JPS62156238A - Selective extraction of gallium - Google Patents
Selective extraction of galliumInfo
- Publication number
- JPS62156238A JPS62156238A JP61297860A JP29786086A JPS62156238A JP S62156238 A JPS62156238 A JP S62156238A JP 61297860 A JP61297860 A JP 61297860A JP 29786086 A JP29786086 A JP 29786086A JP S62156238 A JPS62156238 A JP S62156238A
- Authority
- JP
- Japan
- Prior art keywords
- gallium
- solution
- organic phase
- dust
- enriched
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B58/00—Obtaining gallium or indium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G15/00—Compounds of gallium, indium or thallium
- C01G15/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3846—Phosphoric acid, e.g. (O)P(OH)3
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/02—Working-up flue dust
-
- 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
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
本発明は♂−キサイドと氷晶石との混合物からのアルミ
ニウムの電解製造用装置におけるがス捕集系で回収した
扮ａからガリウムを製造する方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for producing gallium from alumina recovered in a gas collection system in an apparatus for the electrolytic production of aluminum from a mixture of oxide and cryolite.
この粉塵の主成分は炭素及びアルミニウムとナトリウム
と鉄との酸化物である・該粉塵は通常約０．２〜約０．
５ｇ７１のガリウムを含有する。該粉Ｗを過剰のアルカ
リ金属の炭酸塩又はアルカリ金属の水酸化物と混合し、
この混合物を酸化性雰囲気中で上昇温度で処理し、しか
る後に処理した生成ａｔ水溶液中で滲出してガリウム１
１７（することにより前記の粉塵からガリウムを回収す
ることは公知である。しかる後にガリウムを例えば液−
液抽出により♂出溶液から抽出する。しかしながらガリ
ウムの回収率は低く通常７（ｌ以下である。The main components of this dust are carbon and oxides of aluminum, sodium, and iron.The dust is usually about 0.2 to about 0.
Contains 5g71 gallium. Mixing the powder W with excess alkali metal carbonate or alkali metal hydroxide,
This mixture is treated at elevated temperatures in an oxidizing atmosphere and then the treated product is leached into an aqueous solution of gallium 1
It is known to recover gallium from said dust by
Extract from the female solution by liquid extraction. However, the recovery rate of gallium is low and is usually less than 7 (l).
少憶のガリウムを金屑するクレー（ケイ戚アルミニウム
）を塩酸で処理してガリウム′ｔ″［有］出−Ｃ１しか
も抽出剤として′ｒミン化合抛を用いて液−液抽出によ
りガリウムをガリウムの富化した滲出溶液から抽出でき
ることも公知である。次いでガリウムを塩酸含有追出し
溶液によってガリウムを有機相から追出し、こ１によっ
てＧａｐ／、溶ｉを得る・しかしながらケイ酸アルミニ
ウム向質はアルミニウムの電解裏造装置でのがス捕集系
から回収した粉塵とはきわめて異なっている。Gallium is extracted by liquid-liquid extraction by treating clay (silicate aluminum) with hydrochloric acid to extract gallium and using amine compound as an extractant. It is also known that gallium can be extracted from an exudate solution enriched with silicate.The gallium is then driven out of the organic phase by means of a hydrochloric acid-containing expulsion solution, thereby obtaining Gap/, solution i. The dust collected by the backing equipment is very different from the dust collected from the collection system.
最後に、有機抽出剤として希釈したトリ−ｎ −ブチル
ホスフエート（ＴＢＰ）を用いることにょＱ 、 ｆ
ｓを／ニウム製造からの廃棄溶液から、ｆ １７ウムを
抽出できることも公知である。これらの樗類の溶液は硫
酸と塩酸との混合液であり、脂肪族の希釈剤（シンナー
）に溶解した１０暢ＴＢＰｔ”含んでなる有機抽出剤を
用いてガリウムの選択抽出ｆｔ達成するのが必要である
０この有機抽出剤の使用は多酸の有機溶液と用いねばな
らないことを意味する。Finally, using diluted tri-n-butyl phosphate (TBP) as the organic extractant
It is also known that f17um can be extracted from waste solutions from s/nium production. These chestnut solutions are mixtures of sulfuric acid and hydrochloric acid, and the selective extraction of gallium is accomplished using an organic extractant containing 10 TBPt dissolved in an aliphatic diluent (thinner). The use of this organic extractant means that organic solutions of polyacids must be used.
本発明の目的は、高純度のガリウムをアルミニウムの電
Ｍ製造装置でガス捕集系において回収した粉塵から回収
できる。簡単で低経費のガリウム！ｌ！造法を提供する
ものである・
従って本発明によると・アルミニウムの電解用装置にお
けるガス捕集系で捕集した粉厘刀為らガリウムを選択的
に抽出する方法において・該粉塵を５０〜１２０′ｃの
儲度で塩酸水心版に９．滲出させ。An object of the present invention is to recover high-purity gallium from dust collected in a gas collection system in an aluminum electric M manufacturing apparatus. Easy and low-cost gallium! l! Therefore, according to the present invention, in a method for selectively extracting gallium from powder collected by a gas collection system in an apparatus for electrolyzing aluminum, 9. Hydrochloric acid water core version with yield rate of 'c. Exude.
これによってガリウムを塩化ガリウムとして溶解させ、
しかる後に未希釈のトリ−ｎ−ブチルホスフエートより
なる有機相により塩化ガリウムをガリウムの富化した滲
出溶液から選択的に抽出し。This dissolves gallium as gallium chloride,
Gallium chloride is then selectively extracted from the gallium-enriched exudate solution with an organic phase consisting of undiluted tri-n-butyl phosphate.
ガリウムを水又は０．１〜３Ｍａ度好ましくは１〜２Ｍ
濃度のＮａＯＨの溶液により有機相から追出すことな特
徴とするガリウムの選択的抽出法が提供される・
前記の粉塵は３〜８Ｍの＃！注度の塩酸溶液により９５
〜１０５℃の温度で滲出するのが好ましい。Gallium in water or 0.1 to 3 Ma degree, preferably 1 to 2 M
A method for the selective extraction of gallium is provided, characterized in that it is driven out of the organic phase by a solution of NaOH at a concentration of 3-8M #! 95% by pouring hydrochloric acid solution
Preferably, leaching is carried out at a temperature of -105°C.
本発明の好ましい実施形式によると、ガリウムと共に溶
解している何れもの第二鉄を還元剤好ましくは鉄粉の添
加により第一鉄に還元してからｆ ＩＪウムの富化した
滲出溶液を有機抽出相と接触させる・
本発明の別の実施形式によると、該粉ｍを５ｏ。According to a preferred embodiment of the invention, any ferric iron dissolved together with the gallium is reduced to ferrous iron by the addition of a reducing agent, preferably iron powder, and then the fIJium-enriched exudate solution is organically extracted. According to another embodiment of the invention, the powder m is brought into contact with the phase.
〜１０００℃ の温度で酸化性雰囲気中で処理してから
滲出工程にかける・この処理により炭素、７ツ化物及び
タールを粉塵を除去し、これによって粉塵の＋Ａｔ”約
５０９６だけ減少させる。Treatment in an oxidizing atmosphere at a temperature of ˜1000° C. followed by a leaching step. This treatment removes the dust from carbon, heptides and tar, thereby reducing the dust by about 5096 +At”.
本発明の方法により８０−以上のガリウムの高い滲出収
率が達成され、、ｆｌＪウムは未希釈のＴＢＰによって
選択的に抽出される。未希釈のＴＯＦを用いると・脂肪
族希釈剤に希釈した１ｏＳＴＢＰを含んでなる有機相を
用いた既知の方法と比較すると有機抽出相の容量が実質
的に低下される。High leaching yields of gallium above 80 are achieved by the method of the invention, and flJ um is selectively extracted by undiluted TBP. Using undiluted TOF - the volume of the organic extraction phase is substantially reduced compared to known methods using an organic phase comprising 1oSTBP diluted in an aliphatic diluent.
本発明を次の実施例により更に説明する。The invention is further illustrated by the following examples.
実施例１
アルミニウムの電解製造用装置でのガス捕集系から捕集
した粉塵２００．ｆを６Ｍ塩酸溶液１０００−によＶ滲
出させた・滲出温度はｌ ＯＯ’Ｃであった・
該粉塵の化学的分析は次の如くであった：炭 素
３３ 重わ
フッ素 １７ 重を係
酸 素 １７ ｇ量嘩
アルミニウム １３ 重、ｔｉ％ナトリウム
ｑ ｉｔ憾
鉄 ６ ３１１優
硫 黄 ３ 重り
カルシウム １．５ 重敏係
ガリウム ０．４７重欧暢
ガリウムの富化した滲出溶液の化学的分析は次の如くで
あった：
ガリウム ｏ、ｓ ｌ／Ｌ
鉄 １３．４ ＃
アルミニウム ２５．０ ’
ナトリウム １７．４ １
フツ素 ２９．４ ＃
塩素 ２１２
ガリウムの滲出収率はかくしてｇ５−であった。Example 1 Dust collected from a gas collection system in an equipment for electrolytic production of aluminum 200. f was leached in 6M hydrochloric acid solution 1000-V. The leaching temperature was lOO'C. The chemical analysis of the dust was as follows: Carbon.
33 Weight: Fluorine 17 Weight: Oxygen 17 Weight: Aluminum 13 Weight, Ti% Sodium
The chemical analysis of the enriched exudate solution of gallium was as follows: Gallium o, s l/L Iron 13.4 # Aluminum 25.0 ' Sodium 17.4 1 Fluorine 29.4 # Chlorine 212 The leaching yield of gallium was thus g5-.
鉄粉をガリウムの富化した滲出溶液に添加して第二鉄を
第一鉄に還元させた。これによって滲出ｍ液中の鉄の含
着は１８．４９／ｌに増大した・しかる後に富化滲出溶
液を未希釈のトＩＩ −ｎ −ブチルホスフエートと・
５／１の水性相と有機相との容量比で接触させこれによ
ってｆ ＩＩウムを有機相に抽出させた。滲出溶液中の
ガリウム含ｌはこれによってｏ、ｇｙｉｔから０．０２
１１／を以下に低下した。この低下は滲出溶液中のガリ
ウムの９７．５蝿以上が未希釈のＴＢＰとの接触により
抽出されたことを意味する。Iron powder was added to the gallium-enriched exudate solution to reduce ferric iron to ferrous iron. This increased the iron impregnation in the exudate solution to 18.49/l.The enriched exudate solution was then mixed with undiluted TII-n-butyl phosphate.
Contact was made at a volume ratio of aqueous phase to organic phase of 5/1, thereby extracting the f IIium into the organic phase. The gallium content in the exudate solution is thereby reduced from o, gyit to 0.02
11/ or less. This reduction means that more than 97.5 gallium in the exudate solution was extracted by contact with undiluted TBP.
ガリウムは次いで有機相を−７の水と２工程で接触させ
ることにより有機相から追出した。水と有機相との容量
比は１：１であった。ガリウムを含有する得られた水溶
液をしかる後に再びＴＢＰと５／１の水／有機相の容量
比で接触させた。しかる後に、ｐ ＩＪウムは有機相を
水と前記と同じ様に接触させることにより追出した・
最終的に得られる追出し溶液は次の分析値を有した：
ガリウム ５ １１／を
鉄 ＜０．０５ １
アルミニウム ＜０．０５ 。Gallium was then driven from the organic phase by contacting the organic phase with -7 water in two steps. The volume ratio of water to organic phase was 1:1. The resulting aqueous solution containing gallium was then contacted again with TBP in a water/organic phase volume ratio of 5/1. The pIJium was then expelled by contacting the organic phase with water in the same manner as above. The final expelled solution had the following analysis: Gallium 5 11/Fe <0. 05 1 Aluminum <0.05.
ナトリウム ０．０５４ Ｉ
フッ素 ０．０２６ ＃
富化した滲出溶液中のＧａ ／ Ｆｅの比率は０．０６
であったけれども、最終的な追出し溶液中のＧａ／Ｆｅ
の比率は１００以上であった◎実施例２
アルミニウムの電解製造用装置におけるガス捕集系η島
ら回収した粉塵からガリウムを連続的に製造する／’Ｐ
イロットプラントでは、１２に９の粉塵ｔ３０ｔ／時の
６ Ｍ ＨＣＩで滲出した。ｆ＃出湯温度１００’Ｃに
保持した。Sodium 0.054 I Fluorine 0.026 # The ratio of Ga/Fe in the enriched exudate solution is 0.06
However, the Ga/Fe in the final expulsion solution
The ratio was 100 or more. ◎Example 2 Continuous production of gallium from dust collected from the gas collection system η island in equipment for electrolytic production of aluminum/'P
In the Ilot plant, 12 to 9 dust tons were exuded with 30 t/h of 6 M HCI. f# The hot water temperature was maintained at 100'C.
ガリウムの富化した滲出溶液は次の平均分析値を示した
。The gallium-enriched exudate solution had the following average analysis values:
ガリウム ＋、Ｉｐ／Ｌ
アルミニウム ３５ ＃
鉄 ２０ Ｉ
ナトリウム ２５１
フッ素 ５０９μ
塩素 ２１２１
富化した滲出溶液中の第二鉄は元素態鉄の添加により第
一鉄に還元された＠これによって滲出溶液中の平均鉄含
量は４０ ｇ７ｔに増大した。Gallium +, Ip/L Aluminum 35 # Iron 20 I Sodium 251 Fluorine 509 μ Chlorine 2121 The ferric iron in the enriched exudate solution was reduced to ferrous iron by the addition of elemental iron @thereby the average in the exudate solution Iron content increased to 40 g7t.
しかる後にガリウムの富化した滲出溶液は混合／沈降装
置中で未希釈のトＩＪ −ｎ−ブチルホスフエートと接
触させた。滲出溶液とＴＢＰとの容量比は５／１に調節
した◎これによってガリウムは有機相に抽出された。滲
出溶液中のｆｆ ＩＪウム含“ｌはこれによって０．０
２９７．を以下に低下した。このガリウム含量の低下は
ガリウム金遣の９８．１１が有機相中に抽出されたこと
を意味する。ガリウム含量の追出しのため有機相のＩ
／ ４１＆：連続的に流出さセタ（ｂｌｅｅｄ ｏｕｔ
） ａ有機相は追出し後に抽出工程に返送した＠ガリ
ウムは有機相を水と有機相／水の１：１の容量比で接触
させることにより有機相から追出したＯ
平衡用達するまで・譬イロットグラントを操業させた後
に追出し溶液の平均含ｔは次の如くであった：
ガリウム ＋ｓｇ７をThe gallium-enriched leaching solution was then contacted with undiluted IJ-n-butyl phosphate in a mixing/settling apparatus. The volume ratio of the leaching solution and TBP was adjusted to 5/1. ◎As a result, gallium was extracted into the organic phase. The ff IJ content in the exudate solution is thereby 0.0
297. decreased to below. This decrease in gallium content means that 98.11 of the gallium content has been extracted into the organic phase. I of the organic phase to expel the gallium content
/ 41&: bleed out continuously
) a The organic phase was returned to the extraction process after being expelled. @ Gallium was expelled from the organic phase by contacting the organic phase with water in a 1:1 volume ratio of organic phase/water. After running Grant, the average content of the expelled solution was as follows: Gallium + sg7
Claims (1)
から回収した粉塵からガリウムを選択的に抽出する方法
において、該粉塵を塩酸水溶液に滲出させこれによつて
ガリウムを塩化ガリウムとして溶解させ、しかる後に未
希釈のトリ−ｎ−ブチルホスフエートよりなる有機相に
よつてガリウムの富化した滲出溶液から塩化ガリウムを
選択的に抽出し、ガリウムを水又は０．１〜３Ｍ濃度の
ＮａＯＨのアルカリ溶液により有機相から追出すことを
特徴とするガリウムの選択的抽出法。 ２、粉塵を３〜８Ｍの酸性度の塩酸水溶液で滲出し、滲
出温度は５０〜１２０℃に保持する特許請求の範囲第１
項記載の方法。 ３、ガリウムの富化した滲出溶液を有機相と接触させる
前に、還元剤の添加により、富化した滲出溶液中の第二
鉄を第一鉄に還元する特許請求の範囲第１項記載の方法
。 ４、粉塵を５００〜１０００℃の温度で酸化性雰囲気中
で処理してから滲出工程にかける特許請求の範囲第１項
記載の方法。[Claims] 1. In a method for selectively extracting gallium from dust collected from a gas collection system in equipment for electrolytic production of aluminum, the dust is leached into an aqueous hydrochloric acid solution, thereby converting gallium into gallium chloride. The gallium chloride is then selectively extracted from the gallium-enriched exudate solution by an organic phase consisting of undiluted tri-n-butyl phosphate, and the gallium is dissolved in water or at a concentration of 0.1-3M. A selective extraction method for gallium, characterized in that it is expelled from the organic phase by an alkaline solution of NaOH. 2. The dust is leached with an aqueous hydrochloric acid solution having an acidity of 3 to 8M, and the leaching temperature is maintained at 50 to 120°C.Claim 1
The method described in section. 3. Before contacting the gallium-enriched leaching solution with the organic phase, the ferric iron in the gallium-enriched leaching solution is reduced to ferrous iron by adding a reducing agent. Method. 4. The method according to claim 1, wherein the dust is treated in an oxidizing atmosphere at a temperature of 500 to 1000°C and then subjected to a leaching step.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NO854797A NO158028C (en) | 1985-12-16 | 1985-12-16 | GALLIUM EXTRACTION. |
| NO854797 | 1985-12-16 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62156238A true JPS62156238A (en) | 1987-07-11 |
| JPS642654B2 JPS642654B2 (en) | 1989-01-18 |
Family
ID=19888611
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61297860A Granted JPS62156238A (en) | 1985-12-16 | 1986-12-16 | Selective extraction of gallium |
Country Status (11)
| Country | Link |
|---|---|
| JP (1) | JPS62156238A (en) |
| AU (1) | AU572412B2 (en) |
| BR (1) | BR8606230A (en) |
| CA (1) | CA1309869C (en) |
| DE (1) | DE3640381A1 (en) |
| ES (1) | ES2002227A6 (en) |
| FR (1) | FR2591582B1 (en) |
| GB (1) | GB2184108B (en) |
| NL (1) | NL8602997A (en) |
| NO (1) | NO158028C (en) |
| NZ (1) | NZ218419A (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2624524B1 (en) * | 1987-11-24 | 1990-05-18 | Metaleurop Sa | METHOD FOR HYDROMETALLURGICAL TREATMENT OF GALLIFER MATERIAL SOLUTION |
| CN100396804C (en) * | 2005-12-09 | 2008-06-25 | 韶关市华韦实业有限公司 | Technology for extracting Gallium metal from lead-zine tail ore slug smelting by extracting-electrolytic method |
| CN103276407B (en) * | 2013-05-13 | 2016-12-28 | 攀枝花学院 | A kind of from low-grade containing gallium, ferrum raw material reclaim gallium and the method for ferrum |
| CN113667839B (en) * | 2021-08-20 | 2022-06-28 | 安徽工业大学 | Method for recovering metal gallium from gallium nitride waste under normal pressure |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60166224A (en) * | 1984-02-03 | 1985-08-29 | Mitsui Alum Kogyo Kk | Method of recovery of gallium from dust of aluminum smelting |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2848398A (en) * | 1955-05-11 | 1958-08-19 | Zh Sekitan Sogo Kenkyujo | Recovery of gallium compounds from the combustion gases of coal |
| GB991614A (en) * | 1960-08-27 | 1965-05-12 | Asahi Chemical Ind | Process for recovering gallium in the purification of crude alumina |
| GB991613A (en) * | 1960-11-28 | 1965-05-12 | Asahi Chemical Ind | Process for the recovery of gallium |
| DD127573A1 (en) * | 1976-09-06 | 1977-10-05 | ||
| FR2397464A2 (en) * | 1977-07-13 | 1979-02-09 | Rhone Poulenc Ind | PROCESS FOR RECOVERING GALLIUM FROM VERY BASIC SOLUTIONS BY LIQUID / LIQUID EXTRACTION |
| FR2411894A1 (en) * | 1977-12-15 | 1979-07-13 | Rhone Poulenc Ind | GALLIUM EXTRACTION PROCESS |
| FR2460276A1 (en) * | 1979-07-03 | 1981-01-23 | Rhone Poulenc Ind | PROCESS FOR TREATING RARE EARTH OXIDES AND GALLIUM MIXTURES |
| FI70693C (en) * | 1980-12-05 | 1986-10-06 | Rhone Poulenc Ind | FOERFARANDE FOER RENING AV EN GALLIUMLOESNING |
| JPS6058170B2 (en) * | 1982-12-17 | 1985-12-18 | 三井アルミニウム工業株式会社 | Method for recovering gallium from dust generated in an aluminum electrolytic furnace |
-
1985
- 1985-12-16 NO NO854797A patent/NO158028C/en unknown
-
1986
- 1986-11-24 CA CA 523662 patent/CA1309869C/en not_active Expired - Lifetime
- 1986-11-25 NL NL8602997A patent/NL8602997A/en active Search and Examination
- 1986-11-26 DE DE19863640381 patent/DE3640381A1/en active Granted
- 1986-11-27 NZ NZ21841986A patent/NZ218419A/en unknown
- 1986-11-28 FR FR8616649A patent/FR2591582B1/en not_active Expired
- 1986-12-15 ES ES8603423A patent/ES2002227A6/en not_active Expired
- 1986-12-16 JP JP61297860A patent/JPS62156238A/en active Granted
- 1986-12-16 AU AU66588/86A patent/AU572412B2/en not_active Ceased
- 1986-12-16 BR BR8606230A patent/BR8606230A/en unknown
- 1986-12-16 GB GB8629961A patent/GB2184108B/en not_active Expired
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60166224A (en) * | 1984-02-03 | 1985-08-29 | Mitsui Alum Kogyo Kk | Method of recovery of gallium from dust of aluminum smelting |
Also Published As
| Publication number | Publication date |
|---|---|
| NO854797L (en) | 1987-06-01 |
| NO158028C (en) | 1988-06-29 |
| CA1309869C (en) | 1992-11-10 |
| GB2184108B (en) | 1989-10-18 |
| AU6658886A (en) | 1987-06-25 |
| AU572412B2 (en) | 1988-05-05 |
| NO158028B (en) | 1988-03-21 |
| FR2591582A1 (en) | 1987-06-19 |
| FR2591582B1 (en) | 1988-07-01 |
| GB8629961D0 (en) | 1987-01-28 |
| GB2184108A (en) | 1987-06-17 |
| JPS642654B2 (en) | 1989-01-18 |
| NL8602997A (en) | 1987-07-16 |
| NZ218419A (en) | 1989-04-26 |
| BR8606230A (en) | 1987-09-29 |
| DE3640381A1 (en) | 1987-06-04 |
| ES2002227A6 (en) | 1988-07-16 |
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