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WO2023148644A1 - Procédé de récupération de manganèse à partir de minerai de manganèse - Google Patents

Procédé de récupération de manganèse à partir de minerai de manganèse Download PDF

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Publication number
WO2023148644A1
WO2023148644A1 PCT/IB2023/050904 IB2023050904W WO2023148644A1 WO 2023148644 A1 WO2023148644 A1 WO 2023148644A1 IB 2023050904 W IB2023050904 W IB 2023050904W WO 2023148644 A1 WO2023148644 A1 WO 2023148644A1
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WO
WIPO (PCT)
Prior art keywords
manganese
ranging
ppm
group
ore
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/IB2023/050904
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English (en)
Inventor
Arijit Biswas
Kallam Venkata Krishna Reddy
Gajanan U. KAPURE
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Tata Steel Ltd
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Tata Steel Ltd
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Filing date
Publication date
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Publication of WO2023148644A1 publication Critical patent/WO2023148644A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/24—Binding; Briquetting ; Granulating
    • C22B1/2406—Binding; Briquetting ; Granulating pelletizing
    • 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
    • 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
    • C22B47/00—Obtaining manganese
    • C22B47/0018—Treating ocean floor nodules
    • C22B47/0045—Treating ocean floor nodules by wet processes
    • C22B47/0054—Treating ocean floor nodules by wet processes leaching processes
    • 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 disclosure relates to field of metallurgy.
  • the disclosure particularly relates to method for recovering manganese from manganese ore while preventing formation of dithionate. Said method is improved, simple and economical for recovering manganese from the manganese ore.
  • the present disclosure describes an improved method of extraction of manganese from manganese ore without formation of dithionate and significantly reduces the dissolution of iron with manganese during leaching.
  • the present disclosure describes an improved, simple and economical method for extracting/recovering manganese from manganese ore, wherein dithionate formation is prevented and dissolution of iron alongside manganese is significantly reduced or negligible.
  • the method for recovering manganese from manganese ore while preventing formation of dithionate comprises- mixing the manganese ore with sulphur to generate pellets, followed by roasting to obtain roasted pellets; mixing the roasted pellets with solvent to obtain slurry; leaching the slurry with sulphuric acid to obtain leach solution, followed by filtering to obtain leach liquor; and purifying the leach liquor to obtain pregnant leach solution (PLS), followed by recovering the manganese.
  • PLS pregnant leach solution
  • Figure 1 illustrates flow chart depicting the method of recovering manganese from manganese ore according to the present disclosure.
  • Figure 2 illustrates Scanning Electron Microscope (SEM) image depicting roasted sulphated pellets, wherein 1, 2, 6 and 7 (in the image) represent micro structure of Fe2O3.
  • SEM Scanning Electron Microscope
  • Figure 3 illustrates X-ray diffraction plot of roasted manganese ore depicting manganese sulphate as major product.
  • the present disclosure relates to simple, efficient and economical method for recovering manganese from manganese ore including but not limited to lean manganese ore, sub-grade manganese ore and low grade high iron bearing manganese ore.
  • Said method involves treatment of manganese ore through pyro-hydrometallurgical processing for selective extraction/recovery of manganese.
  • the method prevents formation of dithionate during recovering manganese from the manganese ore.
  • the steps followed in the described method for recovering manganese prevents formation of dithionate.
  • Inventors have particularly identified that sulphating roasting (roasting in presence of sulphur) of manganese ore prevents generation of dithionate.
  • the method for recovering manganese from manganese ore while preventing formation of dithionate comprises- mixing the manganese ore with sulphur to generate pellets, followed by roasting to obtain roasted pellets; mixing the roasted pellets with solvent to obtain slurry; leaching the slurry with sulphuric acid to obtain leach solution, followed by filtering to obtain leach liquor; and purifying the leach liquor to obtain pregnant leach solution (PLS), followed by recovering the manganese.
  • PLS pregnant leach solution
  • the mixing of the manganese ore with sulphur comprises- mixing pulverized manganese ore with sulphur powder and binder in presence of moisture and pelletizing to obtain pellets.
  • the pulverization of the manganese ore is carried out by crushing the manganese ore in primary crusher including but not limited to jaw crusher to reduce the size of the manganese ore, followed by subsequently reducing size of the manganese ore by feeding the ore into ball mill or roll pulveriser to achieve pulverized manganese ore having predetermined size which are amenable for roasting and leaching.
  • the pulverized ore used for the pellet making is have a size distribution of about -75+25 micron.
  • the sulphur powder is in an amount ranging from about 20% to 80%, including all the values in the range, for instance, 21%, 22%, 23%, 24% and so on and so forth.
  • the binder is selected from a group comprising sodium, aluminium silicate and a combination thereof.
  • the binder is in an amount ranging from about 20% to 80%, including all the values in the range, for instance, 21%, 22%, 23%, 24% and so on and so forth.
  • the moisture content is ranging from about 3% to 7%, including all the values in the range, for instance, 3.1%, 3.2%, 3.3%, 3.4% and so on and so forth.
  • ratio of sulphur powder to manganese ore is ranging from about 0.1 to 0.8. In an embodiment, the ratio of sulphur powder to manganese ore is about 0.1, about 0.2, about 0.3, about 0.4, about 0.5, about 0.6, about 0.7 or about 0.8.
  • the pellets have size ranging from about 4 mm to 6 mm, including all the values in the range, for instance, 4.1 mm, 4.2 mm, 4.3 mm, 4.4 mm and so on and so forth.
  • the pellets have strength ranging from about 80 Kgf to 150 Kgf, including all the values in the range, for instance, 81Kgf, 82 Kgf, 83 Kgf, 84 Kgf and so on and so forth.
  • the mixing of the manganese ore with sulphur comprises- pulverising the manganese ore to achieve predetermined size of the manganese ore; mixing the pulverized manganese ore, the sulphur powder and the binder in presence of moisture; and pelletizing the mixture to obtain sulphur containing manganese pellet.
  • the pellets are subjected to roasting at a temperature ranging from about 400 °C to 650 °C, including all the values in the range, for instance, 401 °C, 402 °C, 403 °C, 404 °C and so on and so forth.
  • the roasting is carried out for a duration ranging from about 30 minutes to 120 minutes, including all the values in the range, for instance, 31 minutes, 32 minutes, 33 minutes, 34 minutes and so and so forth.
  • the roasting of the pellets is carried out in presence of sulphur dioxide having partial pressure ranging from about 0.1 atm to 0.6 atm.
  • the partial pressure of the sulphur dioxide is about 0.1 atm, about 0.2 atm, about 0.3, about 0.4 atm, about 0.5 atm or about 0.6 atm.
  • air is supplied at a flow rate ranging from about 2 LPM to 10 LPM, including all the values in the range for instance, 2.1 LPM, 2.2 LPM, 2.3 LPM, 2.4 LPM and so on and so forth.
  • feedback control loop is established for addition of air at a flow rate of about 2 LPM to 10 LPM depending on the exit of SO2 from the device, which has direct relationship with partial pressure of SO2 during roasting.
  • the roasting of the sulphur containing manganese pellets is carried out under the atmosphere of O2, N2 and SO2 by maintaining partial pressure of the SO2 to a range of about 0.1 atm to 0.6 atm.
  • the roasted pellets are subjected to cooling until the desired temperature of the pellets are achieved.
  • the roasted pellets are cooled to about 80 °C to 100 °C under non-oxidation environment.
  • roasting of the pellets leads to reduction of manganese ore.
  • the manganese ore in the pellets is partly converted to mixture of manganese oxide and manganese sulphate along with mixture of iron present as hematite and magnetite.
  • roasting of the sulphur containing manganese pellets with sulphur dioxide at a temperature ranging from about 400 °C to 650 °C, for a duration ranging from about 30 minutes to 120 minutes prevents formation of dithionate during leaching.
  • the roasting described herein is selective reductive roasting using combination of sulphur (in the pellets) and sulphur dioxide, which converts manganese from higher oxidation state to lower oxidation state.
  • the Figure 2 illustrates Scanning Electron Microscope (SEM) image depicting roasted sulphated pellets, wherein 1, 2, 5 and 7 (in the image) represent micro structure of Fe2O3.
  • SEM Scanning Electron Microscope
  • the Figure 3 illustrates X-ray diffraction plot of roasted manganese ore depicting manganese sulphate as major product.
  • the roasted pellets are mixed with solvent to obtain slurry.
  • the solvent is selected from a group comprising water, recycled liquor, sulphuric acid and a combination thereof.
  • the slurry has pulp density ranging from about 10% to 25%, including all the values in the range, for instance, 10.1%, 10.2%, 10.3%, 10.4% and so on and so forth.
  • the pellets prior to mixing the roasted pellets with solvent, are pulverized to achieve size ranging from about 50 micron to 150 micron, including all the values in the range, for instance, 51 micron, 52 micron, 53 micron, 54 micron and so on and so forth.
  • the slurry is prepared by mixing the pulverized roasted pellet with recycled water and mother liquor from manganese sulphate crystallization.
  • the slurry was mixed sufficiently for a duration ranging from about 15 to 60 minutes.
  • the slurry has pH ranging from about 3.0 to 5.5. In an embodiment, pH of the slurry is at least 4.
  • the slurry is subjected to leaching in presence of sulphuric acid to obtain leach solution.
  • dosing of the sulphuric acid during leaching is carried out in such manner that the pH of the leach solution is maintained in a range of about 3 to 3.5. In other words, the dosing of the sulphuric acid during the leaching is controlled based on the pH of the leach solution.
  • the sulphuric acid during leaching is added in an amount ranging from about 2 vol% to 10 vol%, including all the values in the range, for instance, 2.1 vol%, 2.2 vol%, 2.3 vol%, 2.4 vol% and so on and so forth, to maintain pH of the solution ranging from about 3 to 3.5.
  • additive selected from a group comprising sodium, sulphur, oxygen, hydrogen and any combination thereof is added in an amount ranging from about 0.5 vol% to 3 vol%, including all the values in the range for instance, 0.6 vol%, 0.7 vol%, 0.8 vol%, 0.9 vol% and so on and so forth.
  • the leaching is carried out in continuous arrangement followed by co-current manner and dosing of the sulphuric acid to maintain pH in the range of about 3 to 3.5 in counter current manner. It is noted that, this way of leaching involving continuous arrangement, co-current manner and by counter current manner provides for improved control over manganese dissolution with higher productivity.
  • the leaching is carried out at a temperature ranging from about 45 °C to 60 °C, including all the values in the range, for instance, 46 °C, 47 °C, 48, °C, 49 °C and so forth, for a duration ranging from about 60 minutes to 180 minutes, including all the values in the range, for instance, 61 minutes, 62 minutes, 63 minutes, 64 minutes and so on and so forth.
  • the leaching is carried until desired values of Mn (II), Fe (II) and Al (III) in the solution is achieved.
  • the leach solution upon stopping the leaching process, is subjected to filtration by technique selected from a group comprising filter press, drum filter and belt filter, to obtain leach liquor.
  • the filtration is carried out to separate solid and liquid in the leach solution to obtain leach liquor.
  • there is no presence of dithionate and free SO2 is below 0.1 g/1.
  • the leach liquor is subjected to purification to obtain pregnant leach solution (PLS).
  • PLS pregnant leach solution
  • total iron in the PLS is less than lg/1, preferably less than 0.5 g/1, more preferably less than 0.2 g/1.
  • purification of leach liquor removes metal selected from a group comprising iron, aluminium, copper, zinc, cobalt, arsenic, lead and any combination thereof.
  • purification of leach liquor is carried out by adding additive mixture and hydrated lime slurry.
  • the additive mixture comprises an oxidizing agent and acid.
  • the oxidizing agent is selected from a group comprising hydrogen peroxide, sodium perchlorate, manganous oxide, potassium permanganate and any combination thereof and the acid is selected from a group comprising, citric acid, acetic acid, ascorbic acid, sulphuric acid, tartaric acid and any combination thereof.
  • the additive mixture is in an amount ranging from about 20 vol% to 50 vol%, including all the values in the range, for instance, 21 vol%, 22 vol%, 23 vol%, 24 vol% and so on and so forth.
  • the hydrated lime slurry is in an amount ranging from about 10% to 25%, including all the values in the range for instance, 11%, 12%, 13%, 14% and so on and so forth.
  • the additive mixture in the purification of leach liquor, is added to the liquor, followed by holding for a duration ranging from about 1 hour to 2 hours.
  • the oxidizing agent in the additive mixture oxidizes Fe (II) to Fe (III).
  • Addition of hydrated lime slurry into liquor increase the pH of the liquor to a range of about 4.4 to 6.3.
  • purification of leach liquor precipitates Fe and Al as hydroxides.
  • the PLS has pH ranging from about 3.2 to 7.7, including all the values in the range for instance, 3.3, 3.4, 3.5, 3.6 and so on and so forth.
  • the PLS comprises about 85 g/L to 110 g/L Mn, about 10 ppm to 80 ppm of Fe, about 5 ppm to 20 ppm of Cu, about 5 ppm to 20 ppm of Co and about 0.5 g/1 to 1.2 g/1 of Al.
  • the PLS is subjected to purification by addition of sulphide compound.
  • the sulphide compound is selected from a group comprising sodium hydro sulphide, ammonium sulphide, potassium hydrosulphide, sodium bisulfate and a combination thereof.
  • the sulphide compound is in an amount ranging from about 10 wt % to 30 wt%, including all the values in the range for instance, 10.1 wt%, 10.2 wt%, 10.3 wt% 10.4 wt% and so on and so forth.
  • the purification of PLS with sulphide compound removes heavy metal selected from a group comprising zinc, copper, nickel, cobalt and any combination thereof and leads to formation of manganese sulphate.
  • the solution after purification by adding sulphide compound comprises about 83 g/L to 98 g/L Mn, about 5 ppm to 20 ppm of Fe
  • the manganese sulphate is subjected to filtration by technique selected from a group comprising nanofiltration, adsorption and ion exchange to remove traces of impurities including but not limited to Fe, Ni, Co, As, Pb, Zn, Se and K.
  • the manganese sulphate is subjected to electrowinning to obtain electrolytic manganese metal (EMM), wherein the electrowinning is carried out by mixing the manganese sulphate with additive and sulphur dioxide.
  • EMM electrolytic manganese metal
  • the additive employed during electrowinning is selected from a group comprising selenium, oxygen, nitrogen, hydrogen, sulphur, oxygen, carbon and any combination thereof.
  • the additive is in an amount ranging from about 0.5 wt% to 10 wt%, including all the values in the range, for instance, 0.6 wt%, 0.7 wt%, 0.8 wt%, 0.9 wt% and so on and so forth.
  • the sulphur dioxide employed during electrowinning is in amount ranging from about 200 ppm to 1000 ppm, including all the values in the range, for instance, 201 ppm, 202 ppm, 203 ppm, 204 ppm and so on and so forth.
  • the solution obtained from the electrowinning is subjected to manganese sulphate crystallization.
  • the crystallization is carried out by adjusting pH of the solution to a range of about 4.0 to 6.0, including all the values in the range, for instance, 4.1, 4.2, 4.4, 4.5 and so on and so forth.
  • the solution obtained from the electrowinning is subjected to production of manganese carbonate.
  • the manganese carbonate is produced by alkaline precipitation.
  • the alkaline precipitation is carried out by adjusting pH of the solution to 6.0 to 8.5, including all the values in the range, for instance, 6.1, 6.2, 6.3, 6.4 and so on and so forth, by employing salt selected from a group comprising sodium carbonate, ammonium carbonate, ammonium bicarbonate and any combination thereof.
  • the Figure 1 provides a flow chart depicting the method of recovering manganese from manganese ore according to the present disclosure.
  • the method of recovering manganese from the manganese ore including but not limited to lean manganese ore, sub-grade manganese ore and low grade high iron bearing manganese ore- Manganese ore is fed to crushing and grinding circuit and screened to obtain minus 30 fraction.
  • This fraction is fed to primary crusher, such as jaw crusher followed by grinding in pulveriser circuit with separation carried out through air classifier circuit.
  • the desired size of fraction of the manganese ore is sent to pelletization circuit, wherein the pulverized ore is mixed with sulphur fines and binder, in presence of desired moisture content.
  • the mixture is mixed thoroughly in mixing drum and eventually passed through pelletization disc to obtain pellets having size ranging from about 4 mm to 6mm, followed by drying the pellets for a duration of about 2 days.
  • the dried pellets are passed through induration furnace to sulphate the manganese ore to reduce the manganese to manganese sulphate for a predetermined duration for induration.
  • the pellets are fired in a rotary tube furnace, with three heating zones.
  • the pellets are pre-heated to a temperature of about 200 °C for a duration of about 20 minutes.
  • the pre-heated pellets are fired at a temperature of about 500 °C for about 1 hour so that the reduction reaction between manganese oxide and sulphur can be carried out.
  • roasted pellets are cooled under SO2 environment to minimize the oxidation of manganese.
  • Pre-cooled manganese ore pellets are pulverized to desired size before leaching.
  • the pulverized fractions of the pellets are mixed with hot water and sulphuric acid to dissolve manganese sulphate in water.
  • sulphuric acid to dissolve manganese sulphate in water.
  • MnO which also forms manganese sulphate in reaction with sulphuric acid.
  • pH of slurry is maintained for dissolution of manganese from the sulphated ore.
  • filtration of the slurry Upon completion of leaching, filtration of the slurry is carried out. During filtration, some part of iron hydroxide which was generated in-situ is filtered. Solids obtained is washed thoroughly to reclaim any residual manganese. The sludge obtained after filtration mostly contains a complex of (MgFe)SO4 and the sludge contains MgSC above 90%.
  • the leach liquor is subjected to purification to obtain pregnant leach solution (PLS), followed by filtration to remove iron.
  • Iron free PLS solution is passed to sulphidizing (by adding sulphide compound) process for removal of heavy metals, including but not limited to nickel, zinc, cobalt and copper as their respective sulphides.
  • the heavy metal precipitates are removed by fine cartridge filtration and subsequently the purified manganese sulphate solution is stored for preparation of manganese salts or subjected to electrowinning (EMM section).
  • part of the solution is subjected to electrodepositing to obtain electrolytic manganese metal (EMM)and part (solution of MnSCU) is bled out of the electro winning.
  • EMM electrolytic manganese metal
  • part of bled out MnSCL solution is taken to purification section to remove heavy metals which is passed through adsorbent bed and eventually for preparation of manganese sulphate, wherein the solution is subjected to evaporation and crystallization.
  • manganese carbonate is also produced by employing alkaline precipitation.
  • the manganese is recovered as electrolytic manganese metal (EMM), manganese sulphate or manganese carbonate.
  • EMM electrolytic manganese metal
  • manganese sulphate manganese carbonate
  • the above described method for recovering manganese is simple and efficient in recovering high purity manganese in the form of EMM, manganese sulphate or manganese carbonate and efficient in preventing formation of dithionate during leaching.
  • the method is environmentally friendly with significant amount of waste water recycling with minimal discharge of off gas and water.
  • Example 1 Recovering Manganese from low grade manganese ore lumps
  • the manganese ore was crushed to size distribution of less than 1mm using jaw crusher and pulveriser based system.
  • the oversized particles were screened and sent again for crushing.
  • Crushed manganese ore which ws sorted out from the dry circuit was sent to the pelletization circuit.
  • Pulverized manganese ore was mixed with sulphur powder in a ratio of about 0.75, followed by adding about 2.5 g of binder and moisture of about 5 g and subjected to pelletization process to obtain pellets of size of about 4 mm and having strength of about 2.5 kg/pellet.
  • the pellets were roasted in a roasting furnace under a partial pressure of SO2 by recycling part of the SO2 from the exist gas. A controlled flow of air was maintained during the roasting. Roasting was carried out at a temperature of about 500 °C for a duration of about 45 minutes.
  • roasted manganese ore was crushed to a size of about 100 micron through a pulveriser circuit.
  • the pulverized roasted ore was mixed with water from recycle stream and fresh water to obtain slurry having pulp density of about 25% and charged into leach reactor for leaching process.
  • dosing of the sulphuric acid was carried out in a manner that pH of the leach solution is maintained at about 3.5. Dosing of the sulphuric acid during the leaching is controlled based on the pH of the solution.
  • intermittent liquid solutions are tested for Mn (II), Fe (II) and Al (III) dissolved in the solution. Upon reaching the desired value of Mn concentration of 85 gpl, the leaching is stopped, and the solution was allowed to stabilize.
  • the leach solution was subjected to filtration through filter press for solid liquid separation and cake washing was carried out to wash out manganese values from the solid cake.
  • the wash liquor was separately recycled in subsequent batch.
  • the leach liquor obtained was subjected to purification by adding additive mixture of oxide (about 30 wt% to 40wt% of hydrogen peroxide) and acid. Subsequently, hydrated lime slurry of about 20 wt % was added and pH of the solution was increased to about 5.5-6.0 to precipitate iron, and aluminium as hydroxide cake. This purification of leach liquor led to pregnant leach solution (PLS).
  • PLS pregnant leach solution
  • Table 3 provides chemical analysis of the solution after removal of iron from PLS through filtration.
  • Table 3 Further, the PLS was subjected to purification through sulphidization by addition of about 30 wt% of sodium hydro sulphide with continuous monitoring of Eh and pH for about 1 to 4 hours to remove heavy metals, such as zinc copper, nickel, cobalt and arsenic.
  • Table 4 provides chemical analysis of solution after sulphidization.
  • Purified PLS is subjected to manganese sulphate preparation, wherein the PLS is adjusted and conditioned to pH of about 4.5 and further was to evaporation and crystallization to obtain manganese sulphate.
  • Example 2 Recovering manganese (manganese carbonate) from low grade manganese ore lumps
  • the purified PLS was subjected to extracting manganese as manganese carbonate by increasing pH of the solution to about 8.0 by addition of alkali or ammonium carbonate.
  • the purified PLS was sent to electrowinning cell for production of manganese metal by electrodeposition. During the process about 0.5 gm additive was added and about 500 ppm SO2 was mixed to the solution and was sent to electrowinning circuit to obtain electric manganese metal (EMM).
  • EMM electric manganese metal

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Abstract

La présente divulgation concerne un procédé simple, efficace et économique de récupération de manganèse à partir de minerai de manganèse, y compris, mais sans y être limité, un minerai de manganèse pauvre, un minerai de manganèse de qualité inférieure et un minerai de manganèse de faible qualité à teneur élevée en fer. Ledit procédé utilise un traitement pyro-hydrométallurgique pour récupérer le manganèse, avec pour résultat d'éviter la formation de dithionate.
PCT/IB2023/050904 2022-02-04 2023-02-02 Procédé de récupération de manganèse à partir de minerai de manganèse Ceased WO2023148644A1 (fr)

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IN202231005991 2022-02-04

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA688892A (en) * 1964-06-16 Zubryckyj Nicolas Process for the treatment of lateritic ores
WO2005012582A1 (fr) * 2003-07-30 2005-02-10 Hitec Energy Limited Traitement hydrometallurgique ameliore de materiaux contenant du manganese
US7951282B2 (en) * 2002-10-10 2011-05-31 Mesa Minerals Limited Hydrometallurgical processing of manganese containing materials
EP3418403B1 (fr) * 2017-06-22 2020-11-18 Lifezone Limited Procédé de traitement hydrométallurgique d'extraction d'éléments précieux, de base et rares
WO2020232505A1 (fr) * 2019-05-21 2020-11-26 Mn Energy Limited Production de sulfate de manganèse

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA688892A (en) * 1964-06-16 Zubryckyj Nicolas Process for the treatment of lateritic ores
US7951282B2 (en) * 2002-10-10 2011-05-31 Mesa Minerals Limited Hydrometallurgical processing of manganese containing materials
WO2005012582A1 (fr) * 2003-07-30 2005-02-10 Hitec Energy Limited Traitement hydrometallurgique ameliore de materiaux contenant du manganese
EP3418403B1 (fr) * 2017-06-22 2020-11-18 Lifezone Limited Procédé de traitement hydrométallurgique d'extraction d'éléments précieux, de base et rares
WO2020232505A1 (fr) * 2019-05-21 2020-11-26 Mn Energy Limited Production de sulfate de manganèse

Non-Patent Citations (1)

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Title
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