JPH10140257A - Wet refining method of nickel by chlorine leaching electrolytic extracting method - Google Patents
Wet refining method of nickel by chlorine leaching electrolytic extracting methodInfo
- Publication number
- JPH10140257A JPH10140257A JP8294905A JP29490596A JPH10140257A JP H10140257 A JPH10140257 A JP H10140257A JP 8294905 A JP8294905 A JP 8294905A JP 29490596 A JP29490596 A JP 29490596A JP H10140257 A JPH10140257 A JP H10140257A
- Authority
- JP
- Japan
- Prior art keywords
- chlorine
- nickel
- leaching
- blowing
- air
- 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
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
- Manufacture And Refinement Of Metals (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
Description
【0001】[0001]
【発明の属する技術分野】本発明は、ニッケル、コバル
ト、銅、銅より卑な金属及び硫黄を含むマット、硫化物
精鉱、電解スライムなどから、塩素浸出電解採取法によ
りニッケルを金属として回収するニッケルの湿式精錬方
法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for recovering nickel as a metal from a mat, a sulfide concentrate, an electrolytic slime, and the like containing nickel, cobalt, copper, a metal lower than copper and sulfur by a chlorine leaching electrowinning method. The present invention relates to a method for refining nickel.
【0002】[0002]
【従来の技術】従来、ニッケル、コバルト、銅、銅より
卑な金属及び硫黄を含むマット、硫化物精鉱、及び電解
スライムなどから、ニッケル等の有価金属を回収する方
法の一つに、塩素浸出電解採取法による湿式精錬方法が
ある。2. Description of the Related Art Conventionally, one of the methods for recovering valuable metals such as nickel from nickel, cobalt, copper, mats containing sulfur and sulfur-containing mats, sulfide concentrates, electrolytic slime, and the like, which is lower than copper, is known as chlorine. There is a wet refining method based on leaching electrowinning.
【0003】この塩素浸出電解採取法では、例えば特公
平7−91599号公報に記載されるように、ニッケル
を含有した粉状硫化物を、一価銅イオンを含む塩化物水
溶液と撹拌混合してスラリーとし、このスラリーに塩素
を吹き込むことにより、銅イオンのレドックスカップル
(Cu2+/Cu+)を介在させた固液反応によってニッ
ケルなどの金属を浸出させる。In this chlorine leaching electrowinning method, for example, as described in Japanese Patent Publication No. Hei 7-91599, a powdery sulfide containing nickel is stirred and mixed with a chloride aqueous solution containing monovalent copper ions. By forming a slurry and blowing chlorine into the slurry, a metal such as nickel is leached by a solid-liquid reaction with a redox couple (Cu 2+ / Cu + ) of copper ions interposed.
【0004】上記浸出工程で得られた浸出液は、順次脱
銅電解工程に送り、銅を電解採取して浸出工程に循環さ
せる。また、浸出液の残渣からは硫黄の回収が行われ
る。浸出工程を循環した浸出液は、更に塩素を吹き込み
ながらpHを調節することにより鉄やコバルトなどの不
純物金属を共沈させる浄液工程を経た後、電解により電
気ニッケルを回収する。[0004] The leaching solution obtained in the above leaching step is sequentially sent to a copper removal electrolysis step, where copper is electrolytically collected and circulated to the leaching step. Further, sulfur is recovered from the residue of the leachate. The leach liquor circulated through the leaching step is subjected to a purification step in which impurity metals such as iron and cobalt are coprecipitated by adjusting the pH while further blowing chlorine, and then electronickel is recovered by electrolysis.
【0005】上記電解工程においては、カソード側に目
的金属であるニッケルを電着させて回収することがで
き、アノード側では塩素イオンが酸化されて塩素ガスが
発生する。この電解工程で発生した塩素ガスは回収さ
れ、通常は前記の浸出工程及び浄液工程に循環して再利
用され、この操作が連続して繰り返し行われる。従っ
て、塩素は酸化と還元を繰り返しながら、工程内を循環
する。In the electrolysis step, nickel as a target metal can be recovered by electrodeposition on the cathode side, and chlorine ions are oxidized on the anode side to generate chlorine gas. The chlorine gas generated in this electrolysis step is collected and usually circulated and reused in the leaching step and the liquid purification step, and this operation is continuously and repeatedly performed. Therefore, chlorine circulates in the process while repeating oxidation and reduction.
【0006】このとき、電解工程で発生した塩素ガスの
全量がニッケルのみを浸出するのに使用されるのであれ
ば、塩素は酸化還元を繰り返しながらロスなく工程内を
循環し、電解工程で回収される電気ニッケル量と浸出工
程で浸出されるニッケル量との釣り合いがとれ、連続し
た各工程内のニッケル濃度が一定となる。At this time, if the entire amount of chlorine gas generated in the electrolysis step is used for leaching only nickel, chlorine circulates through the process without loss while repeating oxidation and reduction, and is recovered in the electrolysis step. The amount of electric nickel and the amount of nickel leached in the leaching step are balanced, and the nickel concentration in each successive step becomes constant.
【0007】しかし、実際には塩素はニッケル以外の金
属を浸出したり、浄液工程で不純物金属を酸化したりす
るので、電解工程で発生した塩素ガスのみで浸出工程に
必要な塩素を賄うことはできない。この塩素の不足量
は、原料となるマツトなどの不純物含有量にもよるが、
通常は5%程度、最大で10%程度にまで達するため、
不足の塩素を補うために系外より塩素ガスを補充し、各
工程内のニッケル量を一定に保つ必要がる。However, since chlorine actually leaches metals other than nickel and oxidizes impurity metals in the purification process, it is necessary to supply chlorine necessary for the leaching process only with chlorine gas generated in the electrolytic process. Can not. This chlorine deficiency depends on the content of impurities such as mat, which is the raw material,
Normally, it reaches about 5%, up to about 10%,
In order to compensate for the lack of chlorine, chlorine gas must be replenished from outside the system to keep the amount of nickel in each process constant.
【0008】[0008]
【発明が解決しようとする課題】上記のごとく、塩素浸
出電解採取法によるニッケルの湿式精錬においては、浸
出工程に用いる塩素として電解工程で発生する塩素ガス
を利用できるが、その場合でもロスにより発生する塩素
の不足分を系外から補充し、連続した各工程内のニッケ
ル量を一定に保つ必要があった。As described above, in the wet refining of nickel by the chlorine leaching electrowinning method, chlorine gas generated in the electrolysis step can be used as chlorine used in the leaching step, but even in that case, chlorine gas generated due to loss is used. It was necessary to replenish the shortage of chlorine from outside the system and to keep the amount of nickel in each successive process constant.
【0009】その場合、系外から補充する塩素は、主
に、ボンベに入った液体塩素、食塩電解などから得られ
る塩素ガスなどであり、そのためランニングコストや設
備的な投資が増大してしまうという欠点があった。In this case, the chlorine to be replenished from the outside of the system is mainly liquid chlorine in a cylinder, chlorine gas obtained from salt electrolysis, etc., which increases running costs and equipment investment. There were drawbacks.
【0010】本発明は、このような従来の事情に鑑み、
塩素浸出電解採取法に用いる塩素の一部に代え、例えば
系外から補充する塩素に代えて、安価な空気などのガス
を浸出工程での吹き込みに使用し、経済性を図りつつ、
ニッケル硫化物から効率よくニッケルを浸出して、回収
することができるニッケルの湿式精錬方法を提供するこ
とを目的とする。The present invention has been made in view of such a conventional situation,
In place of chlorine used in the chlorine leaching electrowinning method, for example, in place of chlorine supplemented from outside the system, gas such as inexpensive air is used for blowing in the leaching process, while achieving economic efficiency,
An object of the present invention is to provide a method for refining nickel by which nickel can be efficiently leached from nickel sulfide and recovered.
【0011】[0011]
【課題を解決するための手段】上記目的を達成するた
め、本発明は、ニッケルを含有した粉状硫化物と一価銅
イオンを含む塩化物水溶液とのスラリーに、塩素を吹き
込むことによりニッケルを浸出させる浸出工程と、得ら
れた浸出液の電解によりニッケルを回収する電解工程と
を含む、塩素浸出電解採取法によるニッケルの湿式精錬
方法において、前記塩素吹き込みにより生成された酸の
存在下で、塩素の一部に代えて空気又は酸素富化空気若
しくは工業用酸素を吹き込みながらニッケルを浸出する
ことを特徴とするニッケルの湿式精錬方法を提供するも
のである。In order to achieve the above object, the present invention provides a method for producing nickel by blowing chlorine into a slurry of a powdery sulfide containing nickel and an aqueous chloride solution containing monovalent copper ions. A leaching step of leaching, and an electrolytic step of recovering nickel by electrolysis of the obtained leachate, in a wet refining method of nickel by chlorine leaching electrowinning method, in the presence of the acid generated by the chlorine injection, chlorine The present invention provides a nickel nickel leaching method characterized in that nickel is leached while blowing air, oxygen-enriched air, or industrial oxygen instead of a part of the method.
【0012】特に、前記塩素浸出電解採取法の電解工程
から発生した塩素を浸出工程での塩素吹き込みに循環使
用すると共に、浸出工程での塩素の不足量を空気又は酸
素富化空気若しくは工業用酸素の吹き込みにより補うこ
とを特徴とする。In particular, chlorine generated from the electrolysis step of the above-mentioned chlorine leaching electrowinning method is circulated and used for blowing chlorine in the leaching step, and the chlorine deficiency in the leaching step is determined by air or oxygen-enriched air or industrial oxygen. It is supplemented by blowing.
【0013】尚、本発明において適用可能な原料は、具
体的には、ニッケルを主成分とし、コバルト又は銅の片
方又は両方と、硫黄とを含むニッケルマット、硫化物精
鉱、及び電解スライムなどである。The raw materials applicable in the present invention are, for example, nickel matte containing nickel as a main component, one or both of cobalt and copper, and sulfur, a sulfide concentrate, and electrolytic slime. It is.
【0014】[0014]
【発明の実施の形態】本発明においては、浸出工程で吹
き込む塩素の一部に代えて、空気又は酸素富化空気、若
しくは工業用酸素を使用する。空気中の酸素などが塩素
に代替し得るのは、ニッケル硫化物の浸出反応が以下に
示す酸素の化学的性質と反応機構とによって進行するか
らである。DETAILED DESCRIPTION OF THE INVENTION In the present invention, air or oxygen-enriched air or industrial oxygen is used in place of part of the chlorine blown in the leaching step. The reason that oxygen in the air or the like can substitute for chlorine is that the leaching reaction of nickel sulfide proceeds according to the following chemical properties and reaction mechanism of oxygen.
【0015】空気中の酸素による、酸(H+)の存在下
での、酸化反応と酸化還元電位(25℃)は、下記化学
式1に示す通りである:The oxidation reaction and oxidation-reduction potential (25 ° C.) of oxygen in the air in the presence of an acid (H + ) are as shown in the following chemical formula 1:
【化1】O2+4H++4e-=2H2O E(V)=1.23−0.059pH+0.015logP
O2 よって、例えばpH=0、PO2=0.2atmの場合、
空気中の酸素の酸化還元電位E(V)=1.22である。Embedded image O 2 + 4H + + 4e − = 2H 2 O E (V) = 1.23-0.059 pH + 0.015logP
According to O 2 , for example, when pH = 0 and PO 2 = 0.2 atm,
The oxidation-reduction potential E (V) of oxygen in the air is 1.22.
【0016】一方、ニッケルの浸出に利用される塩素の
酸化反応と酸化還元電位は、下記化学式2の通りであ
る:On the other hand, the oxidation reaction and oxidation-reduction potential of chlorine used for leaching nickel are represented by the following chemical formula 2:
【化2】Cl2+2e-=2Cl-;E(V)=1.36Embedded image Cl 2 + 2e − = 2Cl − ; E (V) = 1.36
【0017】従って、空気中の酸素は、塩素より若干劣
るものの、酸の存在下において高い酸化力を有している
ことが分かる。尚、酸素の酸化力はpHと酸素分圧によ
って変化し、より低いpHである酸性度の高い領域ほ
ど、あるいは、より高い酸素分圧になるほど、高い酸化
還元電位を示す。Accordingly, it can be seen that oxygen in the air has a high oxidizing power in the presence of an acid, although it is slightly inferior to chlorine. Note that the oxidizing power of oxygen changes depending on the pH and the oxygen partial pressure, and the higher the oxygen content, the lower the pH, or the higher the oxygen partial pressure, the higher the oxidation-reduction potential.
【0018】一方、浸出工程において塩素ガスがニッケ
ル硫化物を浸出する反応は、本来固気反応であるが、塩
化浴中に銅イオンのレドックスカップル(Cu2+/Cu
+)を介在させることで、固液反応によってニッケルの
浸出をスムースに行わせることができる。On the other hand, the reaction in which chlorine gas leaches nickel sulfide in the leaching step is essentially a solid-gas reaction, but a redox couple of copper ions (Cu 2+ / Cu
By intervening + ), nickel can be smoothly leached by a solid-liquid reaction.
【0019】即ち、塩素ガスは勿論のこと、pHが0付
近で空気又は酸素を吹き込む際に、1価の銅イオンが存
在すれば、この1価の銅イオンは2価まで酸化される。
酸化された銅イオンCu2+は、ニッケルなどの硫化物に
比べるとまだ酸化力を有するので、このCu2+とニッケ
ル硫化物との固液反応によりニッケル硫化物の浸出が進
行する。That is, when air or oxygen is blown at a pH of about 0 as well as chlorine gas, if monovalent copper ions are present, the monovalent copper ions are oxidized to divalent copper ions.
Since the oxidized copper ions Cu 2+ still have an oxidizing power as compared with sulfides such as nickel, leaching of the nickel sulfide proceeds by a solid-liquid reaction between the Cu 2+ and the nickel sulfide.
【0020】ところで、上記化学式1で示したとおり、
酸素はH+を消費しながら電子を受け取るので、酸素に
よる酸化反応が起こるためには酸が必要である。また、
酸の活量が大きいほど浸出反応が進み易くなる。従っ
て、効率よくニッケルの浸出反応を起こさせるために
は、空気の吹き込みは酸が存在する条件下で行わなけれ
ばならない。Incidentally, as shown in the above chemical formula 1,
Since oxygen receives electrons while consuming H + , an acid is necessary for an oxidation reaction by oxygen to occur. Also,
The greater the activity of the acid, the easier the leaching reaction proceeds. Therefore, in order for the nickel leaching reaction to occur efficiently, air must be blown in the presence of an acid.
【0021】酸素による酸化反応に必要な酸は、別途添
加することも可能であるが、浸出工程での塩素の吹き込
みにより生成する酸、例えば硫黄の一部が酸化されて生
成する硫酸を利用することができる。即ち、塩素吹き込
みにより通常は硫黄の2〜3%程度が酸化されるが、こ
の硫黄の酸化反応によって生成した硫酸のH+と空気中
の酸素により、ニッケルの浸出反応を起すことができ
る。The acid required for the oxidation reaction with oxygen can be added separately, but an acid generated by blowing chlorine in the leaching step, for example, sulfuric acid generated by oxidizing a part of sulfur is used. be able to. That is, about 2 to 3% of sulfur is usually oxidized by blowing chlorine. Nickel can be leached by H + of sulfuric acid generated by the oxidation reaction of sulfur and oxygen in the air.
【0022】[0022]
【実施例】以下に原料としてニッケルマットを用いた本
発明の実施例を説明する。図1はこの方法の実施に用い
た装置の一例を示す概略図であり、マットからニッケル
等の金属を浸出するための第1、第2、第3の反応槽1
a、1b、1cと、浸出液と残渣を分離するための濾過
装置7と、残渣を濾過した後の浸出液から不純物金属を
除去する浄液装置8と、浄液後の浸出液を電解して電気
ニッケルを回収する電解槽9とを備えている。EXAMPLES Examples of the present invention using nickel matte as a raw material will be described below. FIG. 1 is a schematic view showing an example of an apparatus used for carrying out this method. First, second, and third reaction tanks 1 for leaching a metal such as nickel from a mat.
a, 1b, 1c, a filtration device 7 for separating leachate and residue, a purification device 8 for removing impurity metals from the leachate after filtering the residue, and an electrolytic nickel And an electrolytic cell 9 for recovering water.
【0023】第1、第2、第3の反応槽1a、1b、1
cは、いずれも撹拌手段6を備え、相互にオーバーフロ
ー管5a、5bにより接続されている。また、第1反応
槽1aは原料であるニッケルマットのスラリーを供給す
るための原料供給口2と、塩素吹き込み管3aを備え、
第2反応槽1bは塩素吹き込み管3b、及び第3反応槽
1cは空気吹き込み管4をそれぞれ備えている。尚、濾
過装置7、浄液装置8及び電解槽9は、従来から使用さ
れている通常のものと変わりがない。First, second and third reaction tanks 1a, 1b, 1
c has a stirring means 6 and is connected to each other by overflow pipes 5a and 5b. The first reaction tank 1a includes a raw material supply port 2 for supplying a slurry of nickel matte, which is a raw material, and a chlorine blowing pipe 3a,
The second reaction tank 1b has a chlorine blowing pipe 3b, and the third reaction tank 1c has an air blowing pipe 4. The filtering device 7, the liquid purifying device 8 and the electrolytic cell 9 are the same as those used conventionally.
【0024】上記装置を用いて、本発明の塩素浸出電解
採取法によるニッケルの湿式精錬方法により、以下のご
とくニッケルマットからニッケルを金属として回収し
た。まず、原料のニッケルマットは粉砕して、通常のご
とく使用済み電解廃液と浸出液の一部とで調整した銅を
一価銅イオン(Cu+)として含む塩化物水溶液と混合
し、スラリーとした。Using the above apparatus, nickel was recovered as a metal from a nickel mat by the wet refining method of nickel by the chlorine leaching electrowinning method of the present invention as follows. First, the raw material nickel mat was pulverized and mixed with a chloride aqueous solution containing copper prepared as a monovalent copper ion (Cu + ) as usual by using a used electrolytic waste liquid and a part of a leachate to form a slurry.
【0025】このスラリーを原料供給口2から第1反応
槽1aに供給し、第2反応槽1b及び第3反応槽1cに
順にオーバーフローさせながら、塩素又は空気の吹き込
むことにより、ニッケル、コバルト、銅及び銅より卑な
金属の大部分を浸出させた。このとき、第1反応槽1a
で硫黄が塩素により酸化されて硫酸が生成するので、第
3反応槽1cでも硫酸のH+と空気中の酸素により浸出
反応が起こる。This slurry is supplied from the raw material supply port 2 to the first reaction tank 1a, and is blown into the second reaction tank 1b and the third reaction tank 1c while chlorine or air is blown into the first reaction tank 1a. And leached most of the metals lower than copper. At this time, the first reaction tank 1a
In this case, sulfur is oxidized by chlorine to generate sulfuric acid, so that a leaching reaction occurs in the third reaction tank 1c by H + of sulfuric acid and oxygen in the air.
【0026】第3反応槽1cからオーバーフローしたス
ラリーは、濾過装置7で残渣を分離し、浄液装置8で更
に塩素を吹き込んで鉄やコバルトなどの不純物金属を分
離した後、電解槽9に供給した。電解槽9では、カソー
ドにニッケルを電着させて回収し、アノード側で発生す
る塩素ガスの全量を回収して、第1及び第2反応槽1
a、1bの塩素吹き込み管3a、3bに供給すると共
に、浄液工程での塩素の吹き込みに使用した。尚、図1
には、電解槽9から浄液装置8への塩素の供給は図示し
ていない。The slurry overflowing from the third reaction tank 1 c is separated into residues by a filtration device 7, and chlorine is further blown by a water purification device 8 to separate impurity metals such as iron and cobalt, and then supplied to an electrolysis tank 9. did. In the electrolytic cell 9, nickel is electrodeposited on the cathode and collected, and the entire amount of chlorine gas generated on the anode side is collected and collected in the first and second reaction tanks 1.
a and 1b were supplied to chlorine blowing pipes 3a and 3b, and used for blowing chlorine in the liquid purification process. FIG.
In the figure, the supply of chlorine from the electrolytic cell 9 to the liquid purification device 8 is not shown.
【0027】上記の浸出工程において、各反応槽1a、
1b、1cでのオーバーフロー量を500リットル/分
とし、溶液の酸化還元単位が300〜500mV(Ag
/AgCl)となるように塩素又は空気を吹き込んだ。
塩素の吹き込み量は、容積30m3の第1反応槽1aで
3.5t/hr、容積30m3の第2反応槽1bで0.8
t/hrとした。また、容積20m3の第3反応槽1c
への空気の吹き込み量は5Nm3/分とした。第3反応
槽1cからオーバーフローした浸出後のスラリーを濾過
し、得られた浸出液の分析値を原料マットの組成と共に
表1に示した。In the above leaching step, each reaction tank 1a,
The amount of overflow at 1b and 1c was 500 liter / min, and the oxidation-reduction unit of the solution was 300 to 500 mV (Ag
/ AgCl) was blown with chlorine or air.
Blowing amount of chlorine in the first reaction vessel 1a volume 30 m 3 3.5t / hr, the second reaction vessel 1b of the volume of 30 m 3 0.8
t / hr. In addition, a third reaction tank 1c having a capacity of 20 m 3
The amount of air blown into the container was 5 Nm 3 / min. The leached slurry overflowing from the third reaction tank 1c was filtered, and the analysis values of the obtained leaching solution are shown in Table 1 together with the composition of the raw material mat.
【0028】[0028]
【表1】 [Table 1]
【0029】比較のため、上記と同様の装置を使用し、
ただし第3反応槽1cには空気の代わりにボンベから液
体塩素を吹き込んで、同一組成のニッケルマットからニ
ッケルの浸出を行った。各反応槽における塩素の吹き込
み量は、第1反応槽1aが3.2t/hr、第2反応槽
1bが0.9t/hr、及び第3反応槽1cが0.5t/
hrとし、その他の条件は前記実施例と同様とした。こ
の操業において第3反応槽1cよりオーバーフローした
浸出後のスラリーを濾過し、得られた浸出液の分析値を
表2に示した。For comparison, using the same device as above,
However, liquid chlorine was blown into the third reaction tank 1c from a cylinder instead of air, and nickel was leached from a nickel mat having the same composition. The amount of chlorine blown into each reaction tank was 3.2 t / hr in the first reaction tank 1a, 0.9 t / hr in the second reaction tank 1b, and 0.5 t / hr in the third reaction tank 1c.
hr, and the other conditions were the same as in the above example. In this operation, the leached slurry that overflowed from the third reaction tank 1c was filtered, and the analysis value of the obtained leachate is shown in Table 2.
【0030】[0030]
【表2】 [Table 2]
【0031】表1(本発明例)及び表2(従来例)から
分かるように、浸出工程で吹き込む塩素の一部を硫酸の
H+と空気中の酸素で代替しても、浸出反応は何ら問題
なく進行し、塩素のみの場合と同一レベルまで目的金属
を浸出できた。As can be seen from Table 1 (Example of the present invention) and Table 2 (Conventional example), even if part of the chlorine blown in the leaching step is replaced by H + of sulfuric acid and oxygen in the air, no leaching reaction occurs. The process proceeded without any problems, and the target metal was leached to the same level as in the case of chlorine alone.
【0032】尚、上記実施例では、塩素の一部に代えて
空気を吹き込む場合を述べたが、酸素富化空気や工業用
酸素を用いても同等又はそれ以上の効果が得られること
は言うまでもない。また、空気は第3反応槽にのみ吹き
込んだが、反応槽に酸が存在していれば、いずれの反応
槽に吹き込んでも、あるいは全ての反応槽に塩素と共に
吹き込んでも、同様の効果を得ることができる。In the above embodiment, the case where air is blown in instead of a part of chlorine is described. However, it goes without saying that the same or better effects can be obtained by using oxygen-enriched air or industrial oxygen. No. In addition, air is blown only into the third reaction tank, but if an acid is present in the reaction tank, the same effect can be obtained by blowing into any of the reaction tanks, or even blowing into all the reaction tanks with chlorine. it can.
【0033】[0033]
【発明の効果】本発明の方法によれば、ニッケルを含有
した粉状硫化物を原料とし、該原料から高純度ニッケル
を回収する塩素浸出電解採取法において、浸出工程での
吹き込みに使用する塩素の一部に代えて、液中に塩素吹
き込みにより生成した酸が存在する条件の下で、塩素よ
りもコストの安い空気又は酸素富化空気若しくは工業用
酸素を代替使用することができる。According to the method of the present invention, in a chlorine leaching electrowinning method for recovering high-purity nickel from a powdered sulfide containing nickel as a raw material, chlorine used for blowing in the leaching step is used. Can be used instead of air or oxygen-enriched air or industrial oxygen, which is less expensive than chlorine, under the condition that the acid generated by blowing chlorine is present in the liquid.
【0034】従って、電解工程で発生する塩素を浸出工
程の吹き込みに循環利用する場合にも、ロスにより発生
する吹き込み用塩素の不足分を系外から補充することな
く、安価な空気などのガスを吹き込んでニッケルを浸出
することができ、経済性を図りつつ、効率よくニッケル
を浸出して回収することが可能となった。Therefore, even when chlorine generated in the electrolysis step is circulated and used for blowing in the leaching step, inexpensive gas such as air can be supplied without replenishing the shortage of blowing chlorine generated by loss from outside the system. Nickel can be leached by blowing, and nickel can be leached and recovered efficiently while achieving economic efficiency.
【図1】本発明の実施例で使用したニッケルの湿式精錬
装置の概略図である。FIG. 1 is a schematic view of an apparatus for refining nickel used in an embodiment of the present invention.
1a 第1反応槽 1b 第2反応槽 1c 第3反応槽 2 原料供給口 3a、3b 塩素吹き込み管 4 空気吹き込み管 5a、5b オーバーフロー管 6 撹拌手段 7 濾過装置 8 浄液装置 9 電解槽 1a 1st reaction tank 1b 2nd reaction tank 1c 3rd reaction tank 2 Raw material supply port 3a, 3b Chlorine injection pipe 4 Air injection pipe 5a, 5b Overflow pipe 6 Stirrer 7 Filtration device 8 Purification device 9 Electrolysis tank
Claims (2)
イオンを含む塩化物水溶液とのスラリーに、塩素を吹き
込むことによりニッケルを浸出させる浸出工程と、得ら
れた浸出液の電解によりニッケルを回収する電解工程と
を含む、塩素浸出電解採取法によるニッケルの湿式精錬
方法において、前記塩素吹き込みにより生成された酸の
存在下で、塩素の一部に代えて空気又は酸素富化空気若
しくは工業用酸素を吹き込みながらニッケルを浸出する
ことを特徴とするニッケルの湿式精錬方法。1. A leaching step in which nickel is leached by blowing chlorine into a slurry of a powdery sulfide containing nickel and an aqueous chloride solution containing monovalent copper ions, and nickel is electrolyzed by electrolysis of the obtained leaching solution. And an electrolytic step for recovering, in the wet refining method of nickel by chlorine leaching electrowinning method, in the presence of the acid generated by the chlorine injection, air or oxygen-enriched air or industrial air instead of part of chlorine. A nickel wet smelting method characterized by leaching nickel while blowing oxygen.
程での塩素吹き込みに循環使用すると共に、浸出工程で
の塩素の不足量を空気又は酸素富化空気若しくは工業用
酸素の吹き込みにより補うことを特徴とする、請求項1
に記載のニッケルの湿式精錬方法。2. The method according to claim 1, wherein the chlorine generated in the electrolysis step is circulated and used for blowing chlorine in the leaching step, and the shortage of chlorine in the leaching step is compensated for by blowing air or oxygen-enriched air or industrial oxygen. The feature of claim 1
2. The method for refining nickel according to item 1.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP8294905A JPH10140257A (en) | 1996-11-07 | 1996-11-07 | Wet refining method of nickel by chlorine leaching electrolytic extracting method |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP8294905A JPH10140257A (en) | 1996-11-07 | 1996-11-07 | Wet refining method of nickel by chlorine leaching electrolytic extracting method |
Publications (1)
Publication Number | Publication Date |
---|---|
JPH10140257A true JPH10140257A (en) | 1998-05-26 |
Family
ID=17813782
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP8294905A Pending JPH10140257A (en) | 1996-11-07 | 1996-11-07 | Wet refining method of nickel by chlorine leaching electrolytic extracting method |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPH10140257A (en) |
Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1999066085A1 (en) * | 1998-06-12 | 1999-12-23 | Protium Metals Inc. | Treatment of roasted metal sulphide ores and ferrites by leaching with peroxysulphuric acid |
WO2002024966A1 (en) * | 2000-09-18 | 2002-03-28 | Inco Limited | Recovery of nickel and cobalt values from a sulfidic flotation concentrate by chloride assisted oxidative pressure leaching in sulfuric acid |
GB2380993A (en) * | 2001-09-11 | 2003-04-23 | Sumitomo Metal Mining Co | Recovering nickel |
WO2007039665A1 (en) * | 2005-10-03 | 2007-04-12 | Outotec Oyj. | Method for processing nickel bearing raw material in chloride-based leaching |
JP2009046736A (en) * | 2007-08-21 | 2009-03-05 | Sumitomo Metal Mining Co Ltd | Chlorine leaching method of nickel sulfide |
JP2010007183A (en) * | 2008-06-24 | 2010-01-14 | Korea Inst Of Geoscience & Mineral Resources | Dissolution apparatus for noble metal |
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CN102859012A (en) * | 2010-03-18 | 2013-01-02 | 奥图泰有限公司 | Method of processing nickel bearing raw material |
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JP2013166110A (en) * | 2012-02-15 | 2013-08-29 | Sumitomo Metal Mining Co Ltd | Filter cloth washing apparatus of filter press |
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-
1996
- 1996-11-07 JP JP8294905A patent/JPH10140257A/en active Pending
Cited By (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1999066085A1 (en) * | 1998-06-12 | 1999-12-23 | Protium Metals Inc. | Treatment of roasted metal sulphide ores and ferrites by leaching with peroxysulphuric acid |
WO2002024966A1 (en) * | 2000-09-18 | 2002-03-28 | Inco Limited | Recovery of nickel and cobalt values from a sulfidic flotation concentrate by chloride assisted oxidative pressure leaching in sulfuric acid |
US6428604B1 (en) | 2000-09-18 | 2002-08-06 | Inco Limited | Hydrometallurgical process for the recovery of nickel and cobalt values from a sulfidic flotation concentrate |
AU774519B2 (en) * | 2000-09-18 | 2004-07-01 | Inco Limited | Recovery of nickel and cobalt values from a sulfidic flotation concentrate by chloride assisted oxidative pressure leaching in sulfuric acid |
GB2380993A (en) * | 2001-09-11 | 2003-04-23 | Sumitomo Metal Mining Co | Recovering nickel |
GB2380993B (en) * | 2001-09-11 | 2003-11-19 | Sumitomo Metal Mining Co | Nickel refining method |
US7138005B2 (en) | 2001-09-11 | 2006-11-21 | Sumitomo Metal Mining Co., Ltd. | Nickel refining method |
AU2006298627B2 (en) * | 2005-10-03 | 2011-06-30 | Metso Outotec Finland Oy | Method for processing nickel bearing raw material in chloride-based leaching |
EA013353B1 (en) * | 2005-10-03 | 2010-04-30 | Ототек Оюй | Method for processing nickel bearing raw material in chloride-based leaching |
WO2007039665A1 (en) * | 2005-10-03 | 2007-04-12 | Outotec Oyj. | Method for processing nickel bearing raw material in chloride-based leaching |
JP2009046736A (en) * | 2007-08-21 | 2009-03-05 | Sumitomo Metal Mining Co Ltd | Chlorine leaching method of nickel sulfide |
JP2010007183A (en) * | 2008-06-24 | 2010-01-14 | Korea Inst Of Geoscience & Mineral Resources | Dissolution apparatus for noble metal |
KR101031922B1 (en) | 2009-03-16 | 2011-05-02 | 한국지질자원연구원 | The dissolution apparatus and method for metals having module type circulation strusture |
CN102859012A (en) * | 2010-03-18 | 2013-01-02 | 奥图泰有限公司 | Method of processing nickel bearing raw material |
JP2013158665A (en) * | 2012-02-02 | 2013-08-19 | Sumitomo Metal Mining Co Ltd | Method for controlling slurry supply device |
JP2013166110A (en) * | 2012-02-15 | 2013-08-29 | Sumitomo Metal Mining Co Ltd | Filter cloth washing apparatus of filter press |
JP2013189670A (en) * | 2012-03-13 | 2013-09-26 | Sumitomo Metal Mining Co Ltd | Hydrometallurgical process |
CN109762986A (en) * | 2019-03-20 | 2019-05-17 | 金川集团股份有限公司 | A kind of devices and methods therefor extracting nickel from nickel electrowinning copper ashes |
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