CN114672648A - Method for treating N263 alkaline extraction raffinate - Google Patents
Method for treating N263 alkaline extraction raffinate Download PDFInfo
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- CN114672648A CN114672648A CN202210221134.0A CN202210221134A CN114672648A CN 114672648 A CN114672648 A CN 114672648A CN 202210221134 A CN202210221134 A CN 202210221134A CN 114672648 A CN114672648 A CN 114672648A
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- 238000000605 extraction Methods 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 17
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 60
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- 238000000746 purification Methods 0.000 claims abstract description 28
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910052721 tungsten Inorganic materials 0.000 claims abstract description 17
- 239000010937 tungsten Substances 0.000 claims abstract description 17
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 13
- 238000003723 Smelting Methods 0.000 claims abstract description 9
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 9
- 239000007787 solid Substances 0.000 claims abstract description 9
- 238000004064 recycling Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 239000012074 organic phase Substances 0.000 claims abstract description 5
- 239000002699 waste material Substances 0.000 claims abstract description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 16
- 238000003756 stirring Methods 0.000 claims description 12
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 10
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 claims description 8
- 239000000706 filtrate Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 4
- 239000003350 kerosene Substances 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 238000005352 clarification Methods 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 abstract description 19
- 239000011733 molybdenum Substances 0.000 abstract description 13
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 abstract description 10
- 229910052751 metal Inorganic materials 0.000 abstract description 3
- 239000002184 metal Substances 0.000 abstract description 3
- 239000003513 alkali Substances 0.000 abstract 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 abstract 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 abstract 1
- 230000008569 process Effects 0.000 description 7
- 239000010802 sludge Substances 0.000 description 7
- MGRWKWACZDFZJT-UHFFFAOYSA-N molybdenum tungsten Chemical compound [Mo].[W] MGRWKWACZDFZJT-UHFFFAOYSA-N 0.000 description 6
- 238000005070 sampling Methods 0.000 description 6
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- 229910052698 phosphorus Inorganic materials 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 238000005303 weighing Methods 0.000 description 3
- 230000004075 alteration Effects 0.000 description 2
- 238000000975 co-precipitation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical group C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 241001062472 Stokellia anisodon Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 238000000643 oven drying Methods 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 125000002467 phosphate group Chemical group [H]OP(=O)(O[H])O[*] 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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- 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
- C22B34/00—Obtaining refractory metals
- C22B34/30—Obtaining chromium, molybdenum or tungsten
- C22B34/34—Obtaining molybdenum
-
- 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
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- 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
- C22B34/00—Obtaining refractory metals
- C22B34/30—Obtaining chromium, molybdenum or tungsten
- C22B34/36—Obtaining tungsten
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to the field of tungsten and molybdenum smelting, and relates to a method for treating N263 alkaline extraction raffinate, which comprises the steps of pH value adjustment, extraction, purification conversion, recycling decomposition and the like. The method comprises the steps of firstly adjusting the pH value, adding solid NaOH into N263 alkaline extraction raffinate, controlling the concentration of free alkali in the raffinate to be more than or equal to 5g/L, and then performing 2-stage countercurrent extraction by using an N263 extractant to further reduce WO in the raffinate3Mo concentration, reduced circulation of WO3The Mo metal content and the unsaturated loaded organic phase enter the main flow of N263 extraction, the raffinate is purified and converted by magnesium oxide/sodium hydroxide to remove P in the raffinate, and HCO in the raffinate is simultaneously removed3Conversion to CO3 2‑The purified and converted residual liquid is used for decomposing tungsten smelting waste, and the high-efficiency treatment of the N263 alkaline extraction raffinate is finally completed, so that the WO is reduced3And Mo loss.
Description
[ technical field ] A method for producing a semiconductor device
The invention relates to the field of tungsten and molybdenum smelting, and relates to a method for treating N263 alkaline extraction raffinate.
[ background of the invention ]
Tungsten and molybdenum belong to rare metals and are widely applied. Currently, the tungsten-molybdenum capacity of China accounts for about 90% of the world. With the increasing consumption of high-quality tungsten-molybdenum mineral resources, the utilization of some tungsten-molybdenum wastes difficult to smelt is gradually paid attention, wherein the tungsten-molybdenum wastes are mainly represented by low-grade high-molybdenum high-phosphorus scheelite. In order to improve the utilization technology of low-grade high-molybdenum high-phosphorus scheelite, a Zhongwei professor team of Zhang Guiqing professor team of Zhongnan university, a Wanlinsheng professor team of Jiangxi Ringchang university and the like carry out deep technical development, the technology of mixed sulfur and phosphorus acid/the technology of high-pressure decomposition of sodium carbonate-N263 alkaline extraction/the technology of decomposition of phosphate and the like are invented, the extraction rate of tungsten and molybdenum is obviously improved, and the production cost is reduced. In the process of treating the low-grade high-molybdenum high-phosphorus scheelite N263 extraction by the sodium carbonate high-pressure decomposition-N263 alkaline extraction technology, a large amount of raffinate can be generated, impurity elements such as P can be gradually accumulated in the part of raffinate, and meanwhile, the impurity elements such as P are directly removed, so that the coprecipitation of tungsten and molybdenum can be caused, the recovery rate of the tungsten and molybdenum is reduced, and the production operation is not facilitated.
Aiming at the problem of difficult treatment of the N263 alkaline extraction raffinate, the invention develops a treatment method of the N263 alkaline extraction raffinate, and the treatment of the steps of pH value adjustment, extraction, purification conversion, recycling decomposition and the like is carried out to realize the WO 263 alkaline extraction raffinate3And Mo is recovered, so that the loss of tungsten and molybdenum in the purification and conversion process is reduced, the closed-loop recycling of sodium carbonate in the raffinate is realized, the consumption of auxiliary materials is reduced, and the economic and environmental benefits are obviously improved.
[ summary of the invention ]
The invention aims to overcome the defects of the prior art and provides a method for treating N263 alkaline extraction raffinate, which can be used for efficiently treating the N263 alkaline extraction raffinate, improving the recovery rate of tungsten and molybdenum, reducing the coprecipitation loss of the tungsten and the molybdenum in a purification and conversion process, realizing the closed cycle utilization of sodium carbonate in the raffinate, reducing the consumption of auxiliary materials and improving the economic and environmental benefits.
The invention discloses a method for treating N263 alkaline extraction raffinate, which comprises the following steps:
(1) adjusting the pH value: adding solid NaOH into the N263 alkaline extraction raffinate, stirring and dissolving, controlling the concentration of free NaOH to be more than 5g/L, and entering the next link after the pH value is adjusted.
(2) Extraction: the feed liquid obtained in the step (1) is subjected to 2-stage countercurrent extraction, and the extraction system comprises about N26340 percent, about 30 percent of sulfonated kerosene and about 30 percent of octanol, the extraction ratio is O/A (1/1), and the extraction flow ratio is VO/VA1/2-1/3, the extraction time is 10min, the clarification time is 5-10min, the extraction is completed, the unsaturated load organic phase enters the main process of N263 alkaline extraction, and the raffinate enters the next link.
(3) Purification and transformation: adding MgO/NaOH into the raffinate for purification and conversion, wherein the addition of MgO is 20-80g/L, the addition of NaOH is 5-10g/L, the purification and conversion time is 60-120min, the stirring speed is 60-120r/min, the purification and conversion temperature is 80-95 ℃, the purification and conversion is finished, and the next link is entered.
(4) Recycling and decomposing: the raffinate after purification and conversion is used for decomposing tungsten smelting waste, the liquid-solid ratio of prepared slurry is controlled to be 3/1-4/1, and Na2CO3The concentration of the filtrate is 100-160g/L, the decomposition temperature is 180-200 ℃, the decomposition time is 120-180min, the stirring speed is 60-100r/min, the decomposition is finished, the filtration and washing are carried out, the filter residue is collected and treated, and the filtrate returns to extract WO3Mo main flow.
Compared with the prior art, the invention has the following advantages:
by adjusting the pH value, extracting, purifying, converting, recycling and decomposing, the extraction of tungsten and molybdenum, the removal of P and other impurity elements, HCO and the like in the N263 alkaline extraction raffinate are completed 3 -Conversion of CO3 2-Not only increasing the ratio of the valuable metal WO3And Mo, realizes the closed cycle utilization of sodium carbonate, reduces the consumption of auxiliary materials, and is a high-efficiency N263 alkaline extraction raffinate method.
[ description of the drawings ]
The following detailed description of embodiments of the invention is provided in conjunction with the appended drawings, in which:
FIG. 1 is a process flow diagram of the present invention;
[ detailed description ] embodiments
The invention is further illustrated by the following example and by the accompanying figure 1.
Example 1
In this example, the N263 alkaline raffinate was obtained from a tungsten-molybdenum smeltery, and the sampling and detecting result was WO312.21g/L, Mo1.43g/L, P0.65g/L and total C (sodium carbonate or sodium bicarbonate) 116.54 g/L.
(1) Adjusting the pH value: adding solid NaOH into the N263 alkaline extraction raffinate, stirring and dissolving to obtain free NaOH with the concentration of 6.8g/L, and after the pH value is adjusted, entering the next link.
(2) And (3) extraction: the feed liquid obtained in the step (1) is subjected to 2-stage countercurrent extraction, the extraction system comprises N26340%, 30% of sulfonated kerosene by volume and 30% of octanol by volume, the extraction ratio is O/A (1/1), and the extraction flow ratio is VO/VA1/2, extraction time 10min, clarification time 10min, extraction completed, WO in raffinate3The Mo concentration is 0.79g/L and 0.13g/L respectively, the unsaturated load organic phase enters the main process of N263 alkaline extraction, and the raffinate enters the next link.
(3) Purification and transformation: adding MgO/NaOH into the raffinate for purification and conversion, wherein the addition of MgO is 20g/L, the addition of NaOH is 8g/L, the purification and conversion time is 60min, the stirring speed is 60r/min, the purification and conversion temperature is 90 ℃, completing the purification and conversion, sampling and detecting, WO3、Mo、Na2CO3The concentrations of NaOH and P are respectively 0.62g/L,0.11g/L,108.22g/L, 5.5g/L and 0.02g/L, the removal rate of P is 96.92 percent, the purification and conversion are finished, and the next link is entered.
(4) Recycling and decomposing: the raffinate after purification and conversion is used for decomposing the environment-friendly sludge for tungsten smelting (WO)36.51 percent and Mo2.36 percent) and is called as the environment-friendly sludge for tungsten smelting 500g, the environment-friendly sludge is placed in a high-pressure kettle with the volume of 5000L, the liquid-solid ratio of the prepared slurry is controlled to be 3/1, and Na is added2CO3Has a concentration of 108.22g/L in minutesDecomposing at 200 deg.C for 120min under stirring at 60r/min, filtering, washing, oven drying the residue, weighing 454.22g, and sampling WO3Mo content of 0.21% and Mo content of 0.11%, respectively, WO3The leaching rates of Mo and Mo are 97.07% and 95.77% respectively, and the filtrate is returned to extract WO3Mo main flow.
Example 2
In this example, the N263 alkaline raffinate was obtained from a tungsten-molybdenum smeltery, and the sampling and detecting result was WO36.33g/L, Mo1.08g/L, P0.35, total C (sodium carbonate or sodium bicarbonate) 125.79 g/L.
(1) Adjusting the pH value: adding solid NaOH into the N263 alkaline extraction raffinate, stirring and dissolving to obtain free NaOH with the concentration of 5.8g/L, and adjusting the pH value to be finished, so that the next link is performed.
(2) Extraction: the feed liquid obtained in the step (1) is subjected to 2-stage countercurrent extraction, and the extraction system comprises N26340%, 30% of sulfonated kerosene by volume and 30% of octanol by volume, wherein the extraction ratio is O/A1/1, and the extraction flow ratio is VO/VA1/3, extracting for 10min, clarifying for 10min, and extracting to obtain raffinate containing WO3The Mo concentration is 0.35g/L and 0.10g/L respectively, the unsaturated load organic phase enters the main process of N263 alkaline extraction, and the raffinate enters the next link.
(3) Purifying and converting: adding MgO/NaOH into the raffinate for purification and conversion, wherein the addition of MgO is 20g/L, the addition of NaOH is 6g/L, the purification and conversion time is 60min, the stirring speed is 60r/min, the purification and conversion temperature is 95 ℃, completing the purification and conversion, sampling and detecting, WO3、Mo、Na2CO3The concentration of NaOH and P is 0.30g/L,0.08g/L, 116.54g/L, 5.0g/L and 0.011 respectively, the removal rate of P is 96.86 percent, the purification and conversion are finished, and the next link is entered.
(4) Recycling and decomposing: the raffinate after purification and conversion is used for decomposing the environment-friendly sludge for tungsten smelting (WO)37.89 percent and Mo2.75 percent) of the total weight of the sludge, weighing 500g of the environment-friendly sludge for tungsten smelting, placing the sludge in a high pressure kettle with the volume of 5000L, controlling the liquid-solid ratio of the prepared slurry to be 4/1 and Na 2CO3The concentration of (A) is 116.54g/L, the decomposition temperature is 195 ℃, the decomposition time is 180min, and the stirring speed is 60rMin, decomposition, filtration and washing, drying and collecting filter residue, weighing 441.32g, sampling and measuring WO3Mo content of 0.15% and Mo content of 0.10%, respectively, WO3The leaching rates of Mo and Mo are respectively 98.32% and 96.79%, and the filtrate is returned to extract WO3Mo main flow.
The above description is only a preferred embodiment of the present invention, and it should be noted that a person skilled in the art can make various changes, modifications, substitutions and alterations to the embodiments without departing from the technical principles of the present invention, and such changes, modifications, substitutions and alterations should also be regarded as the protection scope of the present invention.
Claims (1)
1. A method for processing N263 alkaline extraction raffinate is characterized in that: comprises the following steps:
(1) adjusting the pH value: adding solid NaOH into the N263 alkaline extraction raffinate, stirring and dissolving, controlling the concentration of free NaOH to be more than 5g/L, and entering the next link after the pH value is adjusted;
(2) and (3) extraction: the feed liquid obtained in the step (1) is subjected to 2-stage countercurrent extraction, and the extraction system consists of about N26340 percent, about 30 percent of sulfonated kerosene and about 30 percent of octanol, the extraction ratio is O/A (1/1), and the extraction flow ratio is V O/VAWhen the extraction time is 1/2-1/3, the extraction time is 10min, the clarification time is 5-10min, the extraction is completed, the unsaturated loaded organic phase enters the main N263 alkaline extraction process, and the raffinate enters the next link;
(3) purifying and converting: adding MgO/NaOH into the raffinate for purification and conversion, wherein the addition of MgO is 20-80g/L, the addition of NaOH is 5-10g/L, the purification and conversion time is 60-120min, the stirring speed is 60-120r/min, the purification and conversion temperature is 80-95 ℃, the purification and conversion is finished, and the next link is entered;
(4) recycling and decomposing: the raffinate after purification and conversion is used for decomposing tungsten smelting waste, the liquid-solid ratio of prepared slurry is controlled to be 3/1-4/1, and Na2CO3The concentration of the filtrate is 100-160g/L, the decomposition temperature is 180-200 ℃, the decomposition time is 120-180min, the stirring speed is 60-100r/min, the decomposition is finished, the filtration and washing are carried out, the filter residue is collected and treated, and the filtrate returns to extract WO3Mo main flow.
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102634670A (en) * | 2012-05-11 | 2012-08-15 | 河南科技大学 | Treating method for wastes in tungsten molybdenum complexing extraction technology |
| KR20140006409A (en) * | 2012-07-05 | 2014-01-16 | 에쓰대시오일 주식회사 | Manufacturing method of w-containing oxidative desulfurization catalyst |
| CN104120257A (en) * | 2014-07-24 | 2014-10-29 | 厦门钨业股份有限公司 | Method for extracting and separating tungsten molybdenum |
| CN104561545A (en) * | 2013-10-14 | 2015-04-29 | 修水县华伟矿产资源再生有限公司 | Method for separating tungsten and molybdenum from tungsten molybdenum ore |
| CN105525094A (en) * | 2015-12-23 | 2016-04-27 | 北京大学 | Method for extracting tungsten from alkaline crude sodium tungstate solution |
| CN108396142A (en) * | 2018-05-03 | 2018-08-14 | 中南大学 | A kind of method of acid decomposed by phosphoric acid molybdenum calcining |
| CN109306403A (en) * | 2018-10-27 | 2019-02-05 | 湖南懋天世纪新材料有限公司 | The processing method of quaternary ammonium salt alkaline extraction three-phase flocculate in tungsten hydrometallurgy |
| CN113699387A (en) * | 2021-07-16 | 2021-11-26 | 信丰华锐钨钼新材料有限公司 | Method for deeply separating tungsten in sodium molybdate solution by extraction method |
| CN113720987A (en) * | 2021-08-11 | 2021-11-30 | 信丰华锐钨钼新材料有限公司 | Method for removing tungsten, molybdenum, phosphorus and polyacid in tungsten smelting macroporous resin desorption solution |
-
2022
- 2022-03-07 CN CN202210221134.0A patent/CN114672648A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102634670A (en) * | 2012-05-11 | 2012-08-15 | 河南科技大学 | Treating method for wastes in tungsten molybdenum complexing extraction technology |
| KR20140006409A (en) * | 2012-07-05 | 2014-01-16 | 에쓰대시오일 주식회사 | Manufacturing method of w-containing oxidative desulfurization catalyst |
| CN104561545A (en) * | 2013-10-14 | 2015-04-29 | 修水县华伟矿产资源再生有限公司 | Method for separating tungsten and molybdenum from tungsten molybdenum ore |
| CN104120257A (en) * | 2014-07-24 | 2014-10-29 | 厦门钨业股份有限公司 | Method for extracting and separating tungsten molybdenum |
| CN105525094A (en) * | 2015-12-23 | 2016-04-27 | 北京大学 | Method for extracting tungsten from alkaline crude sodium tungstate solution |
| CN108396142A (en) * | 2018-05-03 | 2018-08-14 | 中南大学 | A kind of method of acid decomposed by phosphoric acid molybdenum calcining |
| CN109306403A (en) * | 2018-10-27 | 2019-02-05 | 湖南懋天世纪新材料有限公司 | The processing method of quaternary ammonium salt alkaline extraction three-phase flocculate in tungsten hydrometallurgy |
| CN113699387A (en) * | 2021-07-16 | 2021-11-26 | 信丰华锐钨钼新材料有限公司 | Method for deeply separating tungsten in sodium molybdate solution by extraction method |
| CN113720987A (en) * | 2021-08-11 | 2021-11-30 | 信丰华锐钨钼新材料有限公司 | Method for removing tungsten, molybdenum, phosphorus and polyacid in tungsten smelting macroporous resin desorption solution |
Non-Patent Citations (1)
| Title |
|---|
| 卢博;谢方浩;邓声华;乔珊;杨幼明;: "N263-仲辛醇-煤油体系萃取分离钨钼", 硬质合金, no. 05, 15 October 2011 (2011-10-15), pages 311 - 315 * |
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