CN102433439B - Method for recovering rhenium from arsenic filter cake - Google Patents

Method for recovering rhenium from arsenic filter cake Download PDF

Info

Publication number
CN102433439B
CN102433439B CN2011104229868A CN201110422986A CN102433439B CN 102433439 B CN102433439 B CN 102433439B CN 2011104229868 A CN2011104229868 A CN 2011104229868A CN 201110422986 A CN201110422986 A CN 201110422986A CN 102433439 B CN102433439 B CN 102433439B
Authority
CN
China
Prior art keywords
rhenium
arsenic
filter cake
extraction
arsenic filter
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.)
Expired - Fee Related
Application number
CN2011104229868A
Other languages
Chinese (zh)
Other versions
CN102433439A (en
Inventor
吴海国
许小龙
王智友
姚金江
李婕
肖超
刘景槐
黄彦强
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
YONGXIN XINTAI SILVER INDUSTRY Co Ltd
Hunan Research Institute of Non Ferrous Metals
Original Assignee
YONGXIN XINTAI SILVER INDUSTRY Co Ltd
Hunan Research Institute of Non Ferrous Metals
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by YONGXIN XINTAI SILVER INDUSTRY Co Ltd, Hunan Research Institute of Non Ferrous Metals filed Critical YONGXIN XINTAI SILVER INDUSTRY Co Ltd
Priority to CN2011104229868A priority Critical patent/CN102433439B/en
Publication of CN102433439A publication Critical patent/CN102433439A/en
Application granted granted Critical
Publication of CN102433439B publication Critical patent/CN102433439B/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

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)

Abstract

The invention provides a method for recovering rhenium from an arsenic filter cake. The method comprises the following steps: entering rhenium, arsenic and sulfur into a solution by adopting one-section alkali leaching and second-section oxidization and leaching, and simultaneously enriching lead, bismuth, copper and selenium in leaching slag; in the one-section leachate, converting rhenium into perrhenate in a form of sodium thioperrhenate by adopting an oxidization method, converting sodium thioarsenate into sodium arsenate, and separating out sulfur in a form of simple substance sulfur; removing arsenic from the solution obtained by oxidization conversion by using a sulfur dioxide reduction method or lime method; carrying out rhenium enrichment on the solution obtained after arsenic is removed; treating a rhenium reextraction liquid by using a potassium chloride precipitation method to obtain crude potassium perrhenate; and refining crude potassium perrhenate to obtain potassium perrhenate. The method has short process flow, high rhenium recovery rate and low treatment cost; and by using the method, the comprehensive utilization of valuable metals in the arsenic filter cake can be realized.

Description

A kind of method that from arsenic filter cake, reclaims rhenium
Technical field
The invention belongs to Non-ferrous Metallurgy and environmental improvement technical field, relate to a kind of new method that from arsenic-containing material, reclaims rhenium, particularly take the arsenic filter cake of copper smelting by pyrometallurgy acid making system output as the raw materials recovery rhenium.
Background technology
Extract the main raw material of rhenium: independent rhenium mineral are less at occurring in nature, and it mainly is present in the molybdenum glance with oxide morphology, and molybdenum glance is normal and the copper-sulphide ores symbiosis.Rhenium is enriched in copper sulfide concentrate and brings the pyrometallurgical smelting system of copper in the selecting and purchasing process of copper-sulphide ores.In the pyrometallurgical smelting process of copper, the rhenium volatilization more than 82% enters in the spent acid stoste of flue gas acid preparing system, and wherein the form of 94% above sulfide enters arsenic filter cake.Rhenium is present in the concentrated molybdenum ore equally, and in the oxidizing roasting process of concentrated molybdenum ore, rhenium enters flue gas with the volatilization of rhenium heptoxide form, and rhenium is enriched in the flue dust behind the flue gas dust collection.Therefore the raw material that extracts rhenium mainly contains the arsenic filter cake of concentrated molybdenum ore oxidizing roasting flue dust and pyrometallurgical smelting system output.
The typical case reclaims the technique of rhenium from arsenic filter cake: the enterprise of China's rhenium output maximum is the subordinate's of Jiangxi Copper group Guixi Smelter at present, a small amount of rhenium is contained in the main body mine of this factory, in the process of selecting and purchasing smelting, rhenium enters in the arsenic filter cake of acid making system output of pyrometallurgical smelting.Arsenic filter cake adopts the copper sulfate displacement to leach, and makes the As in the arsenic filter cake 2S 3Be converted into H 3AsO 3, then pass into oxygen toward system and make H 3AsO 3Be converted into H 3AsO 4, the Re in the copper sulfate displacement leaching process in the arsenic filter cake 2S 7With CuSO 4Reaction generates HReO 7And enter solution, and after the solution that contains arsenic, rhenium is removed arsenic by sulphur dioxide reduction, adopt ion exchange method to obtain the pregnant solution of rhenium, obtain the finished product ammonium perrhenate through condensing crystal production again.
The main drawback that adopts the copper sulfate substitution method to extract rhenium has:
(1) long flow path, cost is high: because the arsenic content in the arsenic filter cake up to more than 20%, must be processed arsenic in the process of extracting rhenium, adopt the copper sulfate substitution method to extract rhenium, need to use copper-bath twice in the process of processing, generate As twice 2O 3, technical process is long, and processes ltAs 2O 3Need to consume the 2t copper powder, process the direct processing cost of 1t arsenic filter cake and surpassed 6000 yuan.
(2) the oxidation rinsing level of residue is large, and is difficult: process the above washing residue of 1t arsenic filter cake output 1.2t, the residue water content is high, is difficult to directly return the pyrometallurgical smelting system of copper.
(3) the Recovery of rhenium rate is low: in treating processes, the Recovery of rhenium rate only is 88%.
Summary of the invention
For the deficiencies in the prior art part, the invention provides a kind of method that from arsenic filter cake, reclaims rhenium, this technical process is short, and the rhenium rate of recovery is high, and effective other valuable metals of enrichment.
For achieving the above object, technical scheme of the present invention is:
A kind of method that reclaims rhenium from arsenic filter cake comprises following concrete steps:
(1) will add one section leaching of alkali lye behind the arsenic filter cake ore grinding first, concentration of lye is 80g/L-120g/L, and controlling liquid-solid mass ratio is 3-5: 1, and extraction temperature is controlled at 55 ℃～95 ℃, extraction time 1h～5h; Filter to get one section leach liquor and one section leached mud;
(2) above-mentioned one section leached mud is added two sections leachings of oxygenant, oxidant concentration is 20g/L-25g/L, and controlling liquid-solid mass ratio is 2-5: 1, and control solution oxide current potential 〉=200mv, 55 ℃～95 ℃ of extraction temperatures, extraction time 1h～5h; Filter to get two sections leach liquors and two sections leached muds;
(3) above-mentioned one section leach liquor is added oxygenant oxidation, oxidising process solution system terminal point control of Electric potentials 〉=200mv;
(4) one section leach liquor after the oxidation mixes with two sections leach liquors, adopts using sulfur dioxide reduction method or lime precipitation arsenic removal;
(5) then adopt extraction process separation and concentration rhenium, the raffinate evaporating, concentrating and crystallizing is produced saltcake;
(6) the concentrated rear Repone K that adds of the extraction liquid behind the above-mentioned rich rhenium, crystallisation by cooling is separated out rough potassium perrhenate, and rough potassium perrhenate recrystallizing and refining gets potassium perrhenate.
Ore grinding described in the step (1) is that levigate extremely-100 orders of arsenic filter cake are accounted for more than 80%.
Alkali in the step (1) in the alkali lye is selected from sodium hydroxide, sodium sulphite or yellow soda ash.
Oxygenant in step (2) and the step (3) is selected from clorox, sodium chlorate, Manganse Dioxide, potassium permanganate or hydrogen peroxide.
The described using sulfur dioxide reduction method of step (4) refers to adopt sulfurous gas to make reductive agent, and reduction obtains arsenus acid, makes industrial white arsenic after the arsenus acid dehydration; Described lime precipitation refers to adopt lime precipitation, control precipitation pH value 〉=6.0, and precipitation obtains the Tricalcium arsenate product, as the raw material of producing white arsenic.
The pH of control solution＞6.0 in the described arsenic removal process of step (4).
In the described extraction process separation and concentration of step (5) rhenium: extraction agent adopts N235 (trialkyl mixing tertiary amine), help the extraction agent to adopt secondary octanol, thinner is kerosene, the volume of organic phase consists of: the secondary octanol of 20%N235+10%+70% kerosene, reverse-extraction agent employing mass concentration are 12%～15% ammoniacal liquor.
Behind the described adding Repone K of step (6), the concentration＞5g/L of control solution free chlorine potassium, solution is cooled to 5 ℃, and crystallisation by cooling is separated out rough potassium perrhenate.
Below the present invention will be further explained and the explanation:
Arsenic filter cake of the present invention refers to the arsenic filter cake of output in concentrated molybdenum ore oxidizing roasting flue dust and the pyrometallurgical melting.The main component of the arsenic filter cake that the present invention is used (mass content) has Re:1580-1620g/t, As:20.0%-21.5%, S:53%-55%, Se:1.8%-1.9%, Bi:2.9%-3.2%, Cu:1%-1.5%, Pb:2.5%-2.8%, and all the other are impurity.
Know-why of the present invention comprises:
(1) one section alkali soaks, and arsenic filter cake adopts sodium hydroxide, yellow soda ash, sodium sulphite to leach, and following chemical reaction mainly occurs process:
As 2S 3+6NaOH→Na 3AsS 3+Na 3AsO 3+3H 2O
3S+6NaOH→Na 2SO 3+2Na 2S+3H 2O
As 2S 3+3Na 2S→2Na 3AsS 3
As 2S 3+3Na 2CO 3→Na 3AsS 3+Na 3AsO 3+3CO 2
Re 2S 7+Na 2S→2NaReS 4
4Re 2S 7+8NaOH→7NaReS 4+NaReO 4+4H 2O
4Re 2S 7+4Na 2CO 3→7NaReS 4+NaReO 4+4CO 2
Rhenium, arsenic, sulphur are entered in one section leach liquor, and the valuable metals such as other element such as copper, lead, bismuth, selenium remain in one section leached mud and obtain enrichment.
(2) two sections Oxidation Leachings
When one section leached mud adopted hydrogen peroxide, sodium chlorate, hypochlorite oxidation leaching, the chemical reaction of generation was as follows:
Re 2S 7+28H 2O 2→2HReO 4+7H 2SO 4+20H 2O
3Re 2S 7+7NaClO 3+3H 2O→6HReO 4+7NaCl+21S↓
Re 2S 7+7NaClO+H 2O→2HReO 4+7S↓+7NaCl
Make the sulfide of the rhenium that is wrapped up by metallic sulfide and at a low price the oxide compound of rhenium be oxidized to rhenate and enter two sections leach liquors; Two sections leached muds of process output are allocated copper anode slime treatment process into and are comprehensively reclaimed selenium, copper, lead, bismuth.
(3) one sections leach liquor oxidations
When adopting hydrogen peroxide, sodium chlorate, one section leach liquor of clorox processing, the main chemical reactions of generation is as follows:
NaReS 4+4H 2O 2→NaReO 4+4H 2O+4S↓
3NaReS 4+4NaClO 3→3NaReO 4+4NaCl+12S↓
NaReS 4+4NaClO→NaReO 4+4S+4NaCl
Make rhenium be converted into perrhenate by thioperrhenate, thioarsenous acid sodium is converted into sodium arseniate.
(4) solution dearsenification
Sodium arseniate in the solution and calcium hydroxide reaction generate the Tricalcium arsenate precipitation.
4Na 3AsO 4+6Ca(OH) 2→2Ca 3(AsO 4) 2+12NaOH
(5) rhenium-containing solution extraction and back extraction
The chemical reaction that mainly occurs when adopting the rhenium in the N235 extraction solution is as follows:
R 3N+H ++ReO 4 -→R 3NH 4ReO 4
Load organic phases adopts the ammoniacal liquor back extraction, and it is as follows that chemical reaction occurs:
R 3NH 4ReO 4+NH 4OH→R 3N+NH 4ReO 4+H 2O
(6) heavy rhenium
NH 4ReO 4+KCl→KReO 4↓+NH 4Cl
Compared with prior art, advantage of the present invention is:
(1) the Recovery of rhenium rate is high: this technique whole process Recovery of rhenium rate can reach more than 95%;
(2) flow process is short, cost is low: two sections leachings of this process using, leach liquor oxidation, solution dearsenification, extracting and enriching Separation of Rhenium, the heavy rhenium of Repone K, the refining potassium perrhenate that obtains of thick potassium perrhenate, processing technological flow is short, and the direct processing cost of 1t arsenic filter cake is lower than 4000 yuan.
(3) fully utilize other valuable metals: arsenic filter cake is after two sections leachings, the valuable metals such as the copper in the arsenic filter cake, lead, bismuth, selenium are enriched in the leached mud, its grade improves more than 2.5 times, can allocate the ANODE SLIME TREATMENT operation of copper smelting by pyrometallurgy factory into, the comprehensive valuable metals such as wherein selenium, lead, bismuth, copper that reclaim.
Description of drawings:
Fig. 1 is a kind of concrete technology schema that reclaims the method for rhenium from arsenic filter cake of the present invention.
Embodiment
Below in conjunction with embodiment, the present invention will be further explained and explanation, but the invention is not restricted to the scope of embodiment, and percentage composition described in the embodiment all refers to the quality percentage composition except specifying.
Embodiment 1:
Take the arsenic filter cake of domestic certain copper smelting plant as raw material, wherein main component (mass content) has Re:1580-1620g/t, As:20.0%-21.5%, S:53%-55%, Se:1.8%-1.9%, Bi:2.9%-3.2%, Cu:1%-1.5%, Pb:2.5%-2.8%, and all the other are impurity.
One section leaching process is allocated the sodium hydroxide of material quantity 50% into, liquid-solid ratio control 3: 1,90 ℃ of extraction temperature controls, extraction time 4h.The leaching yield of one section leaching process rhenium is 94%, and the leaching yield of arsenic is 98%, and the leaching yield of selenium is 3%, and lead, bismuth, copper are enriched in the leached mud, one section leached mud that leaches output material quantity about 40%.
The clorox of one section leached mud adding 25g/L carries out two sections leachings, control liquid-solid ratio control 3: 1,60 ℃ of extraction temperature controls, extraction time 2h, control solution oxide current potential 〉=200mv.The leaching yield 86% of two sections leaching process rheniums, the leaching yield 85% of arsenic, the leaching yield 5% of selenium, leached mud rate are 86%.
Total leaching yield of rhenium is 99.16% in the leaching process, and the leaching yield of arsenic is 99.7%, and the leaching yield of selenium is 7.85%.Contain selenium 4.96% in two sections leached muds, cupric 3.58%, leaded 7.7%, bismuth-containing 8.75%.
One section leach liquor adds the sodium chlorate oxidation of 25g/L, the current potential 〉=200mv of control solution, and the retention rate of Re in solution is 98.5%, the sulphur slag sulfur-bearing 86.5% of output contains Re100g/t in the oxidising process, contains arsenic and is lower than 1%.
The oxidizing solution of rhenium-containing, arsenic adds lime, and the pH value of control solution is 8.0, and the content of As is to 200mg/L in the heavy arsenic tail washings, and the Tricalcium arsenate slag of output contains Re less than 5g/t.
It is the secondary octanol of 20%N235+10%+70% kerosene extraction that arsenic removal rhenium-containing solution adopts the organic phase volume proportion, and it is the rich rhenium solution that 12% ammoniacal liquor back extraction obtains rhenium-containing 12～15g/L that load organic phases adopts mass concentration.Rich rhenium solution directly adds Repone K, and Repone K is excessive, and potassium chloride concentration free in the solution is 3g/L, and solution is cooled to 5 ℃, obtains rough potassium perrhenate product, and the content of potassium perrhenate is greater than 95%.Thick potassium perrhenate obtains containing potassium perrhenate greater than 99% refining potassium perrhenate through recrystallization.
Embodiment 2:
Take the arsenic filter cake of domestic certain copper smelting plant as raw material, main component (mass content) has Re:1580-1620g/t, As:20.0%-21.5%, S:53%-55%, Se:1.8%-1.9%, Bi:2.9%-3.2%, Cu:1%-1.5%, Pb:2.5%-2.8%, and all the other are impurity.
One section leaching process is allocated the yellow soda ash of material quantity 60% into, liquid-solid ratio control 4: 1,95 ℃ of extraction temperature controls, extraction time 5h.The leaching yield of one section leaching process rhenium is 92%, and the leaching yield of arsenic is 96%, and the leaching yield of selenium is 1%, and lead, bismuth, copper are enriched in the leached mud, one section leached mud that leaches output material quantity about 45%.
One section leached mud adds about 27% hydrogen peroxide and carries out two sections leachings, control liquid-solid ratio control 4: 1,80 ℃ of extraction temperature controls, extraction time 4h, control solution oxide current potential 〉=200mv.The leaching yield 88% of two sections leaching process rheniums, the leaching yield 84% of arsenic, the leaching yield 5% of selenium, the leached mud rate is about 82%.
Total leaching yield of rhenium is 99.04% in the leaching process, and the leaching yield of arsenic is 99.36%, and the leaching yield of selenium is 5.95%.Contain selenium 4.42% in two sections leached muds, cupric 3.12%, leaded 6.73%, bismuth-containing 7.64%.
One section leach liquor adds about 27% hydrogen peroxide oxidation, the current potential 〉=200mv of control solution, and the retention rate of Re in solution is 98.5%, the sulphur slag sulfur-bearing 86.5% of output in the oxidising process contains and is lower than Re100g/t, contains arsenic and is lower than 1%.
The oxidizing solution of rhenium-containing, arsenic adds lime, and the pH value of control solution is 8.0, and the content of As is to 200mg/L in the heavy arsenic tail washings, and the Tricalcium arsenate slag of output contains Re less than 5g/t.
It is the secondary octanol of 20%N235+10%+70% kerosene extraction that arsenic removal rhenium-containing solution adopts the organic phase volume proportion, and it is the rich rhenium solution that 15% ammoniacal liquor back extraction obtains rhenium-containing 12～15g/L that load organic phases adopts mass concentration.Rich rhenium solution directly adds Repone K, and Repone K is excessive, and potassium chloride concentration free in the solution is 3g/L, and solution is cooled to 5 ℃, obtains rough potassium perrhenate product, and the content of potassium perrhenate is greater than 95%.Thick potassium perrhenate obtains containing potassium perrhenate greater than 99% refining potassium perrhenate through recrystallization.

Claims (9)

1. a method that reclaims rhenium from arsenic filter cake is characterized in that, comprises following concrete steps:
(1) will add one section leaching of alkali lye behind the arsenic filter cake ore grinding first, concentration of lye is 80g/L-120g/L, and controlling liquid-solid mass ratio is 3-5:1, and extraction temperature is controlled at 55 ℃ ~ 95 ℃, extraction time 1 h ~ 5h; Filter to get one section leach liquor and one section leached mud;
(2) above-mentioned one section leached mud is added two sections leachings of oxygenant, oxidant concentration is 20g/L-25g/L, and controlling liquid-solid mass ratio is 2-5:1, control solution oxide current potential 〉=200mv, 55 ℃ ~ 95 ℃ of extraction temperatures, extraction time 1 h ~ 5h; Filter to get two sections leach liquors and two sections leached muds;
(3) above-mentioned one section leach liquor is added oxygenant oxidation, oxidising process solution system terminal point control of Electric potentials 〉=200mv;
(4) one section leach liquor after the oxidation mixes with two sections leach liquors, adopts using sulfur dioxide reduction method or lime precipitation arsenic removal;
(5) then adopt extraction process separation and concentration rhenium, the raffinate evaporating, concentrating and crystallizing is produced saltcake;
(6) the concentrated rear Repone K that adds of the extraction liquid behind the above-mentioned rich rhenium, crystallisation by cooling is separated out rough potassium perrhenate, and rough potassium perrhenate recrystallizing and refining gets potassium perrhenate.
2. described a kind of method that reclaims rhenium from arsenic filter cake according to claim 1 is characterized in that, ore grinding described in the step (1) is to account for more than 80% to-100 orders arsenic filter cake is levigate.
3. described a kind of method that reclaims rhenium from arsenic filter cake according to claim 1 is characterized in that the alkali in the step (1) in the alkali lye is selected from sodium hydroxide, sodium sulphite or yellow soda ash.
4. described a kind of method that reclaims rhenium from arsenic filter cake according to claim 1 is characterized in that the oxygenant in step (2) and the step (3) is selected from clorox, sodium chlorate, Manganse Dioxide, potassium permanganate or hydrogen peroxide.
5. described a kind of method that reclaims rhenium from arsenic filter cake according to claim 1 is characterized in that the described using sulfur dioxide reduction method of step (4) refers to adopt sulfurous gas to make reductive agent, and reduction obtains arsenus acid, makes industrial white arsenic after the arsenus acid dehydration;
Described lime precipitation refers to adopt lime precipitation, the pH value of its solution 〉=6.0 during the control precipitation, and precipitation obtains the Tricalcium arsenate product, as the raw material of producing white arsenic.
6. described a kind of method that reclaims rhenium from arsenic filter cake according to claim 1 is characterized in that the pH of control solution in the described arsenic removal process of step (4)〉6.0.
7. described a kind of method that from arsenic filter cake, reclaims rhenium according to claim 1, it is characterized in that, in the described extraction process separation and concentration of step (5) rhenium: extraction agent adopts trialkyl mixing tertiary amine, be called for short N235, help the extraction agent to adopt secondary octanol, thinner is kerosene, and the volume of organic phase consists of: the secondary octanol of 20%N235+10%+70% kerosene, reverse-extraction agent employing mass concentration are 12% ~ 15% ammoniacal liquor.
8. described a kind of method that reclaims rhenium from arsenic filter cake according to claim 1 is characterized in that, behind the described adding Repone K of step (6), and the concentration of control solution free chlorine potassium〉5g/L, solution is cooled to 5 ℃, and crystallisation by cooling is separated out rough potassium perrhenate.
9. described a kind of method that from arsenic filter cake, reclaims rhenium according to claim 1, it is characterized in that, described arsenic filter cake refers to the arsenic filter cake of output in concentrated molybdenum ore oxidizing roasting flue dust and the pyrometallurgical melting, the mass content of main component is as follows: Re:1580-1620g/t, As:20.0%-21.5%, S:53%-55%, Se:1.8%-1.9%, Bi:2.9%-3.2%, Cu:1%-1.5%, Pb:2.5%-2.8%, all the other are impurity.
CN2011104229868A 2011-12-16 2011-12-16 Method for recovering rhenium from arsenic filter cake Expired - Fee Related CN102433439B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2011104229868A CN102433439B (en) 2011-12-16 2011-12-16 Method for recovering rhenium from arsenic filter cake

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2011104229868A CN102433439B (en) 2011-12-16 2011-12-16 Method for recovering rhenium from arsenic filter cake

Publications (2)

Publication Number Publication Date
CN102433439A CN102433439A (en) 2012-05-02
CN102433439B true CN102433439B (en) 2013-01-23

Family

ID=45981785

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2011104229868A Expired - Fee Related CN102433439B (en) 2011-12-16 2011-12-16 Method for recovering rhenium from arsenic filter cake

Country Status (1)

Country Link
CN (1) CN102433439B (en)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102851497B (en) * 2012-09-21 2014-07-23 北京矿冶研究总院 Method for treating arsenic-containing material
CN103233129B (en) * 2013-05-08 2015-03-25 金川集团股份有限公司 Wet-process open treatment method of arsenic in copper ashes
CN104152705B (en) * 2014-08-08 2016-08-17 西北矿冶研究院 Process for producing cathode zinc by utilizing casting zinc dross tailings
CN105861843A (en) * 2015-01-23 2016-08-17 昆明冶金高等专科学校 Efficient method for enriching rhenium from high-arsenic copper sulfide material containing rhenium
CN105969985B (en) * 2016-03-07 2018-08-24 紫金矿业集团股份有限公司 The method of synthetical recovery rhenium and copper from Copper making spent acid
CN106834715B (en) * 2016-12-21 2018-09-18 中南大学 A kind of method of comprehensive utilization of arsenic-containing material
CN107988487A (en) * 2017-10-30 2018-05-04 四川英创环保科技有限公司 A kind of lead skim wet oxidation decomposition technique
CN107974557A (en) * 2017-12-04 2018-05-01 阳谷祥光铜业有限公司 A kind of method that rhenium is extracted from rich rhenium slag
CN110157909A (en) * 2018-01-29 2019-08-23 安徽华晶微电子材料科技有限公司 Molybdenum metal materials industry recovery method in a kind of waste
CN108677010A (en) * 2018-06-14 2018-10-19 中核通辽铀业有限责任公司 A kind of ground-dipping uranium extraction comprehensive recycling process
CN108929960A (en) * 2018-07-23 2018-12-04 安徽华西稀有金属材料有限公司 A method of ammonium perrhenate is prepared from rhenium-containing solution
CN109930004A (en) * 2019-04-12 2019-06-25 江西铜业股份有限公司 A kind of method of arsenic filter cake resource utilization
CN112708762A (en) * 2020-11-30 2021-04-27 核工业北京化工冶金研究院 Method for preparing potassium perrhenate through back-extraction crystallization
CN114059077B (en) * 2021-10-27 2023-10-20 湖南有色金属研究院有限责任公司 Treatment method of arsenic filter cake

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100420761C (en) * 2007-05-18 2008-09-24 锦州沈宏集团股份有限公司 Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum
CN102162033A (en) * 2011-04-02 2011-08-24 张在海 Method for leaching copper and rhenium from high-sulfur high-arsenic rhenium-containing waste material by thermophilic bacteria

Also Published As

Publication number Publication date
CN102433439A (en) 2012-05-02

Similar Documents

Publication Publication Date Title
CN102433439B (en) Method for recovering rhenium from arsenic filter cake
CN102491287B (en) Process for separating and recovering selenium from selenium-containing material
CN105543485B (en) A kind of method that valuable metal is separated and recovered from copper anode mud
CN102534255B (en) Wet-fire combined smelting process for antimony or bismuth
CN102363522B (en) Technology for extracting selenium from low-grade selenium-containing material
CN102586627B (en) Method for recovering bismuth from bismuth slag
CN105543479B (en) A kind of comprehensive recovering process of bismuth matte
EP2683840B1 (en) Gold and silver extraction technology
CN101328539A (en) Oxidation oven ash hydrometallurgical leaching process
CN112063854B (en) Method for comprehensively recovering bismuth, silver and copper metals by taking precious lead as raw material
CN102363839A (en) Process for recovering silver, lead and bismuth from silver-bearing soot comprehensively
CN104017991A (en) Process for efficiently and selectively separating copper in lead copper matte
CN104445101A (en) Method for extracting copper and tellurium from copper telluride residues
CN108754167A (en) A kind of method that Copper making flue dust efficiently separates copper arsenic
CN103882236A (en) Method for processing high-sulfur copper dust and recovering copper by employing a wet process
CN102230083A (en) Method for separating copper from lead copper matte
CN102392136B (en) Process for comprehensively recovering high arsenic polymetallic material
CN110172570A (en) A kind of processing method of precious metals containing lead
JP7016463B2 (en) How to collect tellurium
CN102586584B (en) Method for selectively separating valuable metals from complex lead-containing precious metal material
CN103484694A (en) Method for extracting bismuth from copper-bismuth concentrate
CN105967153A (en) Technology for recovering tellurium from high-tellurium slag
CN107739829A (en) The recovery method of nickel element, cobalt element, copper and Zn-ef ficiency in smelting laterite-nickel ores and in slag
CN104004907A (en) Method for separating copper from lead matte and comprehensively utilizing lead matte
CN109402392B (en) Method for extracting tellurium from copper anode slime

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20130123

Termination date: 20181216

CF01 Termination of patent right due to non-payment of annual fee