CN103555932B - Method for roasting molybdenum concentrate - Google Patents
Method for roasting molybdenum concentrate Download PDFInfo
- Publication number
- CN103555932B CN103555932B CN201310576583.8A CN201310576583A CN103555932B CN 103555932 B CN103555932 B CN 103555932B CN 201310576583 A CN201310576583 A CN 201310576583A CN 103555932 B CN103555932 B CN 103555932B
- Authority
- CN
- China
- Prior art keywords
- calcining
- liquid
- crystallization
- molybdenum
- sodium sulfate
- 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.)
- Active
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)
Abstract
The invention relates to a method for roasting a molybdenum concentrate. The method comprises the steps of mixing a certain amount of sodium sulfate into the molybdenum concentrate, then forming balls and roasting; performing alkaline leaching on calcine; performing ion exchange adsorption on molybdenum leachate, then performing liquid crystallization to obtain sodium sulfate, and returning the sodium sulfate to serve as a molybdenum concentrate roasting additive; performing molybdenum concentrate ball forming by using a liquid after crystallization. By adopting the method, the chemical dosage of molybdenum calcine alkaline leaching and the production cost can be greatly reduced; moreover, the sodium sulfate obtained through liquid crystallization after the ion exchange adsorption during a molybdenum extraction process flow and the liquid after crystallization can be fully used for performing molybdenum concentrate ball forming, and the wastewater treating amount can be reduced.
Description
One. technical field
The present invention relates to metallurgy industry, relate to a kind of method of calcining molybdenum ore concentrate.
Two. background technology
Molybdenum is a kind of rare metal with multiple high-efficiency high-quality function, is widely used in modern industry with the form of its pure metal, alloy and compound.The molybdenum major part of occurring in nature exists with moly-sulfide form.The core of concentrated molybdenum ore leach molybdenum process is the oxidation of moly-sulfide.The oxidizing process of moly-sulfide mainly contains oxidizing roasting, adds sodium carbonate roasting, acid hot-pressure oxidation, alkaline hot-pressure oxidation, chemical oxidation, electrooxidation etc.At present, the technique that industrial application is more is oxidizing roasting technique.Molybdenum oxide calcining leaches the techniques such as the leaching of general employing ammonia, alkali leaching.Owing to having the advantages such as molybdenum leaching rate is high, adaptability to raw material is strong, the industrial application producer of molybdenum calcining alkali soaking technology gets more and more.
Although the leaching yield of molybdenum calcining alkali leaching molybdenum is high, also come with some shortcomings part, and as the dosing such as sodium hydroxide, sodium carbonate is large, calcining molybdenum content about 48%, during alkali leaching, sodium hydroxide concentration reaches 50% of calcining weight.
Three. summary of the invention
The object of the invention is the deficiency overcoming existing technique, a kind of method of calcining molybdenum ore concentrate is provided, adopt the method, greatly can reduce the dosing of molybdenum calcining alkali leaching, greatly reduce production cost.
The present invention adopts following technical scheme:
Add a certain proportion of sodium sulfate during calcining molybdenum ore concentrate, the sodium sulfate that the attached liquid crystallization of molybdenum leach liquor ion-exchange absorption obtains returns as calcining molybdenum ore concentrate additive, and after utilizing crystallization, liquid carries out concentrated molybdenum ore ball.
Detailed process condition is as follows:
During calcining molybdenum ore concentrate, the addition of sodium sulfate is 5% ~ 20% of concentrated molybdenum ore weight;
During the leaching of calcining alkali, sodium hydroxide concentration is 10% ~ 40% of calcining weight;
During the leaching of calcining alkali, sodium carbonate add-on is 3% ~ 10% of calcining weight;
During the leaching of calcining alkali, chlorine bleach liquor's add-on is 0.2 ~ 0.6m
3/ t calcining.
Per-cent (%) in this specification sheets all refers to mass percent.
Specifically a kind of step of method of calcining molybdenum ore concentrate and processing condition as follows:
1, ball processed: concentrated molybdenum ore allocates the sodium sulfate that the attached liquid crystallization of ion-exchange absorption obtains into, and sodium sulfate addition is 5% ~ 20% of concentrated molybdenum ore weight, mixing, after then utilizing crystallization, liquid carries out ball processed.
2, roasting: concentrated molybdenum ore pelletizing carries out roasting at about 570 DEG C, and roasting time is about 2h.
3, alkali leaching: after concentrated molybdenum ore calcining utilizes crystallization, liquid is sized mixing, add sodium hydroxide, sodium carbonate and chlorine bleach liquor, sodium hydroxide concentration is 10% ~ 40% of calcining weight, and sodium carbonate add-on is 3% ~ 10% of calcining weight, and chlorine bleach liquor's add-on is 0.2 ~ 0.6m
3/ t calcining.
4, ion-exchange: ion-exchange absorption is carried out in the immersion liquid of calcining alkali, obtains the molybdenum stripping liquid of high density after loaded resin desorb.
5, ammonia sinks: after molybdenum stripping liquid regulates the pH value be applicable to, and ammonia is heavy obtains ammonium molybdate.
6, crystallization: the attached liquid of ion-exchange absorption carries out crystallization, obtain liquid after sodium sulfate and crystallization, sodium sulfate returns as concentrated molybdenum ore additive, and after crystallization, liquid is sized mixing for when ball processed and the leaching of calcining alkali.
The method has the following advantages:
1, greatly can reduce the dosing of molybdenum calcining alkali leaching, greatly reduce production cost;
2, after the sodium sulfate that after can making full use of leach molybdenum process flow process intermediate ion exchange adsorption, liquid crystallization obtains and crystallization, liquid carries out concentrated molybdenum ore ball, can reduce wastewater treatment capacity, reduces production cost.
Four. accompanying drawing explanation
Fig. 1 is the schema of the method for a kind of calcining molybdenum ore concentrate of the present invention.
Five. embodiment
Below in conjunction with accompanying drawing 1 and embodiment, the present invention is described in further detail, not as limiting the scope of the present invention.
Embodiment 1:
Certain concentrated molybdenum ore, containing molybdenum 45%, allocates the sodium sulfate of 5% of concentrated molybdenum ore weight into, mixing, utilizes the rear liquid ball of absorption; Concentrated molybdenum ore pelletizing is at 570 DEG C of roasting 2h; Calcining carries out alkali leaching, and sodium hydroxide concentration is 30% of calcining weight, and sodium carbonate add-on is 5% of calcining weight, and chlorine bleach liquor's add-on is 0.2m
3/ t calcining, molybdenum leaching rate is 92%.
Embodiment 2:
Certain concentrated molybdenum ore, containing molybdenum 45%, allocates the sodium sulfate of 10% of concentrated molybdenum ore weight into, mixing, utilizes the rear liquid ball of absorption; Concentrated molybdenum ore pelletizing is at 570 DEG C of roasting 2h; Calcining carries out alkali leaching, and sodium hydroxide concentration is 35% of calcining weight, and sodium carbonate add-on is 7% of calcining weight, and chlorine bleach liquor's add-on is 0.3m
3/ t calcining, molybdenum leaching rate is 95%.
Embodiment 3:
Certain concentrated molybdenum ore, containing molybdenum 45%, allocates the sodium sulfate of 15% of concentrated molybdenum ore weight into, mixing, utilizes the rear liquid ball of absorption; Concentrated molybdenum ore pelletizing is at 570 DEG C of roasting 2h; Calcining carries out alkali leaching, and sodium hydroxide concentration is 40% of calcining weight, and sodium carbonate add-on is 8% of calcining weight, and chlorine bleach liquor's add-on is 0.6m
3/ t calcining, molybdenum leaching rate is 96%.
Embodiment 4:
Certain concentrated molybdenum ore, containing molybdenum 45%, allocates the sodium sulfate of 20% of concentrated molybdenum ore weight into, mixing, utilizes the rear liquid ball of absorption; Concentrated molybdenum ore pelletizing is at 570 DEG C of roasting 2h; Calcining carries out alkali leaching, and sodium hydroxide concentration is 25% of calcining weight, and sodium carbonate add-on is 4% of calcining weight, and chlorine bleach liquor's add-on is 0.2m
3/ t calcining, molybdenum leaching rate is 94%.
Comparative example 1:
Certain concentrated molybdenum ore is containing molybdenum 45%, and at 570 DEG C of roasting 2h, calcining carries out alkali leaching, and sodium hydroxide concentration is 50% of calcining weight, and sodium carbonate add-on is 10% of calcining weight, and chlorine bleach liquor's add-on is 0.7m
3/ t calcining, molybdenum leaching rate is 95%.
Comparative example 2:
Certain concentrated molybdenum ore is containing molybdenum 45%, and at 570 DEG C of roasting 2h, calcining carries out alkali leaching, and sodium hydroxide concentration is 35% of calcining weight, and sodium carbonate add-on is 7% of calcining weight, and chlorine bleach liquor's add-on is 0.3m
3/ t calcining, molybdenum leaching rate is 82%.
Claims (1)
1. the method for a calcining molybdenum ore concentrate, it is characterized in that: step and processing condition as follows: a, ball processed: concentrated molybdenum ore allocates the sodium sulfate that the attached liquid crystallization of ion-exchange absorption obtains into, sodium sulfate addition is 5% ~ 20% of concentrated molybdenum ore weight, mixing, and after then utilizing crystallization, liquid carries out ball processed;
B, roasting: concentrated molybdenum ore pelletizing carries out roasting at about 570 DEG C, and roasting time is about 2h;
C, alkali soak: after concentrated molybdenum ore calcining utilizes crystallization, liquid is sized mixing, add sodium hydroxide, sodium carbonate and chlorine bleach liquor, sodium hydroxide concentration is 10% ~ 40% of calcining weight, and sodium carbonate add-on is 3% ~ 10% of calcining weight, and chlorine bleach liquor's add-on is 0.2 ~ 0.6m
3/ t calcining;
D, ion-exchange: ion-exchange absorption is carried out in the immersion liquid of calcining alkali, obtain the molybdenum stripping liquid of high density after loaded resin desorb;
E, ammonia sink: after molybdenum stripping liquid regulates the pH value be applicable to, and ammonia is heavy obtains ammonium molybdate;
F, crystallization: the attached liquid of ion-exchange absorption carries out crystallization, obtain liquid after sodium sulfate and crystallization, sodium sulfate returns as concentrated molybdenum ore additive, and after crystallization, liquid is sized mixing for when ball processed and the leaching of calcining alkali.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310576583.8A CN103555932B (en) | 2013-11-15 | 2013-11-15 | Method for roasting molybdenum concentrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310576583.8A CN103555932B (en) | 2013-11-15 | 2013-11-15 | Method for roasting molybdenum concentrate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103555932A CN103555932A (en) | 2014-02-05 |
| CN103555932B true CN103555932B (en) | 2015-07-22 |
Family
ID=50010275
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310576583.8A Active CN103555932B (en) | 2013-11-15 | 2013-11-15 | Method for roasting molybdenum concentrate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103555932B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106756122A (en) * | 2016-11-25 | 2017-05-31 | 桂林理工大学 | A kind of method that caustic fusion decomposes molybdenite |
| CN108085487A (en) * | 2017-12-27 | 2018-05-29 | 燕山大学 | The method of molybdenum is leached in a kind of molybdenum concntrate from low-temperature bake |
| CN108715944B (en) * | 2018-05-03 | 2020-02-18 | 中南大学 | One-step alkali leaching method for molybdenum calcine |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4444733A (en) * | 1983-02-28 | 1984-04-24 | Amax Inc. | Process for recovering molybdenum and copper from sulfide concentrates |
| EP0555128A1 (en) * | 1992-02-07 | 1993-08-11 | Eurecat Europeenne De Retraitement De Catalyseurs | Recovery of molybdenum and vanadium from used catalysts |
| CN1386870A (en) * | 2002-04-30 | 2002-12-25 | 云南省冶金研究设计院 | Process for recovering Mo from low-grade molybdenite by dump leaching |
| CN101660045A (en) * | 2009-09-29 | 2010-03-03 | 金堆城钼业股份有限公司 | Method for leaching and recovering molybdenum from ammonia leaching residue |
| CN101792851A (en) * | 2009-11-17 | 2010-08-04 | 灵宝市金源矿业有限责任公司 | Recovery process of low-grade oxidizing molybdenum ore |
| CN101876004A (en) * | 2010-08-03 | 2010-11-03 | 北京科技大学 | Method for recycling rare metal molybdenum from mineral dressing tailings of molybdenum |
| CN101956070A (en) * | 2010-07-07 | 2011-01-26 | 紫金矿业集团股份有限公司 | Recovery method of molybdenum concentrates |
| CN102199704A (en) * | 2011-05-17 | 2011-09-28 | 葫芦岛辉宏有色金属有限公司 | Recycling use method of sodium chloride or sodium sulfate in hydrometallurgy |
-
2013
- 2013-11-15 CN CN201310576583.8A patent/CN103555932B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4444733A (en) * | 1983-02-28 | 1984-04-24 | Amax Inc. | Process for recovering molybdenum and copper from sulfide concentrates |
| EP0555128A1 (en) * | 1992-02-07 | 1993-08-11 | Eurecat Europeenne De Retraitement De Catalyseurs | Recovery of molybdenum and vanadium from used catalysts |
| CN1386870A (en) * | 2002-04-30 | 2002-12-25 | 云南省冶金研究设计院 | Process for recovering Mo from low-grade molybdenite by dump leaching |
| CN101660045A (en) * | 2009-09-29 | 2010-03-03 | 金堆城钼业股份有限公司 | Method for leaching and recovering molybdenum from ammonia leaching residue |
| CN101792851A (en) * | 2009-11-17 | 2010-08-04 | 灵宝市金源矿业有限责任公司 | Recovery process of low-grade oxidizing molybdenum ore |
| CN101956070A (en) * | 2010-07-07 | 2011-01-26 | 紫金矿业集团股份有限公司 | Recovery method of molybdenum concentrates |
| CN101876004A (en) * | 2010-08-03 | 2010-11-03 | 北京科技大学 | Method for recycling rare metal molybdenum from mineral dressing tailings of molybdenum |
| CN102199704A (en) * | 2011-05-17 | 2011-09-28 | 葫芦岛辉宏有色金属有限公司 | Recycling use method of sodium chloride or sodium sulfate in hydrometallurgy |
Non-Patent Citations (1)
| Title |
|---|
| 硫酸化焙烧处理镍钼矿的工艺研究;王志坚;《湖南有色金属》;20090430;第25卷(第2期);25-27 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103555932A (en) | 2014-02-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103540756B (en) | A kind of method processing waste and old neodymium iron boron material dissolution rare earth | |
| CN103266231B (en) | A kind of Tungsten smelting method of high-efficiency cleaning | |
| CN102676814B (en) | Method for removing impurity ferrum in nickel sulfate solution | |
| CN103789552B (en) | Method for recovering rhenium from high-temperature alloy pickle liquor | |
| CN104593611A (en) | Method for efficiently recovering germanium | |
| CN103555932B (en) | Method for roasting molybdenum concentrate | |
| CN104480304B (en) | A kind of method reducing ammonia usage amount in tantalum niobium hydrometallurgy process | |
| CN101824628A (en) | De-ironing method in electrolytic manganese metal production process | |
| CN103695647A (en) | Method for processing copperish electroplating sludge | |
| CN103740930B (en) | A kind of take alkyl trimethyl quaternary ammonium salt as the thiosulfate gold extracting method of additive | |
| CN107640814A (en) | The method of nitrate in in-situ reducing degradation water | |
| CN105821216A (en) | Method for leaching zinc from purification copper, cadmium, cobalt and nickel slag of zinc hydrometallurgy | |
| CN104862494A (en) | Gold leaching process from sulfide gold mine | |
| CN102776370B (en) | Technological method for leaching manganese ore with high spent acid | |
| CN102251103A (en) | Circulating graded leaching method of stone coal acid-leaching vanadium extraction sulfuric acid | |
| CN104404254A (en) | Dechlorinating method | |
| CN104263941B (en) | A kind of technique of comprehensively recovering valuable metal from electroplating sludge | |
| CN103255286B (en) | Method for restraining primary copper sulfide from dissolving in gold concentrate cyaniding process | |
| CN103343244A (en) | Process for separating and purifying molybdenum in low-molybdenum-content tailings | |
| CN106636634B (en) | A kind of technique for being catalyzed Leaching of Gold Using Thiosulfate | |
| CN106507811B (en) | A kind of method of efficient Leaching Uranium in ferro-boron refined ore from uranium-bearing | |
| CN104911361B (en) | The method that steel plant's zinc smoke wet-treating is enriched with zinc oxide concentrate | |
| CN104591104A (en) | Method for recovering tellurium from low-concentration tellurium-containing liquid | |
| CN205398181U (en) | Ion exchange removes electrolysis dechlorination device of chlorine waste water | |
| CN113716757B (en) | Method for removing zinc from extract liquid and application of rare earth saponification wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |