CN101050489A - Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum - Google Patents
Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum Download PDFInfo
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- CN101050489A CN101050489A CNA2007100113813A CN200710011381A CN101050489A CN 101050489 A CN101050489 A CN 101050489A CN A2007100113813 A CNA2007100113813 A CN A2007100113813A CN 200710011381 A CN200710011381 A CN 200710011381A CN 101050489 A CN101050489 A CN 101050489A
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
This invention relates to a method for extracting Re from flue dust and tail gas rinsing solution of Mo concentrate calcination. The method comprises: (1) adding water to flue dust, leaching out Re in the flue dust to obtain Re-containing leaching solution; (2) adjusting the pH value of the Re-containing leaching solution and tail gas rinsing solution to 5 with ammonium bicarbonate so that Mo, Fe, Cu and Zn ions are converted into hydroxides, separated from Re and precipitated, and filtering to obtain Re-containing solution for extraction; (3) extracting with extractant so that Re enters into the extractant, which is named enriched oil; (4) back-extracting the enriched oil with 3 N ammonia solution so that Re enters into the back extraction solution; (5) adding the back extraction solution into an ion exchange system so that Re is adsorbed onto the resin; (6) preparing 5-10% ammonium thiocyanate solution, adding ammonia solution to adjust the pH value to 8-9, and desorbing Re adsorbed onto the resin to obtain Re-containing desorption solution; (7) evaporating the desorption solution, concentrating, and crystallizing to obtain ammonium perrhenate product.
Description
Technical field
The invention belongs to a kind of separating and extracting method of rhenium, particularly a kind of method of from calcining molybdenum ore concentrate flue dust and leacheate, extracting rhenium.
Background technology
Rhenium is a kind of important industrial raw material, and price is very expensive.At present, people also do not find the suitable mineral of rhenium, and it all is to be present in the molybdenum glance as oligo-elements, or are present in niobite, ytterbite and some magnesium, platinum and the uranium ore as trace substance.At present, rhenium generally is to separate from the roasting gas of producing the generation of molybdenum and copper.The common practice is the solution that obtains rhenium-containing earlier, extracts rhenium by the method for ion-exchange or by method of extraction then.Extract the rhenium alkalescence that acid liquid must be neutralized with the method for ion-exchange, the entrainment loss of rhenium is bigger in N-process, because contain a large amount of sulfate radicals and chlorine root in the solution, sulfate radical and chlorine root are adsorbed onto on the resin, cause the exchange capacity of rhenium little, contain a large amount of impurity in the desorbed solution, need periodic crystallisation, bring difficulty for the purification of rhenium.It is low to extract in its strip liquor of rhenium rhenium-containing concentration with method of extraction, needs could crystallization go out the rehenic acid ammonium through concentrating, and the foreign matter content height, needs just can extract rehenic acid ammonium product through recrystallization repeatedly.Therefore, it is lower to adopt single method to extract the rhenium rate of recovery, and foreign matter content height in the product is difficult to obtain the higher rhenium of purity.
Summary of the invention
The objective of the invention is to solve problems such as the rhenium rate of recovery that prior art exists is low, foreign matter content height, a kind of method of extracting rhenium from calcining molybdenum ore concentrate flue dust and leacheate is provided, improve the rate of recovery of rhenium, obtain highly purified rhenium product.
The present invention is a raw material with the flue dust of calcining molybdenum concentrate generation and the tail gas leacheate of calcining molybdenum concentrate, and its concrete extracting method is:
1, add water in flue dust, liquid-solid ratio is 2～4: 1, and temperature is 80～100 ℃, and the time is 2～3 hours, leaches the rhenium in the flue dust, carries out solid-liquid separation then, filters out solid impurity, obtains the leach liquor of rhenium-containing;
2, with leach liquor and leacheate with the bicarbonate of ammonia PH=5 that neutralizes, make metal ions such as wherein molybdenum, iron, copper, lead form oxyhydroxide, separate with rhenium and precipitate, obtain the preceding liquid of collection of rhenium-containing after filtration;
3, will come together before liquid add in the extraction tank, extract with extraction agent, the organic phase of extraction agent consists of 2.5～5%N235,10～20%TBP, 75～87.5% kerosene, the O/A=1 that is in a ratio of of the extraction agent and the preceding liquid that comes together: 2～4, the residence time is 1～4 minute, make rhenium enter into extraction agent, be called rich oil;
4, rich oil is added in the back extraction groove, with the ammoniacal liquor back extraction of 3N, rich oil and ammoniacal liquor be in a ratio of O/A=2～4: 1, the residence time is 1～4 minute, makes rhenium enter into strip liquor;
5, strip liquor is added in the ion exchange system, ion exchange resin in the ion exchange system is gel type strong basic anion exchange resin 201 * 7, the exchange capacity of resin and rhenium is 50～150mg/ml, rhenium is adsorbed onto on the resin, adsorb surplus liquid rhenium-containing＜0.005g/l, and in turning back to and operation;
6, the ammonium thiocyanate solution of preparation 5～10% adds ammoniacal liquor and is transferred to PH=8～9, resolves the rhenium on the resin, and resolution temperature is 40～60 ℃, and rhenium is resolved from resin, obtains the desorbed solution of rhenium-containing;
7, desorbed solution evaporates under 80～100 ℃ temperature, and condensing crystal promptly obtains the ammonium perrhenate product.
Raffinate is evaporation concentration under 80～100 ℃ temperature, obtains ammonium chloride.
After 1: 9 sulfuric acid cleaned of the oil-poor usefulness regeneration after the back extraction, turn back to reuse in the extraction tank.
The invention has the advantages that, methods such as extraction, ion-exchange and condensing crystal are combined, rhenium in flue dust and the leacheate is carried out comprehensive treating process, it is low to have solved the single method extraction rhenium rate of recovery, problems such as foreign matter content height, can well extract the ammonium perrhenate product, and the purity height of product, grade reaches more than 99%.
Embodiment
Embodiment 1:
1.1, in the flue dust that calcining molybdenum concentrate produces, add water, liquid-solid ratio is 2: 1, temperature is 100 ℃, the time is 2 hours, leaches the rhenium in the flue dust, carries out solid-liquid separation then, filters out solid impurity, obtains the leach liquor of rhenium-containing;
1.2, with leach liquor and leacheate with the bicarbonate of ammonia PH=5 that neutralizes, make metal ions such as wherein molybdenum, iron, copper, lead form oxyhydroxide, separate with rhenium and precipitate, obtain the preceding liquid of collection of rhenium-containing after filtration;
1.3, will come together before liquid add in the extraction tank, extract with extraction agent, the organic phase of extraction agent consists of 2.5%N235 10%TBP 87.5% kerosene, the O/A=1 that is in a ratio of of the extraction agent and the preceding liquid that comes together: 2, the residence time is 1 minute, makes rhenium enter into extraction agent, is called rich oil, raffinate is evaporation concentration under 80 ℃ temperature, obtains ammonium chloride;
1.4, rich oil is added in the back extraction groove, with the ammoniacal liquor back extraction of 3N, rich oil and ammoniacal liquor be in a ratio of O/A=4: 1, the residence time is 1 minute, makes rhenium enter into strip liquor, 1: 9 the sulfuric acid cleaned of oil-poor usefulness after the back extraction turns back to reuse in the extraction tank after regenerating;
1.5, strip liquor is added in the ion exchange system, ion exchange resin in the ion exchange system is gel type strong basic anion exchange resin 201 * 7, the exchange capacity of resin and rhenium is 50mg/ml, rhenium is adsorbed onto on the resin, adsorb surplus liquid rhenium-containing＜0.005g/l, and in turning back to and operation;
1.6, preparation 5% ammonium thiocyanate solution, add ammoniacal liquor and be transferred to PH=8, resolve the rhenium on the resin, resolution temperature is 40 ℃, and rhenium is resolved from resin, obtains the desorbed solution of rhenium-containing;
1.7, desorbed solution evaporates under 80 ℃ temperature, condensing crystal promptly obtains the ammonium perrhenate product.
Embodiment 2:
2.1, in the flue dust that calcining molybdenum concentrate produces, add water, liquid-solid ratio is 4: 1, temperature is 80 ℃, the time is 2.5 hours, leaches the rhenium in the flue dust, carries out solid-liquid separation then, filters out solid impurity, obtains the leach liquor of rhenium-containing;
2.2, with leach liquor and leacheate with the bicarbonate of ammonia PH=5 that neutralizes, make metal ions such as wherein molybdenum, iron, copper, lead form oxyhydroxide, separate with rhenium and precipitate, obtain the preceding liquid of collection of rhenium-containing after filtration;
2.3, will come together before liquid add in the extraction tank, extract with extraction agent, the organic phase of extraction agent consists of 5%N235 20%TBP 75% kerosene, the O/A=1 that is in a ratio of of the extraction agent and the preceding liquid that comes together: 4, the residence time is 4 minutes, makes rhenium enter into extraction agent, is called rich oil, raffinate is evaporation concentration under 100 ℃ temperature, obtains ammonium chloride;
2.4, rich oil is added in the back extraction groove, with the ammoniacal liquor back extraction of 3N, rich oil and ammoniacal liquor be in a ratio of O/A=3: 1, the residence time is 4 minutes, makes rhenium enter into strip liquor, 1: 9 the sulfuric acid cleaned of oil-poor usefulness after the back extraction turns back to reuse in the extraction tank after regenerating;
2.5, strip liquor is added in the ion exchange system, ion exchange resin in the ion exchange system is gel type strong basic anion exchange resin 201 * 7, the exchange capacity of resin and rhenium is 150mg/ml, rhenium is adsorbed onto on the resin, adsorb surplus liquid rhenium-containing＜0.005g/l, and in turning back to and operation;
2.6, preparation 10% ammonium thiocyanate solution, add ammoniacal liquor and be transferred to PH=9, resolve the rhenium on the resin, resolution temperature is 50 ℃, and rhenium is resolved from resin, obtains the desorbed solution of rhenium-containing;
2.7, desorbed solution evaporates under 100 ℃ temperature, condensing crystal promptly obtains the ammonium perrhenate product.
Embodiment 3:
3.1, in the flue dust that calcining molybdenum concentrate produces, add water, liquid-solid ratio is 3: 1, temperature is 90 ℃, the time is 3 hours, leaches the rhenium in the flue dust, carries out solid-liquid separation then, filters out solid impurity, obtains the leach liquor of rhenium-containing;
3.2, with leach liquor and leacheate with the bicarbonate of ammonia PH=5 that neutralizes, make metal ions such as wherein molybdenum, iron, copper, lead form oxyhydroxide, separate with rhenium and precipitate, obtain the preceding liquid of collection of rhenium-containing after filtration;
3.3, will come together before liquid add in the extraction tank, extract with extraction agent, the organic phase of extraction agent consists of 4%N235 16%TBP 80% kerosene, the O/A=1 that is in a ratio of of the extraction agent and the preceding liquid that comes together: 3, the residence time is 2 minutes, makes rhenium enter into extraction agent, is called rich oil, raffinate is evaporation concentration under 90 ℃ temperature, obtains ammonium chloride;
3.4, rich oil is added in the back extraction groove, with the ammoniacal liquor back extraction of 3N, rich oil and ammoniacal liquor be in a ratio of O/A=2: 1, the residence time is 2 minutes, makes rhenium enter into strip liquor, 1: 9 the sulfuric acid cleaned of oil-poor usefulness after the back extraction turns back to reuse in the extraction tank after regenerating;
3.5, strip liquor is added in the ion exchange system, ion exchange resin in the ion exchange system is gel type strong basic anion exchange resin 201 * 7, the exchange capacity of resin and rhenium is 100mg/ml, rhenium is adsorbed onto on the resin, adsorb surplus liquid rhenium-containing＜0.005g/l, and in turning back to and operation;
3.6, preparation 8% ammonium thiocyanate solution, add ammoniacal liquor and be transferred to PH=8.5, resolve the rhenium on the resin, resolution temperature is 60 ℃, and rhenium is resolved from resin, obtains the desorbed solution of rhenium-containing;
3.7, desorbed solution evaporates under 90 ℃ temperature, condensing crystal promptly obtains the ammonium perrhenate product.
Claims (3)
1, a kind of method of extracting rhenium from calcining molybdenum ore concentrate flue dust and leacheate is a raw material with the flue dust of calcining molybdenum concentrate generation and the tail gas leacheate of calcining molybdenum concentrate, it is characterized in that, it is to extract according to following method:
(1) add water in flue dust, liquid-solid ratio is 2～4: 1, and temperature is 80～100 ℃, and the time is 2～3 hours, leaches the rhenium in the flue dust, carries out solid-liquid separation then, filters out solid impurity, obtains the leach liquor of rhenium-containing;
(2) with leach liquor and leacheate with the bicarbonate of ammonia PH=5 that neutralizes, make metal ions such as wherein molybdenum, iron, copper, lead form oxyhydroxide, separate with rhenium and precipitate, obtain the preceding liquid of collection of rhenium-containing after filtration;
(3) will come together before liquid add in the extraction tank, extract with extraction agent, the organic phase of extraction agent consists of 2.5～5%N235,10～20%TBP, 75～87.5% kerosene, the O/A=1 that is in a ratio of of the extraction agent and the preceding liquid that comes together: 2～4, the residence time is 1～4 minute, make rhenium enter into extraction agent, be called rich oil;
(4) rich oil is added in the back extraction groove, with the ammoniacal liquor back extraction of 3N, rich oil and ammoniacal liquor be in a ratio of O/A=2～4: 1, the residence time is 1～4 minute, makes rhenium enter into strip liquor;
(5) strip liquor is added in the ion exchange system, ion exchange resin in the ion exchange system is gel type strong basic anion exchange resin 201 * 7, the exchange capacity of resin and rhenium is 50～150mg/ml, rhenium is adsorbed onto on the resin, adsorb surplus liquid rhenium-containing＜0.005g/l, and in turning back to and operation;
(6) ammonium thiocyanate solution of preparation 5～10% adds ammoniacal liquor and is transferred to PH=8～9, resolves the rhenium on the resin, and resolution temperature is 40～60 ℃, and rhenium is resolved from resin, obtains the desorbed solution of rhenium-containing;
(7) desorbed solution evaporates under 80～100 ℃ temperature, and condensing crystal promptly obtains the ammonium perrhenate product.
2, the method for extracting rhenium from calcining molybdenum ore concentrate flue dust and leacheate according to claim 1 is characterized in that raffinate is evaporation concentration under 80～100 ℃ temperature, obtains ammonium chloride.
3, the method for extracting rhenium from calcining molybdenum ore concentrate flue dust and leacheate according to claim 1 is characterized in that, after 1: 9 sulfuric acid cleaned of the oil-poor usefulness regeneration after the back extraction, turns back to reuse in the extraction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100113813A CN100420761C (en) | 2007-05-18 | 2007-05-18 | Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum |
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| CNB2007100113813A CN100420761C (en) | 2007-05-18 | 2007-05-18 | Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum |
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| CN101050489A true CN101050489A (en) | 2007-10-10 |
| CN100420761C CN100420761C (en) | 2008-09-24 |
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| CNB2007100113813A Expired - Fee Related CN100420761C (en) | 2007-05-18 | 2007-05-18 | Method for extracting rhenium from eluate of flue ash generated by baking enriched ore of molybdenum |
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Cited By (22)
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|---|---|---|---|---|
| CN101469377B (en) * | 2007-12-25 | 2010-09-08 | 江西铜业集团公司 | Technique for extracting rhenium in recovered solution by centrifuge extracting machine |
| CN102251107A (en) * | 2011-07-06 | 2011-11-23 | 湖南稀土金属材料研究院 | Method for treating rhenium-containing raw material |
| CN102433439A (en) * | 2011-12-16 | 2012-05-02 | 湖南有色金属研究院 | Method for recovering rhenium from arsenic filter cake |
| CN102628111A (en) * | 2012-04-06 | 2012-08-08 | 阳谷祥光铜业有限公司 | Method for extracting rhenium from rhenium-rich concentrates |
| CN102660676A (en) * | 2012-05-22 | 2012-09-12 | 陕西炼石矿业有限公司 | Method for separating rhenium and molybdenum in molybdenum-rhenium ore concentrate |
| CN102703737A (en) * | 2012-06-28 | 2012-10-03 | 青岛阿库卡稀有金属有限公司 | Method for extracting and separating rhenium from rhenium-containing slag |
| CN102703711A (en) * | 2012-06-28 | 2012-10-03 | 株洲凯特高新材料有限公司 | Method for extracting rhenium from rhenium-containing waste liquor |
| CN102703716A (en) * | 2012-06-28 | 2012-10-03 | 扶元初 | Method for extracting rhenium from rhenium-containing smoke tail gas |
| CN102732713A (en) * | 2012-06-26 | 2012-10-17 | 西部鑫兴金属材料有限公司 | Method for separating and recovering sediments after processing rhenium molybdenum concentrate-containing high lead |
| CN103003455A (en) * | 2010-03-16 | 2013-03-27 | 世界资源公司 | A method for recovering rhenium and other metals from rhenium-bearing materials |
| CN103361500A (en) * | 2013-07-25 | 2013-10-23 | 江西铜业股份有限公司 | Separation method of rhenium in rhenium-containing molybdenum calcine |
| CN103436721A (en) * | 2013-07-08 | 2013-12-11 | 贵研铂业股份有限公司 | Preparation method for ammonium rhenate from waste high temperature alloy enriched material |
| CN103866122A (en) * | 2014-01-06 | 2014-06-18 | 东华理工大学 | Method for microbiological leaching of uranium-molybdenum ore and enrichment and separation of uranium and molybdenum |
| CN103924081A (en) * | 2014-04-28 | 2014-07-16 | 北京矿冶研究总院 | Method for recovering molybdenum and rhenium from molybdenum concentrate pressurized leaching solution |
| CN104630509A (en) * | 2015-02-03 | 2015-05-20 | 嵩县开拓者钼业有限公司 | Method for preparing ammonium perrhenate |
| CN105219980A (en) * | 2015-10-30 | 2016-01-06 | 嵩县开拓者钼业有限公司 | A kind of method extracting rhenium |
| CN105543512A (en) * | 2015-12-28 | 2016-05-04 | 中南大学 | Application of nitrogen heterocyclic compound functional ion exchange material to recover rhenium from waste water |
| CN106367599A (en) * | 2016-09-08 | 2017-02-01 | 江西铜业股份有限公司 | Method for extracting rhenium from molybdenum smelting flue gas |
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| CN107460316A (en) * | 2017-07-10 | 2017-12-12 | 核工业北京化工冶金研究院 | A kind of method that low concentration rhenium is reclaimed in immersion liquid from uranium ore |
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| CN112322901A (en) * | 2020-11-04 | 2021-02-05 | 中国地质科学院郑州矿产综合利用研究所 | Method for selectively leaching rhenium from molybdenum concentrate roasting soot |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3710725A1 (en) * | 1987-03-31 | 1988-10-13 | Gock Eberhard | Process for the direct treatment of rhenium-containing molybdenum sulphides with ammonia |
| FR2673617A1 (en) * | 1991-03-06 | 1992-09-11 | Pechiney Recherche | PROCESS FOR SEPARATING RHENIUM FROM ACID SOLUTIONS CONTAINING MOLYBDENE. |
| CN1039437C (en) * | 1991-12-21 | 1998-08-05 | 冯亦初 | MOlybdenum smelting and its comprehensive applications |
-
2007
- 2007-05-18 CN CNB2007100113813A patent/CN100420761C/en not_active Expired - Fee Related
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| CN101469377B (en) * | 2007-12-25 | 2010-09-08 | 江西铜业集团公司 | Technique for extracting rhenium in recovered solution by centrifuge extracting machine |
| CN103003455A (en) * | 2010-03-16 | 2013-03-27 | 世界资源公司 | A method for recovering rhenium and other metals from rhenium-bearing materials |
| CN103003455B (en) * | 2010-03-16 | 2016-03-02 | 世界资源公司 | The method of rhenium and other metals is reclaimed from the material of rhenium-containing |
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| 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 |
| CN112322901A (en) * | 2020-11-04 | 2021-02-05 | 中国地质科学院郑州矿产综合利用研究所 | Method for selectively leaching rhenium from molybdenum concentrate roasting soot |
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