CN102154546A - Method for smelting molybdenum-nickel mineral association by wet process - Google Patents
Method for smelting molybdenum-nickel mineral association by wet process Download PDFInfo
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Abstract
The invention discloses a method for smelting molybdenum-nickel mineral association by wet process, which comprises the steps of: (1) leaching mineral powder: grinding and ball milling raw mineral powder, controlling the solid-to-liquid ratio to be 1: 3, and controlling the reaction temperature to be within the range of 60-90 DEG C and the reaction time to be within the range of 3-4h, wherein the leachate is KClO4, NaClO3 or KMnO4 and 30% of nitric acid or 98% of sulfuric acid; (2) filtering for solid-liquid separation; (3) adjusting the pH value to be approximately equal to 2, precipitating filtrate and obtaining H2MoO4; (4) heating the obtained H2MoO4 for dehydration, and obtaining MoO3; (5) extracting residual molybdenum in the filtrate; (6) using anion exchange resin to absorb nickel, treating and obtaining nickel chloride; and (7) after the nickel is absorbed, treating the obtained solution by quick lime through neutralization. The method is high in recovery rate, simple in technique and short in process flow, the total recovery rate of molybdenum reaches about 98%, the total recovery rate of nickel reaches 94-97%, and the method is environment-friendly; and the wet process is adopted, and the raw ore is not roasted, so that dust and harmful gas are not generated, and the method is beneficial to environmental protection.
Description
Technical field
The present patent application relates to the hydrometallurgy field, is specifically related to the method for comprehensive utilization in the hydrometallurgy molybdenum-nickel paragenetic ore deposit in the hydrometallurgy.
Background technology
In 169 kinds in important mineral products that China finds, proven reserve has 159 kinds, and the mineral products that wherein have world's advantage have rare earth, tungsten, tin, molybdenum, nickel etc.In these mineral products, the ground such as Keshen in the Zhijin in southwest, Nayong, Zun Yi, Kaiyang, Fuquan, Wengan, Tongren, Jishou one band and Xinjiang store a kind of molybdenum ore, and the grade 2.5%～10% of molybdenum does not wait; And association has nickel, its grade 1.5%～5.0%; Carbon content 10%～12%; Sulphur content 25%～32%; Iron level 25%～30%.These mineral can not adopt the method for flotation that the grade of molybdenum is improved because contain carbon, and existing method for floating can only be enriched to low-grade molybdenum about 8%, and improves little to nickel and other associated elements.Though there are many enterprises these mineral to be carried out proposing the smelting production of molybdenum.The enterprise that has adopts and handles the molybdenum glance wet method smelting process, the roasting of ore deposit elder generation, alkali soaks again, prepare molybdic oxide behind the heavy molybdenum, the technology that the enterprise that has adopts is the system cake roasting of the broken back of breeze, with making molybdic oxide behind the heavy molybdenum of sulfuric acid leaching, the enterprise that also has is the system cake roasting of the broken back of this breeze, with the leaching of alkali pressurization oxygenation.Above-mentioned several method can only obtain to get the molybdenum product, and symbiotic other elements all enter waste residue, can't further handle and slatterns.Several wet processings of above-mentioned this, present total recovery is lower than 87%.
At present, concentrated molybdenum ore there is following several method both at home and abroad:
1. subliming method: the follow-up high-temperature to 1200 of continuing rising of calcining molybdenum ore concentrate desulfurization ℃, bubbling air or oxygen make molybdenum be oxidized to the molybdic oxide volatilization and collect with dust suction.The molybdic oxide purity height (99.95%) of this method preparation, but maximum shortcoming is to distil only to reach about 70%, and the molybdenum in the slag also needs to handle recovery with additive method.
2. ammonia-alkaline process: behind the calcining molybdenum ore concentrate, leach with ammoniacal liquor or caustic soda, leaching yield is about 90%.Solution NH
4HS purification and impurity removal (as assorted elements such as iron, copper).The total yield of molybdenum is greater than 85%.
3. electrooxidation-solvent extraction-charcoal absorption-crystallization process: this method is the method that Utah, USA mug(unit of measure) Na Chang adopts.This method has improved the total yield that selects the smelting process, and concentrate does not produce SO without roasting
2Gas, environmentally friendly.
4. oxygen is pressed and boiled-solvent extraction-crystallization process: this method is a kind of method of USSR (Union of Soviet Socialist Republics) research.At a certain temperature, pressurization digestion a few hours, rate of decomposition can reach 99.5%.
Above-mentioned four kinds of methods hydrometallurgy at concentrated molybdenum ore, and do not relate to the smelting process that solves the molybdenum-nickel paragenetic ore deposit.
1988, professor Wu Hongpei of department of chemistry of Guizhou University for Nationalities invented a kind of method to molybdenum-nickel paragenetic ore wet process metallurgy, " the depolymerization solvent extration is leached in vitriol oil slaking ".The rate of recovery of this method molybdenum reaches 95%～97%, and the rate of recovery of nickel is 75%.The advantage of this method is more outstanding, but its shortcoming also clearly.At first be to use the vitriol oil, produce very big acid mist, environmental hazard.Secondly the waste liquid amount after leaching is big, and is acid strong, the aftertreatment difficulty.And sulphur content height in this ore deposit, roasting produces a large amount of SO
2The harm environment.
Abroad, the U.S. handles this molybdenum-nickel paragenetic ore deposit patent US3922580, and this invention obtains molybdenum recovery 60%, nickel recovery 30%.
Molybdenum in China nickel mineral intergrowth aboundresources, reserves are big, if can fully utilize, make these resources bring into play due effect, can increase economic benefit and social effect.But the technology of comprehensive utilization is also immature, some sport technique segment awaits perfect, and some enterprises maximize for profit-push, not stinting to destroy environment is cost, continue to use backward Technology, the a large amount of obnoxious flavour contaminate environment of discharging in mass production molybdenum product is destroyed ecological.So finding out a kind of novel process of environmentally friendly, cleaning, to fully utilize the molybdenum-nickel paragenetic ore deposit be too impatient to wait.
Summary of the invention
The objective of the invention is to develop a kind of novel process of environmentally friendly, cleaning, can fully utilize the molybdenum-nickel paragenetic ore deposit,, the rate of recovery of molybdenum nickel is improved greatly, simultaneously, and do not produce obnoxious flavour by wet method smelting process is carried out in the molybdenum-nickel paragenetic ore deposit.
Purpose of the present invention realizes through following measure:
Technology of the present invention comprises seven steps of solution-treated behind breeze leaching, filtration, filtrate precipitation molybdic acid, molybdic acid dehydration, the extraction of filtrate residue molybdenum, anionite-exchange resin absorbed Ni, the absorbed Ni, and its step is as follows:
1. breeze leaches: after raw ore was pulverized ball milling, between the control solid-to-liquid ratio 1: 3,60 ℃～90 ℃ of temperature of reaction, reaction times 3h～4h, leach liquor were KClO
4(or NaClO
3, KMnO
4) and 30% nitric acid (or sulfuric acid of 98%).
2. filter: leach the back solid-liquid separation, separate the back slag muck and put.
3. filtrate is precipitated molybdic acid: pH value of filtrate is transferred to pH ≈ 2, separate out a large amount of H
2MoO
4Precipitation filters to isolate H
2MoO
4
4. molybdic acid dehydration: with the H of gained
2MoO
4Be heated to 400 ℃～500 ℃, get MoO after the dehydration
3
5. filtrate residue molybdenum extraction: will precipitate the molybdic acid rear filtrate and extract the molybdenum that has not precipitated, and strip with the ammoniacal liquor of 8mol/L with 5% tributyl phosphate (TBP).Anti-stripping agent makes ammonium paramolybdate after concentrating, and gets MoO behind 450 ℃ of heating deaminations
3
6. anionite-exchange resin absorbed Ni: tributyl phosphate (TBP) raffinate is with 201 * 7 resin absorption Ni
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets nickelous chloride after concentrating.
7. the solution-treated behind the absorbed Ni: behind the absorbed Ni solution through the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.
Among the present invention, the content 2.5%～10% of molybdenum in the raw ore, the content of nickel is 1.5%～5.0%, raw ore is pulverized ball milling to-200 orders 85% and is passed through.The extraction agent of step in 5. is that used sulfonated kerosene is commercially available with the tributyl phosphate of sulfonated kerosene dilution.Step 6. in 201 * 7 resins be the home-made strongly basic anion exchange resin, commercially available.
Advantage and effect that the present invention adopts above-mentioned flow process to have are as follows:
1. rate of recovery height: technology is simple, and flow process is short, and the total yield of molybdenum reaches about 98%, and the total yield of nickel reaches 94%～97%.
2. environmentally friendly: the wet processing of employing, raw ore be without roasting, thereby do not produce dust and obnoxious flavour, helps the protection to environment.
Description of drawings:
The process flow sheet of Fig. 1 the inventive method.
In Fig. 1, the explanation of numerical markings among the figure: 1. raw ore, 2. leach, 3. filter, 4. filtrate, 5. heavy molybdic acid 6. filters 7.H
2MoO
4, 8. dehydration, 9.MoO
3, 10. filtrate, the 11.TBP extraction, 12. back extractions, 13. concentrate 14. ammonium paramolybdates, 15. deaminations, 16.MoO
3, 17. raffinates, 18.201 * 7 absorbed Nis, 19. desorbs, 20. concentrate, 21. nickelous chlorides, 22. inhale back liquid, 23. neutralizations, 24. sedimentations, 25. discharging of waste liquid, 26. filter residues are stacked.
The present invention does detailed explanation in conjunction with the accompanying drawings and embodiments:
Embodiment
Embodiment 1
Take by weighing the raw ore 400kg that contains molybdenum 3.5%, nickel 3%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1100kg, KClO
410kg and 30% nitric acid 80kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 98.7%, and the leaching yield of Ni is 95.9%; And the total yield of Mo is 98.4%, and the total yield of Ni is 95.5%.
Embodiment 2
Take by weighing the raw ore 400kg that contains molybdenum 3%, nickel 4.9%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, NaClO
312kg and 30% nitric acid 100kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 99.3%, and the leaching yield of Ni is 97.5%; And the total yield of Mo is 99.0%, and the total yield of Ni is 96.8%.
Embodiment 3
Take by weighing the raw ore 400kg that contains molybdenum 4%, nickel 3.2%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1000kg, KMnO
420kg and 98% sulfuric acid 140kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 98.9%, and the leaching yield of Ni is 97.5%; And the total yield of Mo is 98.5%, and the total yield of Ni is 97.1%.
Embodiment 4
Take by weighing the raw ore 400kg that contains molybdenum 5%, nickel 3%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, water adds 1200kg, NaClO
314kg and 30% nitric acid 120kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 99.3%, and the leaching yield of Ni is 97.1%; And the total yield of Mo is 98.8%, and the total yield of Ni is 96.7%.
Embodiment 5
Take by weighing the raw ore 400kg that contains molybdenum 6%, nickel 2.5%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, KClO
414kg and 98% sulfuric acid 120kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 99.0%, and the leaching yield of Ni is 94.9%; And the total yield of Mo is 98.7%, and the total yield of Ni is 94.5%.
Embodiment 6
Take by weighing the raw ore 400kg that contains molybdenum 6.5%, nickel 2.5%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, NaClO
316kg and 30% nitric acid 150kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 98.7%, and the leaching yield of Ni is 97.4%; And the total yield of Mo is 98.3%, and the total yield of Ni is 97.0%.
Embodiment 7
Take by weighing the raw ore 400kg that contains molybdenum 6.5%, nickel 3%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, KClO
418kg and 98% sulfuric acid 150kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 99.1%, and the leaching yield of Ni is 97.1%; And the total yield of Mo is 98.7%, and the total yield of Ni is 96.8%.
Take by weighing the raw ore 400Kg that contains molybdenum 7%, nickel 2.5%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, NaClO
318kg and 30% nitric acid 150kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 98.9%, and the leaching yield of Ni is 94.9%; And the total yield of Mo is 98.5%, and the total yield of Ni is 94.5%.
Embodiment 9
Take by weighing the raw ore 400kg that contains molybdenum 8%, nickel 3.5%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, NaClO
320kg and 30% nitric acid 120kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 99.2%, and the leaching yield of Ni is 95.1%; And the total yield of Mo is 98.7%, and the total yield of Ni is 94.8%.
Take by weighing the raw ore 400kg that contains molybdenum 10%, nickel 3.2%, behind the pulverizing ball milling, drop into 2m
3In the enamel reaction still, add entry 1200kg, NaClO
325kg and 30% nitric acid 120kg are warming up to 85 ℃, start agitator, leach 3.5h.Leach after-filtration and make solid-liquid separation, solution is transferred pH ≈ 2, separates out the xanchromatic molybdic acid.Leach molybdic acid, behind 400 ℃～500 ℃ heating 1h, obtain grayish MoO
3Filtrate behind the filter molybdic acid extracts with 5% TBP, gets ammonium paramolybdate after the ammoniacal liquor back extraction of 8mol/L concentrates cooling, gets MoO behind 450 ℃ of heating deaminations
3TBP extraction back surplus solution is with the Ni in 201 * 7 resin absorption solution
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets green nickelous chloride after concentrating.Solution behind resin absorption nickel adds the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.The leaching yield of Mo of the present invention is 99.3%, and the leaching yield of Ni is 96.1%; And the total yield of Mo is 98.9%, and the total yield of Ni is 95.7%.
Claims (1)
1. the method in hydrometallurgy molybdenum-nickel paragenetic ore deposit, it is characterized in that seven steps of solution-treated after method comprises breeze leaching, filtration, filtrate precipitation molybdic acid, molybdic acid dehydration, the extraction of filtrate residue molybdenum, anionite-exchange resin absorbed Ni, absorbed Ni, its step is as follows:
1. breeze leaches: after raw ore was pulverized ball milling, between the control solid-to-liquid ratio 1: 3,60 ℃～90 ℃ of temperature of reaction, reaction times 3h～4h, leach liquor were KClO
4Or NaClO
3Or KMnO
4With 30% nitric acid or 98% sulfuric acid;
2. filter: leach the back solid-liquid separation, separate the back slag muck and put;
3. filtrate is precipitated molybdic acid: pH value of filtrate is transferred to pH ≈ 2, separate out a large amount of H
2MoO
4Precipitation filters to isolate H
2MoO
4
4. molybdic acid dehydration: with the H of gained
2MoO
4Be heated to 400 ℃～500 ℃, get MoO after the dehydration
3
5. filtrate residue molybdenum extraction: will precipitate the molybdic acid rear filtrate and extract the molybdenum that has not precipitated, and strip with the ammoniacal liquor of 8mol/L with 5% tributyl phosphate; Make after anti-stripping agent concentrates and stretch ammonium molybdate, behind 450 ℃ of heating deaminations, get MoO
3
6. anionite-exchange resin absorbed Ni: the tributyl phosphate raffinate is with 201 * 7 resin absorption Ni
2+, then first HCl wash-out Fe with 5mol/L
3+, use the HCl wash-out Ni of 8mol/L again
2+, this liquid gets nickelous chloride after concentrating;
7. the solution-treated behind the absorbed Ni: behind the absorbed Ni solution through the unslaked lime neutralizing treatment, supernatant liquid discharging behind the sedimentation calcium salt.
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| CN102676803A (en) * | 2012-06-05 | 2012-09-19 | 南京元泰环保科技有限公司 | Resource utilization method for catalytic oxidation leaching of molybdenum and nickel from molybdenum-nickel ore |
| CN108396142A (en) * | 2018-05-03 | 2018-08-14 | 中南大学 | A kind of method of acid decomposed by phosphoric acid molybdenum calcining |
| CN109055727A (en) * | 2018-11-05 | 2018-12-21 | 中南大学 | A kind of method of nickel molybdenum in synthetical recovery nickel-molybdenum ore |
| CN109837393A (en) * | 2019-01-31 | 2019-06-04 | 中南大学 | A kind of selective recovery is given up the method for valuable metal in hydrogenation catalyst |
| CN112831660A (en) * | 2020-12-30 | 2021-05-25 | 成都虹波钼业有限责任公司 | Process for comprehensively utilizing molybdenum ore leaching slag |
| CN114921650A (en) * | 2022-03-29 | 2022-08-19 | 江门市崖门新财富环保工业有限公司 | Method for extracting metal from waste hydrogenation catalyst |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102676803A (en) * | 2012-06-05 | 2012-09-19 | 南京元泰环保科技有限公司 | Resource utilization method for catalytic oxidation leaching of molybdenum and nickel from molybdenum-nickel ore |
| CN108396142A (en) * | 2018-05-03 | 2018-08-14 | 中南大学 | A kind of method of acid decomposed by phosphoric acid molybdenum calcining |
| CN108396142B (en) * | 2018-05-03 | 2020-10-23 | 中南大学 | Method for decomposing molybdenum calcine by phosphoric acid |
| CN109055727A (en) * | 2018-11-05 | 2018-12-21 | 中南大学 | A kind of method of nickel molybdenum in synthetical recovery nickel-molybdenum ore |
| CN109837393A (en) * | 2019-01-31 | 2019-06-04 | 中南大学 | A kind of selective recovery is given up the method for valuable metal in hydrogenation catalyst |
| CN112831660A (en) * | 2020-12-30 | 2021-05-25 | 成都虹波钼业有限责任公司 | Process for comprehensively utilizing molybdenum ore leaching slag |
| CN114921650A (en) * | 2022-03-29 | 2022-08-19 | 江门市崖门新财富环保工业有限公司 | Method for extracting metal from waste hydrogenation catalyst |
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Application publication date: 20110817 |