
【００１８】以上説明したように、亜鉛と銅とを分離す
る簡便な方法を確立した。As described above, a simple method for separating zinc and copper has been established.
【００１９】以下本発明の実施例を説明する。なお本発
明は実施例に限定されるものではない。Hereinafter, embodiments of the present invention will be described. Note that the present invention is not limited to the embodiments.
【００２０】銅、亜鉛を含むハロゲン系液の組成は、表
４の通りである。Table 4 shows the composition of the halogen-based liquid containing copper and zinc.
【００２１】[0021]
【表４】 [Table 4]
【００２２】この浸出液を溶媒抽出（25vol％DP-8R、25
℃×1hr、相比＝１、平衡pH＝3.17、アルゴン封入）し
た結果、銅と亜鉛の有機相への抽出率は次の表５のよう
になった。This leachate was extracted with a solvent (25 vol% DP-8R, 25 vol.
C. x 1 hr, phase ratio = 1, equilibrium pH = 3.17, argon enclosed). As a result, the extraction rates of copper and zinc into the organic phase were as shown in Table 5 below.
【００２３】[0023]
【表５】 [Table 5]
【００２４】浸出液中のCu（+）をCu（2+）とした以外
は実施例と同様に溶媒抽出した結果、銅と亜鉛の有機相
への抽出率は次の表６のようになった。即ちCu（2+）
は、Znと共に抽出された。Solvent extraction was performed in the same manner as in Example except that Cu (+) in the leachate was changed to Cu (2+). As a result, the extraction rates of copper and zinc into the organic phase were as shown in Table 6 below. . That is, Cu (2+)
Was extracted with Zn.
【表６】 [Table 6]
【００２５】[0025]
【発明の効果】以上説明したように、本発明により銅及
び亜鉛を含むハロゲン系液から亜鉛と銅を分離すること
が可能となった。As described above, according to the present invention, zinc and copper can be separated from a halogen-based solution containing copper and zinc.
【図１】は、本発明の処理フローの一態様を示す。FIG. 1 shows one embodiment of the processing flow of the present invention.
Claims (2)
系酸性抽出剤を接触させ溶媒抽出処理を行なう方法にお
いて、対象処理液中の２価の銅を予め１価に還元し、そ
の後還元処理液を不活性雰囲気下で、２５℃以上、ｐＨ
１．８〜５．６の条件下で溶媒抽出することにより、ハ
ロゲン系液の亜鉛を有機溶媒中に移行させ銅と亜鉛を分
離することを特徴とする、亜鉛の分離方法。In a method of performing a solvent extraction treatment by bringing a halogen-based solution containing copper and zinc into contact with an organic phosphoric acid-based acidic extractant, divalent copper in a target treatment solution is previously reduced to monovalent, Reduce the reducing solution under an inert atmosphere at 25 ° C or higher, pH
A zinc separation method, wherein zinc is separated from copper and zinc by transferring zinc in a halogen-based solution into an organic solvent by solvent extraction under the conditions of 1.8 to 5.6.
００〜３５０ｇ／Ｌ、臭化ナトリウム０〜５０ｇ／Ｌで
あることを特徴とする請求項１記載の亜鉛の分離方法。2. The composition of a halogen-based liquid is sodium chloride 2
The method for separating zinc according to claim 1, wherein the amount is from 0 to 350 g / L and from 0 to 50 g / L of sodium bromide.
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|---|---|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009050334A1 (en) * | 2007-10-16 | 2009-04-23 | Outotec Oyj | Method for the hydrometallurgical processing of sulphidic material containing zinc and copper |
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- 2001-03-12 JP JP2001068119A patent/JP3769201B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009050334A1 (en) * | 2007-10-16 | 2009-04-23 | Outotec Oyj | Method for the hydrometallurgical processing of sulphidic material containing zinc and copper |
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