WO2005098061A1 - ニッケルまたはコバルトの浸出方法および回収方法 - Google Patents
ニッケルまたはコバルトの浸出方法および回収方法 Download PDFInfo
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- WO2005098061A1 WO2005098061A1 PCT/JP2005/004578 JP2005004578W WO2005098061A1 WO 2005098061 A1 WO2005098061 A1 WO 2005098061A1 JP 2005004578 W JP2005004578 W JP 2005004578W WO 2005098061 A1 WO2005098061 A1 WO 2005098061A1
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- leaching
- cobalt
- nickel
- ore
- sulfuric acid
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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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—Sulfurated acids or salts thereof
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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
- 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
Definitions
- the present invention relates to a method for leaching nickel or cobalt and a method for recovering nickel or cobalt.
- Non-Patent Document 1 Non-Patent Document 2
- Non-Patent Document 3 a pressure leaching method for obtaining a sulfuric acid solution containing nickel and cobalt under high temperature and high pressure
- Non-patent document l Proc. Australas. Inst. Metall. No. 265, March. 1978
- Non-Patent Document 2 The metallurgical Society, 1988 p447
- Non-Patent Document 3 Journal of Metals.March, 1960, P206
- Non-Patent Document 4 ISU International Vol43 (2003) No 2 pl81—pl86 Disclosure of Invention
- Non-Patent Document 2 while oxidizing ore containing nickel, conoreto, magnesium and iron is leached with sulfuric acid under atmospheric pressure as described in Non-Patent Document 2, nickel, In addition to cobalt, iron is also leached at the same time. If nickel and cobalt are to be leached at 80% by weight or more, iron is also leached at 15% by weight or more. In general, oxidized ore containing nickel and cobalt contains 10 to 40 times as much iron as nickel, so the method described in the literature requires a large amount of sulfuric acid for leaching, and the strength is also leached. Since the concentration of iron in the liquor becomes high, the processing cost for removing iron also increases, and there remains a problem in terms of cost.
- Non-Patent Document 4 (recent research report on atmospheric leaching), under a mixed gas atmosphere of CO / CO (30Z70vol%) and a temperature of 700 ° C, Okke
- Non-Patent Document 3 when oxidized ore is leached under pressure with sulfuric acid under high temperature and high pressure, leaching of iron is suppressed, and the leaching rate of nickel and cobalt is high. Is obtained. Therefore, the amount of sulfuric acid used is small, and the processing cost for removing iron is also low.Autoclave is necessary for sulfuric acid leaching operation under high temperature and high pressure. Also, expensive materials such as titanium are required. Also, energy consumption is increased compared to leaching under atmospheric pressure. Furthermore, since scale adheres to and grows on the inner wall of the autoclave, it is often necessary to interrupt the operation to remove the scale, resulting in a decrease in the operation rate.
- the present invention has been made in view of the above circumstances, and an object of the present invention is to provide a method for leaching or recovering nickel or cobalt from an oxide ore containing nickel or cobalt and iron. And to improve the leaching rate and recovery rate of cobalt.
- a method for leaching nickel or cobalt from an oxide ore containing nickel or cobalt and iron wherein a reducing agent containing iron and sulfuric acid are added to the oxide ore to obtain nickel.
- a leaching method characterized by including a leaching step of obtaining a sulfuric acid leaching solution containing cobalt and a leaching residue.
- a cobalt component in an oxide ore is reduced using a reducing agent containing iron.
- a reducing agent containing iron By using such a reducing agent, the leaching rate of cobalt can be improved while stabilizing the process.
- the oxide ore is made of a small-grain oxide ore and a large-grain oxide ore.
- a leaching step of adding a reducing agent and sulfuric acid to small-sized oxide ore to obtain a sulfuric acid leaching solution containing nickel or cobalt, and a leaching residue, and a sulfuric acid containing leaching residue There is provided a leaching method characterized by comprising a reaction step of reacting a leaching solution with an oxide ore having a large particle diameter to obtain a reaction solution containing nickel or cobalt and a reaction residue containing iron. .
- Small-sized oxide ores have difficulty in leaching cobalt as compared with large-sized oxide ores. Therefore, in the above configuration, first, the small-grain oxide ore and the large-grain oxide ore are classified, and the obtained small-grain oxide ore is subjected to leaching treatment. A reaction liquid containing nickel or cobalt is obtained by reacting with the oxidized ore having a particle size of. In this way, small-diameter oxidized ore, from which conoreto is not easily leached, is selected and introduced into the system at a stage where the consumption of the reducing agent and sulfuric acid is low, so that the leaching rate of cobalt is significantly reduced. Can be improved.
- large-grain oxide ores generally contain a large amount of magnesium as compared with small-grain oxide ores, and thus the large-grain oxidized ore is introduced in the reaction step as described above. Thus, the reaction in the reaction step can be effectively promoted.
- both the leaching step and the reaction step can be performed at a temperature of 90 ° C. or higher. By doing so, the leaching rate of the conoreto can be further improved.
- both the leaching step and the reaction step can be performed under normal pressure. By doing so, it is possible to suppress an increase in equipment costs.
- a method for recovering nickel or cobalt from an oxidized ore containing nickel or cobalt and iron, wherein sulfuric acid, a sodium salt and a reducing agent are refined A leaching step of obtaining a sulfuric acid leaching solution containing leaching residue and leaching residue, a sulfuric acid leaching solution containing the leaching residue and magnesium being adjusted to adjust the pH, and a reaction solution containing nickel or cobalt, and iron And a reaction step for obtaining a reaction solution containing the reaction residue, and neutralizing the reaction solution containing the reaction residue using a neutralizing agent, and neutralizing a neutralization solution containing nickel or cobalt and a neutralization residue containing iron. And obtaining a neutralization step.
- the leaching step sulfuric acid, a sodium salt, and iron are combined to form natrojarosite, and, at the same time, sulfuric acid and a reducing agent are used to reduce the cobalt component in the oxide ore.
- the leaching rate of nickel and cobalt can be improved.
- the pH can be adjusted using magnesium. Since iron can be precipitated before the neutralization step, an increase in the cost of treating iron in the neutralization step can be suppressed. Therefore, the recovery rate of nickel and cobalt can be improved more efficiently.
- a step of classifying the oxide ore into a small-diameter oxidized ore and a large-diameter oxidized ore containing magnesium is included.
- the pH may be adjusted by reacting a sulfuric acid leaching solution containing a leaching residue with magnesium contained in a large particle size acid ore in the reaction step. This reduces nickel and cobalt recovery costs while reducing nickel
- the leaching rate of cobalt can be further improved.
- a step of solid-liquid separation of the neutralized solution and the neutralized residue using a coagulant and using a thickener to separate the neutralized solution and the neutralized residue may further include.
- both the leaching step and the reaction step may be performed at a temperature of 90 ° C. or higher. By doing so, the leaching rate of cobalt can be further improved. Further, both the leaching step and the reaction step may be performed under normal pressure. By doing so, it is possible to suppress an increase in equipment costs.
- normal pressure includes the vicinity of normal pressure.
- the method for leaching or recovering nickel and cobalt using sulfuric acid and a reducing agent to reduce the amount of oxidized ore By reducing the conorate component, the leaching rate or recovery rate of nickel and cobalt can be improved.
- FIG. 1 is a flowchart for explaining steps in an embodiment of the present invention.
- FIG. 2 is a flowchart for explaining steps in an embodiment of the present invention.
- the amount used and the amount added are the amount used and the amount added based on the weight of each substance.
- the same components are denoted by the same reference numerals, and description thereof will not be repeated.
- an oxide ore whose components are described in Table 1 can be used.
- the two types of oxide ores shown in Table 1 can be from mines with different origins.
- Figure 1 shows a process diagram for recovering nickel and cobalt from oxide ores containing nickel, cobalt and iron.
- step a the oxide ore 202 is classified into oversize and undersize, the undersize is converted into slurry ore 204 using service water 207, and the oversize is pulverized by grinding. 203.
- step b (leaching step) trivalent cobalt oxide is reduced by adding sulfuric acid 205 and a reducing agent 220 to the slurry ore 204, and leached with sulfuric acid 205 to remove nickel, cobalt And a leaching residue 209 containing
- the leach residue 209 is formed by the reaction between the iron leached from the slurry ore 204, the sulfuric acid 205, and the sodium salt 206.
- the Natrojaro site was included.
- step c (reaction step) free sulfuric acid in the sulfuric acid leachate 208 containing the leach residue 209 is reacted with magnesium contained in the pulverized product 203 pulverized in the classification step to obtain free palladium.
- the pH is adjusted by consuming sulfuric acid to obtain a reaction solution 210 and a reaction residue 211.
- natrojarosite is precipitated in the reaction residue 211, whereby the iron concentration in the reaction liquid 210 can be reduced.
- step d neutralization step
- the pH is adjusted by adding a neutralizing agent 212 to the reaction solution 210 containing the reaction residue 211, and a neutralization solution 213 and a neutralization residue 214 are obtained.
- natrojarosite is precipitated, and the iron concentration in the reaction solution 210 is reduced, so that the amount of the additional force of the neutralizing agent 212 can be reduced.
- step e solid-liquid separation step
- the coagulant 215 is added to the neutralization liquid 213 containing the neutralization residue 214, and the mixture is subjected to solid-liquid separation using a thickener. And the neutralized residue 214 are separated.
- the neutralized solution 213 is sent to a nickel-cobalt recovery step, and nickel and cobalt are recovered.
- Step a Classification step
- the undersize is made into a slurry ore 204 using water 207, and the oversize is made into a crushed product 203 using a device such as a ball mill.
- the size of classification using a vibrating sieve or the like is not particularly limited, but a sieve having a size of 0.5 mm or more and 2 mm or less, for example, can be used from the viewpoint of improving process stability.
- Step b leaching step
- the slurry ore 204 obtained in the step a is leached by, for example, kneading the sulfuric acid 205 and the reducing agent 220 under normal pressure, for example, at a temperature of 90 ° C or more and 100 ° C or less.
- a sulfuric acid leaching solution 208 containing nickel, cobalt, magnesium and iron and a leaching residue 209 are obtained.
- the leaching speed of nickel and cobalt in the slurry ore 204 can be improved. Thereby, the leaching time of nickel and cobalt contained in the slurry ore can be shortened. At the same time, the leaching rate of nickel and conoreto can be increased. Also, by leaching nickel and cobalt contained in the slurry ore at a temperature of 100 ° C or lower, nickel and cobalt can be leached at a temperature of the boiling point of water or lower. Therefore, it is not necessary to pressurize the leaching vessel of the apparatus used for leaching nickel and cobalt. Therefore, an increase in equipment cost can be suppressed.
- the temperature at which the leaching temperature is 90 ° C. or higher may be selected as appropriate, for example, in the range of 70 ° C. or higher. Further, nickel and cobalt in the slurry ore 204 may be leached at a temperature exceeding 100 ° C. Further, nickel and cobalt in the slurry ore 204 may be leached under pressure conditions other than normal pressure.
- the amount of sulfuric acid to be added can be 0.5 times or more and 0.8 times or less the amount of the oxide ore 202 used. By adding 0.5 times or more of sulfuric acid, leaching of nickel and cobalt can be sufficiently performed. When the amount of sulfuric acid added is around 0.8 times, the leaching rates of nickel and cobalt reach an equilibrium state. Therefore, the amount of sulfuric acid to be added should be 0.8 times or less. Thus, the amount of excessive sulfuric acid (free sulfuric acid) can be suppressed. Therefore, it is possible to suppress the increase in the cost of recovering nickel and cobalt while maintaining the leaching rate of nickel and cobalt from the oxidized ore.
- the reducing agent 220 for example, iron powder, sodium sulfite, or a mixture thereof is used. Among them, iron such as iron powder can be used. When iron powder is used as the reducing agent 220, a high effect as the reducing agent 220 can be obtained with a smaller amount of use. In addition, since iron powder is inexpensive, it is possible to stably improve the leaching rate of nickel and cobalt while suppressing an increase in production cost.
- the particle diameter of the iron powder a powder having a diameter of about lmm can be used, and a powder whose surface is not oxidized can be used. In addition to iron powder, use iron scraps finely crushed by a grinder.
- the amount of the reducing agent 220 to be added is appropriately selected according to its type.
- iron powder When iron powder is used, it can be added in a range of 0.1% by weight to 1% by weight, particularly 0.2% by weight to 0.5% by weight based on the amount of the oxide ore 202 used.
- sodium sulfite When sodium sulfite is used, it can be in the range of 1% by weight to 10% by weight, particularly 5% by weight to 8% by weight, based on the amount of the oxidized ore 202 used.
- the effect of the iron powder as the reducing agent 220 can be sufficiently exerted, and the leaching rate of nickel and cobalt, particularly the leaching rate of conoreto can be further improved efficiently. it can. Therefore, it is possible to further improve the leaching rate of nickel and cobalt while reducing the cost.
- the effect of the reducing agent 220 can be sufficiently exhibited, and the leaching rate of nickel and cobalt, particularly the leaching rate of cobalt, can be further efficiently improved. be able to. Therefore, the recovery rate of nickel and cobalt can be further improved while reducing the cost of removing iron.
- the cobalt in the oxide ore 202 is composed of a divalent oxide (CoO) and a trivalent oxide (Co
- Such a bonding state between cobalt and oxygen is that Co O is stronger and more stable than CoO, It is not easy for the sulfuric acid 205 to break the bond between cobalt and oxygen in the trivalent conoret acid sulfide contained in the slurry ore 204. Therefore, the reducing agent 220 is added to sulfuric acid 205 to reduce the bonding force between cobalt and oxygen in the trivalent cobalt oxide, and the valence of cobalt is reduced from trivalent to divalent. It is presumed that the leaching of konoleto with sulfuric acid 205 became easier.
- iron powder When iron powder is used as reducing agent 220, the same effect as reducing agent 220 can be obtained with a smaller amount of reducing agent 220 used. Iron powder is inexpensive. Therefore, when iron powder is used as the reducing agent, the recovery rate of nickel and cobalt can be improved while suppressing an increase in production cost.
- the following effects can be obtained by using an undersized ore classified in the classification step.
- nickel and cobalt in the oxide ore are less likely to be leached from the undersized ore than the pulverized oversized ore 203.
- the oversized ore crushed product 203 has a higher magnesium content than the undersized ore, it may consume free sulfuric acid used for leaching. Therefore, in the leaching process, undersize ore is used, an excessive amount of sulfuric acid is used, and trivalent cobalt oxide is reduced to divalent cobalt oxide by the reducing agent 220. By simultaneously leaching nickel and cobalt in the oxide ore, the leaching rate of nickel and cobalt can be further improved.
- a sodium salt 206 such as sodium sulfate or sodium salt is removed.
- the amount of sodium added by the sodium salt 206 can be about 0.01 to 1.05 times the amount of the oxide ore 202 used.
- sodium salt 206 is contained in seawater in an amount of about lOgZl. Therefore, nickel and cobalt can be leached from the oxide ore while suppressing an increase in the cost of recovering nickel and cobalt.
- the iron leached from the oxide ore reacts with sodium sulfate in the sulfuric acid leaching solution 208 to form a sulfuric acid leaching solution. 8 can reduce the concentration of iron.
- the addition of sodium salt 206 generates natrojarosite, and the addition of reducing agent 220 reduces trivalent conoreto oxide to divalent cobalt oxidite which is easily leached.
- the leaching rate of nickel and cobalt by sulfuric acid 205 can be improved at the same time.
- nickel and cobalt can be leached more efficiently while suppressing an increase in the cost of recovering nickel and cobalt from oxide ores.
- the leaching time can be 1 hour or more and 10 hours or less, and 3 hours or more and 6 hours or less. Can be below.
- the equipment required for the leaching step is, for example, a commonly used vessel equipped with a stirrer, and the like, and the material used is, for example, stainless steel or steel lining with rubber lining.
- the material used is, for example, stainless steel or steel lining with rubber lining.
- nickel and cobalt can be leached from the oxidized ore 202 used in pressure leaching at high temperature and high pressure without using expensive equipment such as a titanium-lined autoclave. Therefore, nickel and cobalt can be leached while suppressing an increase in cost required for recovering nickel and cobalt.
- the sulfuric acid leaching solution 208 and the leaching residue 209 obtained in the step b, and the pulverized oversized iron ore 203 obtained in the step a for example, under atmospheric pressure, for example, at 90 ° C.
- the reaction is carried out at a temperature equal to or lower than C based on the following formula (4)-(7). Based on the reaction formula described below, a reaction solution 210 containing nickel, cobalt, magnesium and a small amount of iron and a reaction residue 211 are obtained.
- a reducing agent 220 may be added.
- the reducing agent 220 may not be added in the step b, and the reducing step may be performed in both the step b and the present step.
- the reducing agent 220 for example, iron powder, sodium sulfite, or a mixture thereof is used.
- iron powder when iron powder is used, it can be added in a range of 0.1% by weight or more and 1% by weight or less, particularly 0.2% by weight or more and 0.5% by weight or less based on the amount of the oxide ore 202 used.
- particle diameter of the iron powder a powder having a diameter of about lmm can be used, and a powder whose surface is not oxidized can be used.
- sodium sulfite it can be in the range of 1% by weight to 10% by weight, particularly 5% by weight to 8% by weight, based on the amount of oxide ore 202 used.
- iron other than iron powder such as iron shavings finely ground by a grinder, methanol, ethanol
- Other reducing agents may be used, such as alcohols such as, and reducing gases such as sulfurous acid gas.
- the method of adding the pulverized product 203 may be solid as it is, or may be made into slurry using water.
- the water used in this process can be either river water, groundwater or seawater. May be.
- sodium water 206 such as sodium sulfate and sodium salt may be added to these waters for use.
- the reaction temperature is 90 ° C. or higher
- the leaching rate of nickel and cobalt contained in the pulverized product 203 can be improved.
- the efficiency of precipitation and removal of the iron leached in step b as a natroja mouth site can be improved.
- a reaction based on a chemical formula described below can be performed at a temperature of the boiling point of water or lower. For this reason, it is not necessary to pressurize the reaction vessel of the apparatus used for the above reaction. Therefore, an increase in equipment cost can be suppressed.
- a reaction based on a chemical formula described below may be performed under the condition that the leaching temperature is lower than 90 degrees or higher than 100 degrees Celsius. Further, a reaction based on a chemical formula described below may be performed under pressure conditions other than the atmospheric pressure.
- the iron concentration of the sulfuric acid leaching solution 208 in the step b is 30 gZl—90 g / 1, and contains 30 g / l or more of free sulfuric acid.
- the iron concentration is reduced to 1Z10 or less and free sulfuric acid is reduced to 1Z3 or less as compared with the sulfuric acid leachate 208 before the reaction.
- the free sulfuric acid in the sulfuric acid leachate 208 reacts with the magnesium contained in the pulverized product 203, and the amount of free sulfuric acid decreases, thereby increasing the pH in the liquid. . Therefore, as the pH in the solution increases, natrojarosite and gamesite are formed according to the equations (5) to (7), and iron precipitates.
- the efficiency is improved more efficiently.
- the above reaction can be caused.
- the component ratio of magnesium Z iron is 0.125 or more
- the amount of iron contained in the oxidized ore 202 is relatively small.
- the force also leaches relatively little iron. Therefore, the iron concentration in the reaction solution can be reduced.
- the amount of magnesium contained in the oxide ore 202 is relatively large, the amount of magnesium which reacts with the free sulfuric acid brought into the reaction process from the sulfuric acid leachate 208 is relatively large. Therefore, the free sulfuric acid in the sulfuric acid leaching solution 208 can be sufficiently consumed using magnesium by the reaction of the formula (4).
- the upper limit of the component ratio of magnesium-Z iron is, for example, 0.75 or more.
- the oxide ore 202 used in this embodiment is a limonite ore containing 20% by weight or more and 50% by weight or less of iron and 2.5% by weight or more and 15% by weight or less of magnesium.
- the composition ratio of Z iron does not exceed 0.75.
- the reason for using the oversized crushed product 203 in the step c is that the oversized crushed product 203 has a higher magnesium content than the undersized crushed product 203, and therefore the reaction of the formula (4)-(7) But it is also the power to go more effectively.
- the reaction time can be 3 hours or more and 10 hours or less, or 4 hours or more and 6 hours or less, and the reaction time of the formula (4) 1 ( The reaction of 7) can be terminated.
- the sulfuric acid is reacted with magnesium to adjust the pH while leaching nickel and cobalt in the pulverized product 203. Can be. Therefore, the recovery rate of nickel and cobalt can be further improved.
- the equipment required for the reaction is, for example, a commonly used vessel with a stirrer or the like, and the material thereof is, for example, a stainless steel or steel material rubber-junged. It is enough. Therefore, the reaction of this step can be performed without using expensive equipment used in a reaction under high temperature and high pressure, for example, an autoclave of titanium lining. Therefore, it is possible to suppress an increase in cost required for recovering nickel and cobalt.
- the nickel slag having a relatively high nickel content among the nickel slags used in the neutralization step may be used simultaneously with the oversized pulverized product.
- the final pH during the reaction can be used within a range of less than 3. If the pH is less than 3, the presence of free sulfuric acid in the liquid can suppress a decrease in the leaching efficiency of nickel from the oxide ore.
- the content of nickel is 1% by weight or less, the content of magnesium is 15% by weight or more, and a relatively nickel content which is not usually used for recovering nickel and cobalt.
- Use oxide ore In addition, such an oxide ore has a feature that the iron content is relatively low, for example, which is often present in a deep layer of a nickel or cobalt mine. Therefore, by using the above-mentioned oxidized ore in the step c, it is possible to perform the pH adjustment with magnesium while leaching nickel and conoreto into the sulfuric acid solution, and to suppress an increase in the amount of leached iron. As a result, it is possible to reduce the cost of recovering nickel and cobalt while improving the recovery rate of nickel and cobalt.
- other than ore oxide ore containing magnesium may be used.
- step c When pH is adjusted in step c, an oxide ore containing oversized magnesium classified in step a and an oxide ore containing magnesium other than oxidized ore are used.
- step c when the pH is adjusted in step c, the nickel quality is low and the magnesium quality is low.
- a material containing magnesium other than oxidized ore is used.
- the oxide ore containing oversized magnesium classified in step a the nickel ore having a low nickel grade and a high magnesium grade, and It is also possible to use those containing magnesium other than ore.
- Step d neutralization step
- the pH can be adjusted to 2 or more and 6 or less, and the neutralization reaction is performed at a pH of 3 or more and 5 or less. be able to.
- a neutralization solution 213 containing nickel, cobalt, and magnesium having an iron concentration of lg / 1 or less and a neutralization residue 214 are obtained.
- the pH is 2 or more, the precipitation of iron can be sufficiently performed, and when the pH is 6 or less, most of the iron is precipitated and removed while suppressing the coprecipitation of nickel and cobalt. You. Therefore, the recovery of nickel and cobalt can be improved.
- the pressure in this step is not particularly limited.
- a neutralization reaction may be performed using the reaction solution 210, the reaction residue 211, and the neutralizing agent 212 under atmospheric pressure.
- the neutralization reaction may be performed under pressure conditions other than atmospheric pressure.
- alkaline earth metals such as sodium hydroxide, which is a hydroxide of an alkali metal, and sodium carbonate, which is a carbonate of an alkali metal
- Alkaline earth metal charcoal such as alkaline earth metal oxidizers such as calcium hydroxide and magnesium hydroxide, which are metal hydroxides. Oxides such as calcium carbonate and magnesium carbonate can be used.
- nickel slag having a composition shown in Table 1 can be used.
- the above-mentioned neutralizing agents may be used alone or in a combination of two or more.
- the Hue nickel slag refers to magnesium generated when producing Hue nickel by a dry manufacturing method using ore containing magnesium containing 2% by weight or more of nickel. Refers to slag including.
- the amount of nickel slag generated at the Hue mouth in the dry manufacturing method is about 30-35 times the amount of nickel 1, and only a part of it is used effectively.
- nickel slag having a mouth containing magnesium as neutralizing agent 212
- magnesium contained in the nickel slag having a mouth can be effectively used as a neutralizing agent, and reaction solution 210 and reaction residue can be effectively used.
- 211 can be neutralized. Therefore, while effectively utilizing resources, it is possible to recover nickel and cobalt while suppressing an increase in the cost of recovering nickel and cobalt.
- the neutralizing agent 212 if it is possible to neutralize the reaction solution 210 and the reaction residue 211, for example, calcium hydroxide, magnesium hydroxide, calcium oxide, magnesium oxide other than Hue nickel slag can be used. , Calcium carbonate, magnesium carbonate and the like may be used.
- the neutralized solution 213 and the neutralized residue 214 obtained in the step d are separated by adding the flocculant 215.
- the flocculant 215 for example, a polymer flocculant is used.
- a generally used thickener method is adopted, and a countercurrent washing method using six or more thickeners can be used.
- nickel and cobalt in the neutralized solution can be produced at a high yield of 99% by weight or more and a neutralized solution 213 containing nickel, conoreto, and magnesium having a low iron content of less than lgZl and a low iron content. It is easily and efficiently separated into the neutralization residue 214 and solid-liquid separation.
- the flocculant 215 may be a flocculant that can be separated into the neutralizing solution 213 and the neutralization residue 214 other than the polymer flocculant.
- the solid-liquid separation into the neutralized solution 213 and the neutralized residue 214 may be performed by using another solid-liquid separating device other than the countercurrent washing method using a thickener having six or more stages.
- the neutralized solution 213 may be, for example, sodium bisulfide described in JP-A-6-81050, A method of adding sulfuric acid soda, sulfuric acid ammon, sulfuric acid hydrogen and the like to precipitate and recover as a mixed sulfide of nickel and cobalt, and a method described in Japanese Patent Application Laid-Open No. 12-234130.
- a method of kneading a sword, a sword and a carbonated sardine to obtain a mixed stilt of nickel and cobalt, and collecting and recovering the mixture as a mixed stilt.
- FIG. 2 is a flow diagram illustrating the steps according to the present embodiment.
- FIG. 2 illustrates the steps up to the step b (leaching step) .
- the sulfuric acid leaching solution 208 and the leaching residue 209 are processed by performing the steps c and subsequent steps described in the first embodiment, and the nickel and cobalt are removed. Collect. Even in this case, effects similar to those described in the above embodiment can be obtained.
- the oxide ore containing nickel, cobalt and iron was described in the form of recovering nickel and cobalt. Nickel may be recovered, or cobalt may be recovered from an oxide ore containing cobalt and iron.
- each component of the oxide ore in Tables 2 and 3 below is expressed in terms of% by weight based on the weight of the oxide ore.
- Tables 2 and 3 show the conditions and results of the examples and comparative examples.
- Example 1 In Example 5 and Comparative Example 1, the oxide ore Nol (Ni: 1.65% Co:
- Example 6 In Example 10 and Comparative Example 2, the oxidizing ore Nol and the mine power of the locality S different from the oxidizing ore Nol (Ni: 1.71% Co: 0.2357%, Fe: 22.7% Mg: ll.1%
- Oxidized ore Nol is sieved with a 2mm sieve and 64% by weight of 2mm oxidized ore and 36% by weight
- + 2mm oxide ore was ground to a total volume of 2mm.
- 2mm Sodai ore is made into 28% by weight slurry with seawater, and 98% by weight sulfuric acid is classified. 0.73 times the total amount of the previous oxide ore was leached by stirring at 95 ° C and atmospheric pressure for 6 hours.
- the same oxidized ore as in Comparative Example 1 was used under the same conditions except that iron powder was added in an amount of 0.003 times the total amount of oxidized ore in the leaching step.
- the leaching rate of nickel at this time was 89.0% by weight, which was almost the same as that of Comparative Example 1.
- the leaching rate of force konoleto increased to 80.2% by weight.
- Comparative Example 2 The same oxide ore as in Comparative Example 1 was used under the same conditions except that iron powder was added in an amount of 0.005 times the total amount of oxide ore in the reaction step. As described above, the addition of iron powder or sodium sulfite in oxide ore No. 1 improved the leaching rate of cobalt by 15% to 20% by weight. [0112] (Comparative Example 2)
- Oxide ore No2 was classified with a 2mm sieve to obtain 61% by weight of -2mm oxide ore and 39% by weight of + 2mm oxide ore.
- + 2mm oxide ore was ground to a total volume of 2mm.
- 2mm Sodai ore is made into a 28% by weight slurry with seawater, and 98% by weight sulfuric acid is 0.73 times the total amount of oxidized ore before classification. It was leached by stirring at atmospheric pressure for 6 hours.
- the mixture of sulfuric acid leach liquor and leach residue obtained in this way was crushed with a slurry of +2 mm oxidized ore in seawater as a 40% by weight slurry, and heated at 95 ° C and atmospheric pressure. The mixture was stirred and reacted for 6 hours.
- the same oxidized ore as in Comparative Example 2 was used under the same conditions except that iron powder was added in the leaching step in an amount of 0.003 times the total amount of oxidized ore.
- the leaching rate of nickel was 92.2% by weight
- the leaching rate of cobalt was 87.0% by weight
- the leaching rate of nickel was about 5% by weight
- that of cobalt was about 74% by weight. was gotten.
- the oxidizing ore Nol is different from the oxidizing ore No2 in that the leaching rate of nickel is improved and the leaching rate of cobalt is improved by removing iron powder or sodium sulphite in the oxidizing ore No2 of different origin. As a result, a significant increase in the leaching rate of 64% by weight to 82% by weight was obtained.
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- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP05720833A EP1731623A4 (en) | 2004-03-31 | 2005-03-15 | EXTRACTION METHOD AND METHOD FOR OBTAINING NICKEL OR COBALT |
JP2006516883A JP4456110B2 (ja) | 2004-03-31 | 2005-03-15 | ニッケルまたはコバルトの浸出方法 |
BRPI0505977 BRPI0505977B1 (pt) | 2004-03-31 | 2005-03-15 | processo para recuperação de níquel ou cobalto a partir de um minério de óxido contendo níquel ou cobalto e ferro |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2004108203 | 2004-03-31 | ||
JP2004-108203 | 2004-03-31 |
Publications (2)
Publication Number | Publication Date |
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WO2005098061A1 true WO2005098061A1 (ja) | 2005-10-20 |
WO2005098061A8 WO2005098061A8 (ja) | 2006-09-21 |
Family
ID=35125096
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2005/004578 WO2005098061A1 (ja) | 2004-03-31 | 2005-03-15 | ニッケルまたはコバルトの浸出方法および回収方法 |
Country Status (4)
Country | Link |
---|---|
EP (2) | EP2108708B1 (ja) |
JP (2) | JP4456110B2 (ja) |
BR (1) | BRPI0505977B1 (ja) |
WO (1) | WO2005098061A1 (ja) |
Cited By (3)
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JP2009515044A (ja) * | 2005-11-10 | 2009-04-09 | コンパニア バレ ド リオ ドセ | 複合浸出プロセス |
JP2012036420A (ja) * | 2010-08-03 | 2012-02-23 | Sumitomo Metal Mining Co Ltd | ニッケル及びコバルトの浸出方法、及びリチウムイオン電池からの有価金属の回収方法 |
WO2024024930A1 (ja) * | 2022-07-28 | 2024-02-01 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
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FR2905383B1 (fr) | 2006-09-06 | 2008-11-07 | Eramet Sa | Procede de traitement hydrometallurgique d'un minerai de nickel et de cobalt lateritique,et procede de preparation de concentres intermediaires ou de produits commerciaux de nickel et/ou de cobalt l'utilisant. |
US7988938B2 (en) | 2007-12-24 | 2011-08-02 | Bhp Billiton Ssm Development Pty Ltd. | Selectively leaching cobalt from lateritic ores |
CN101978080A (zh) | 2008-03-19 | 2011-02-16 | Bhp比利通Ssm开发有限公司 | 使用超咸浸提液常压浸提红土矿石的方法 |
WO2009114903A1 (en) * | 2008-03-20 | 2009-09-24 | Bhp Billiton Ssm Development Pty Ltd | Process for the recovery of nickel and/or cobalt from high ferrous content laterite ores |
EP2553129B1 (en) * | 2010-04-01 | 2019-06-19 | Incor Technologies Limited | Low acid leaching of nickel and cobalt from lean iron-containing nickel ores |
US8361191B2 (en) | 2010-04-01 | 2013-01-29 | Search Minerals, Inc. | Low acid leaching of nickel and cobalt from lean iron-containing nickel ores |
CN102658234B (zh) * | 2012-04-10 | 2015-03-25 | 西北有色地质研究院 | 消泡剂在石煤型钒矿选矿抛尾-湿法冶金的应用方法 |
JP5904100B2 (ja) * | 2012-11-20 | 2016-04-13 | 住友金属鉱山株式会社 | 中和スラリーの沈降分離方法、並びにニッケル酸化鉱石の湿式製錬方法 |
JP5880488B2 (ja) * | 2013-06-17 | 2016-03-09 | 住友金属鉱山株式会社 | ヘマタイトの製造方法、並びにそのヘマタイト |
CN104805308A (zh) * | 2014-12-31 | 2015-07-29 | 金川集团股份有限公司 | 一种从低品位红土镍矿中回收镍、钴、铁、硅和镁的新方法 |
CN104789797A (zh) * | 2014-12-31 | 2015-07-22 | 金川集团股份有限公司 | 一种从低品位红土镍矿中回收镍、钴、铁、硅和镁的新方法 |
CN104789799A (zh) * | 2014-12-31 | 2015-07-22 | 金川集团股份有限公司 | 常压酸浸和中等压力浸出相结合处理红土镍矿的方法 |
CN104805309A (zh) * | 2014-12-31 | 2015-07-29 | 金川集团股份有限公司 | 一种从红土镍矿中回收镍、钴和铁的方法 |
CN104805306A (zh) * | 2014-12-31 | 2015-07-29 | 金川集团股份有限公司 | 一种从低品位红土镍矿中回收镍、钴和铁的新方法 |
CN104630501A (zh) * | 2014-12-31 | 2015-05-20 | 金川集团股份有限公司 | 一种通过联合浸出工艺从低品位红土镍矿中回收镍、钴、铁和硅的方法 |
CN104630504A (zh) * | 2014-12-31 | 2015-05-20 | 金川集团股份有限公司 | 一种从褐铁矿中回收镍的方法 |
CN104805307A (zh) * | 2014-12-31 | 2015-07-29 | 金川集团股份有限公司 | 一种从低品位红土镍矿中回收镍、钴和铁的新方法 |
CN104762493A (zh) * | 2014-12-31 | 2015-07-08 | 金川集团股份有限公司 | 常压酸浸和中等压力浸出相结合处理红土镍矿的方法 |
CN104789798A (zh) * | 2014-12-31 | 2015-07-22 | 金川集团股份有限公司 | 常压酸浸和中等压力浸出相结合处理红土镍矿的方法 |
CN104651634A (zh) * | 2014-12-31 | 2015-05-27 | 金川集团股份有限公司 | 一种从红土镍矿中回收镍、钴和铁的方法 |
CN104831087A (zh) * | 2014-12-31 | 2015-08-12 | 金川集团股份有限公司 | 一种通过联合浸出工艺从低品位红土镍矿中回收镍、钴、铁和硅的方法 |
CN104593584A (zh) * | 2015-02-03 | 2015-05-06 | 赣州逸豪优美科实业有限公司 | 一种机械活化强化钴白合金浸钴工艺 |
CN104726717B (zh) * | 2015-04-01 | 2017-04-19 | 云南驰宏锌锗股份有限公司 | 一种逆锑净化钴渣回收钴的方法 |
CN106244811B (zh) * | 2016-08-24 | 2018-04-06 | 盛隆资源再生(无锡)有限公司 | 一种铜铁含量低、锡镍含量高的电镀污泥的回收利用方法 |
CN109280768A (zh) * | 2018-12-04 | 2019-01-29 | 浙江中金格派锂电产业股份有限公司 | 钴精矿及钴中间品混合浸出-除铁同步进行的生产方法 |
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JPS50154111A (ja) * | 1974-05-10 | 1975-12-11 | ||
JP2003514109A (ja) * | 1999-11-03 | 2003-04-15 | ビーエイチピー ミネラルズ インターナショナル インコーポレイテッド | ライモナイト及びサプロライト鉱石からニッケル及びコバルトを回収するための大気浸出プロセス |
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CA1043576A (en) * | 1975-06-10 | 1978-12-05 | Inco Limited | Two stage leaching of limonitic ore and sea nodules |
CA1050278A (en) * | 1975-06-10 | 1979-03-13 | Inco Limited | Leaching limonitic ores |
US4415542A (en) * | 1982-06-21 | 1983-11-15 | Compagne Francaise D'entreprises Minieres, Metallurgiques Et D'investissements | Controlling scale composition during acid pressure leaching of laterite and garnierite ore |
US4548794A (en) * | 1983-07-22 | 1985-10-22 | California Nickel Corporation | Method of recovering nickel from laterite ores |
JP3203707B2 (ja) * | 1991-10-09 | 2001-08-27 | 大平洋金属株式会社 | 酸化鉱石から有価金属を回収する方法 |
JPH0681050A (ja) | 1991-10-31 | 1994-03-22 | Taiheiyo Kinzoku Kk | ニッケル、コバルトの回収方法 |
JP3385997B2 (ja) | 1999-02-12 | 2003-03-10 | 大平洋金属株式会社 | 酸化鉱石から有価金属を回収する方法 |
US6350420B1 (en) * | 1999-10-15 | 2002-02-26 | Bhp Minerals International, Inc. | Resin-in-pulp method for recovery of nickel and cobalt |
AUPS201902A0 (en) * | 2002-04-29 | 2002-06-06 | Qni Technology Pty Ltd | Modified atmospheric leach process for laterite ores |
-
2005
- 2005-03-15 JP JP2006516883A patent/JP4456110B2/ja active Active
- 2005-03-15 EP EP20090165952 patent/EP2108708B1/en active Active
- 2005-03-15 WO PCT/JP2005/004578 patent/WO2005098061A1/ja not_active Application Discontinuation
- 2005-03-15 EP EP05720833A patent/EP1731623A4/en not_active Withdrawn
- 2005-03-15 BR BRPI0505977 patent/BRPI0505977B1/pt active IP Right Grant
-
2009
- 2009-01-09 JP JP2009003888A patent/JP4538073B2/ja active Active
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
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JPS50154111A (ja) * | 1974-05-10 | 1975-12-11 | ||
JP2003514109A (ja) * | 1999-11-03 | 2003-04-15 | ビーエイチピー ミネラルズ インターナショナル インコーポレイテッド | ライモナイト及びサプロライト鉱石からニッケル及びコバルトを回収するための大気浸出プロセス |
Non-Patent Citations (1)
Title |
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See also references of EP1731623A4 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2009515044A (ja) * | 2005-11-10 | 2009-04-09 | コンパニア バレ ド リオ ドセ | 複合浸出プロセス |
JP2012036420A (ja) * | 2010-08-03 | 2012-02-23 | Sumitomo Metal Mining Co Ltd | ニッケル及びコバルトの浸出方法、及びリチウムイオン電池からの有価金属の回収方法 |
WO2024024930A1 (ja) * | 2022-07-28 | 2024-02-01 | 住友金属鉱山株式会社 | ニッケル酸化鉱石の湿式製錬方法 |
Also Published As
Publication number | Publication date |
---|---|
WO2005098061A8 (ja) | 2006-09-21 |
JPWO2005098061A1 (ja) | 2008-02-28 |
JP4456110B2 (ja) | 2010-04-28 |
BRPI0505977A (pt) | 2006-10-24 |
EP2108708B1 (en) | 2014-09-17 |
EP1731623A4 (en) | 2008-09-17 |
EP2108708A1 (en) | 2009-10-14 |
BRPI0505977B1 (pt) | 2013-07-16 |
JP2009102742A (ja) | 2009-05-14 |
JP4538073B2 (ja) | 2010-09-08 |
EP1731623A1 (en) | 2006-12-13 |
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