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WO2007106969A1 - Processus de récupération de d'espèces métalliques de valeur dans des minerais latéritiques - Google Patents

Processus de récupération de d'espèces métalliques de valeur dans des minerais latéritiques Download PDF

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Publication number
WO2007106969A1
WO2007106969A1 PCT/CA2006/001352 CA2006001352W WO2007106969A1 WO 2007106969 A1 WO2007106969 A1 WO 2007106969A1 CA 2006001352 W CA2006001352 W CA 2006001352W WO 2007106969 A1 WO2007106969 A1 WO 2007106969A1
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WO
WIPO (PCT)
Prior art keywords
fraction
solution
laterite
hci
leaching
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/CA2006/001352
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English (en)
Inventor
Jean-Marc Lalancette
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Nichromet Extraction Inc
Original Assignee
Nichromet Extraction Inc
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Nichromet Extraction Inc filed Critical Nichromet Extraction Inc
Publication of WO2007106969A1 publication Critical patent/WO2007106969A1/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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/08—Chloridising roasting
    • 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
    • C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn process
    • 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
    • C22B23/0423—Halogenated acids or salts thereof
    • 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
    • C22B23/0453—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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
    • 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
    • C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
    • 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 process for recovering value metal species from laterite-type feedstock. More specifically, the present invention relates to a process for recovering metal species such as nickel, cobalt, iron, aluminum and/or magnesium from laterite-type feedstock.
  • Laterite minerals consist of residual weathering products of rocks such as basalts, granites and shales. These metamorphic materials are found on all continents in tropical or semi-tropical zones. They can have variable compositions where iron, aluminum, magnesium and/or silica predominate. In several instances, significant amounts of nickel and cobalt are associated with the dominant constituents.
  • Serpentine minerals can also be found associated with laterites ores.
  • Serpentine is a magnesium-rich silicate mineral that is found as a major constituent in many metamorphic and weathered igneous rocks. Some serpentinic minerals contain significant amounts of nickel and cobalt.
  • Lalancette discloses a closed-circuit method for recovering nickel and cobalt from laterite ores, which essentially comprises the steps of grinding the ore, treating the ore with gaseous hydrochloric acid (gaseous HCI), wherein the remainder of gaseous HCI is scrubbed with water into a concentrated HCI solution, curing the ores in the concentrated HCI solution, followed by filtration of the resulting lixiviate and selective recovery of nickel and cobalt with known techniques. Gaseous HCI is thereafter recycled by roasting or pyrohydrolysis at a minimum of 45O 0 C and returned to the treating stage.
  • gaseous hydrochloric acid gaseous hydrochloric acid
  • Moyes et al. disclose a process for recovering a target metal from an oxidized metalliferous material comprising the steps of: leaching the oxidized metalliferous material with an acidic aqueous halide solution to leach the target metal into solution, the leaching solution being generated by adding sulfuric acid to a solution comprising a metal halide; passing the solution from the leaching stage to a target metal recovery stage in which the target metal is recovered from the solution whilst the metal halide is retained in solution; and returning the solution with the metal halide therein from the target metal recovery stage to the leaching stage.
  • the process preferably comprises two leaching stages, wherein the solid residue from the first leaching stage is directed to the second leaching stage, and the liquid residue of the second leaching stage is at least partially redirected to the first leaching stage.
  • the process also possibly includes a separate hydrohalous acid generation stage in which sulfuric acid is added to a solution comprising the metal halide, thereby forming an acidic leaching solution that is then fed to the second leaching stage and mixed with the first leached solids.
  • the present invention generally relates to an essentially open-circuit process for recovering value metal species from a laterite-type feedstock.
  • an essentially open-circuit process for recovering value metal species from a laterite-type feedstock comprising the sequential or unsequential steps of: a) separating the laterite-type feedstock into a first and a second fraction; b) reacting an acid with a chloride salt in a first compartment, thereby generating gaseous HCI; c) chlorinating the first fraction with the gaseous HCI in a second compartment, thereby producing a chlorinated fraction, wherein excess HCI is recovered and dissolved in water, thereby producing a concentrated HCI solution; d) combining the chlorinated fraction and the second fraction into a mixture; e) leaching the mixture with the concentrated HCI solution in a third compartment, thereby producing a reaction mass; f) submitting the reaction mass to a separation of phases, thereby separating an insoluble residue from a head solution; and g) selectively recovering value metal species from the head solution.
  • Figure 1 is a block diagram illustrating the broad aspects of the process of the present invention.
  • FIG. 2 is a block diagram illustrating the various steps of an embodiment of the process of the present invention. DESCRIPTION OF ILLUSTRATIVE EMBODIMENTS
  • the present invention relates to an essentially open-circuit process for recovering value metal species from a laterite-type feedstock.
  • laterite-type feedstock refers to nickel-containing sedimentary oxide materials that are relatively rich in iron oxide, magnesium oxide and/or aluminum oxide, and/or nickel-containing magnesium-rich silicates, which possibly further contain trace amounts of cobalt and/or chromium.
  • Non-limiting examples of such laterite-type feedstock include laterites, laterite ores, lateritic materials, serpentine, serpentine ores, serpentinic materials and talc.
  • value metal species refers to any valuable metal species that can be found in the laterite-type feedstock, non-limiting examples of which include nickel, cobalt, iron, aluminum, magnesium and chromium.
  • the expression "essentially open-circuit process” means that the process is mainly unidirectional, in a forward direction, that the hydrochloric acid, when combined to give an essentially stable chloride, is not recycled after the leaching step and that a by-product is recovered and used for itself outside the process, without being recycled to a step that precedes its formation in the overall process. It is to be understood that an "essentially open-circuit" process as used herein does not preclude a product or reagent used in the process to be redirected to another step of the overall process.
  • an "essentially stable chloride” refers to a metal chloride that would not be hydrolyzed under oxidant conditions at a temperature less than 400 0 C, a non-limiting example of which is magnesium chloride.
  • an "essentially unstable chloride" non-limiting examples of which are iron or aluminum chlorides.
  • gaseous HCI is generated by reacting an acid with a chloride salt in a first compartment, while the laterite-type feedstock is separated into a first and a second fraction.
  • the hydrochloric acid generation can involve different couples of acid/chloride salts, non-limiting examples of which are sulfuric acid/sodium chloride, sulfuric acid/calcium chloride, sulfuric acid/potassium chloride, nitric acid/sodium chloride, nitric acid/potassium chloride or phosphoric acid/sodium chloride (although this last example is not preferred because of the rather low reactivity of phosphoric acid.
  • Hydrochloric acid is advantageous because of its fast dissolving capability, as compared to sulfuric or phosphoric acid for example. Since hydrochloric acid is about five times more expensive than sulfuric acid on an acidic-proton basis, in situ generation of hydrochloric acid from sulfuric acid provides a substantial economy. In addition, such reaction further generates a sellable product, namely sodium sulfate (in form of a salt cake), used in large amounts in pulp and paper production, glass making and other industries. This by-product may therefore substantially amortize the cost of the reagents required to produce the hydrochloric acid.
  • the amount of gaseous HCI needed is determined experimentally and depends on the feedstock composition. For example, the more iron or magnesium is present in the feedstock, the higher amount of HCI will generally be needed.
  • the acid-generation reaction from sulfuric acid and sodium chloride is performed at a temperature between 300 and 400 0 C and therefore requires an input of energy.
  • the highly reactive hot gaseous HCI by the reaction with the first fraction, liberates a substantial amount of energy so that the following chlorination and leaching steps can be operated without further energy input, which is another significantly cost-effective aspect of the process of the present invention at an industrial scale.
  • the laterite-type feedstock is separated into a magnetic and a nonmagnetic fractions.
  • the "first fraction" used for chlorination is the magnetic fraction, which tends to be more acidic (since it is richer in iron and silica) and therefore less reactive in the presence of another acid.
  • the process of the present invention thus takes advantage of the high reactivity of the hot gaseous HCI produced to operate a reaction that would otherwise have been difficult.
  • the leaching is then done on the combination of the magnetic, chlorinated fraction and the nonmagnetic fraction (which tends to be more basic since it is richer in alumina and magnesia).
  • chlorination and leaching reactions are advantageously performed at temperatures ranging from about 90 to about 12O 0 C, preferably about 100 0 C.
  • the dry chlorination takes approximately 15 to 30 minutes and the wet leaching step preferably for a duration of from 4 to 9 hours.
  • the laterite-type feedstock is simply separated into two fractions of approximately equal weight before treatment by HCI.
  • the chlorination and leaching steps are usually performed at atmospheric pressure, thereby limiting operation costs. These reactions are usually made in vats or stirred reactors.
  • the reaction mass comprised of solid particles and a liquid lixiviate
  • the reaction mass is filtered or centrifuged (separation of phases in Figure 2) and the insoluble residue discarded, optionally after rinsing.
  • the nickel/cobalt chlorides are then recovered from the resulting head solution (to which the rinsing solution is optionally added) by conventional techniques, such as, contacting with selective ion exchange resins, solvent extraction, electrowinning or sulfide precipitation.
  • the first soluble residue after Ni/Co removal is then usually deprived of iron and aluminum by simple pH adjustment in the range of 3-3.5 after aeration.
  • the resulting second soluble residue is then adjusted to a pH ranging between 6 and 7, and reduced in volume so as to separate magnesium chloride, which may be crystallized as a solid and/or commercialized as such.
  • the first soluble residue, still rich in iron (in the form of an essentially unstable chloride), can optionally be hydrolyzed and oxidized in the presence of air at a temperature ranging between about 200 and 400 0 C, preferably between about 200 and 35O 0 C, to liberate a substantial amount of gaseous HCI, which can then be used as a chlorination agent, thereby partly replacing the NaCI/H 2 SO 4 mixture. It is to be understood that such additional step does not necessitate an energy input higher than that required forHCI production by NaCI/H 2 SO 4 .
  • Such hydrolysis converts the essentially unstable iron and aluminium chlorides into insoluble oxides, without affecting the magnesium chloride in the resulting second soluble residue.
  • a simple rinsing may be used to recover it, followed or not by crystallization.
  • the process according to the present invention essentially operates in "open circuit", wherein the essentially stable magnesium chloride is usually recovered as a useful product rather than submitted to a high energy-consuming, high-temperature roasting so as to recycle the hydrochloric acid. Only when a relatively high-iron feedstock allows it, HCI may advantageously be recycled by a hydrolysis at a temperature between about 200 and 400 0 C. In either case, the process according to the present invention may generally lead to surprisingly low operational costs.
  • An additional step of size reduction may be added to the process of the present invention. Indeed, it has been noted that submitting the laterite-type feedstock to grinding before or after the separation step accelerates the reaction and improves the yield of metal recovery. Such grinding preferably takes place before the separation step, particularly in a case of magnetic separation, which is facilitated by smaller particles.
  • the granulometry of the feedstock resulting from such grinding may range between minus 35 and minus 200 mesh, but preferably the whole feedstock would pass through a 120 mesh screen (i.e. granulometry of 100% minus 120 mesh).
  • the process of the present invention can be advantageously applied to laterite-type feedstocks comprising (as a result of an analysis on an ore dried at 100 0 C): 4 to 50% iron, 0.1 to 10% aluminum, ⁇ 1% to 15% magnesium and 0.2 to 5% nickel.
  • the process of the present invention allows a recovery of nickel in the range of about 95 to 99 %, while the magnesium recovery was observed in the range of about 98 percent.
  • the useful products at the end of the process are mainly in the form of chlorides of nickel, cobalt, iron and magnesium and sulfate of sodium.
  • Vycor tube kept at 12O 0 C, at atmospheric pressure.
  • the non-reacted HCI was taken up with water and the reaction completed by leaching of the combined first and second fractions in a stirred reactor at a temperature ranging from 9O 0 C to 12O 0 C, still at atmospheric pressure.
  • a 25 gram sample of this material was submitted to a magnetic separation (wet separation of a 20% solid slurry previously reduced to minus 120 mesh, with a 5000 gauss permanent magnet).
  • the resulting dried magnetic and non-magnetic fractions represented respectively 55% and 45% of the starting sample.
  • the chlorination and leaching were done following the procedure described in Examples 1 to 5, the amount of HCI used being 31.5 g and the duration of the whole digestion being of 6.5 hours at 95 0 C.
  • the workup of the solution gave a recovery of 96% of the nickel and of 91% of the cobalt in the starting sample.
  • iron generally predominates in the feedstock sample and therefore constitutes the biggest consumer of HCI during the whole digestion.
  • An oxydative hydrolysis of the ferrous chloride was performed on the solution after removal of the nickel and cobalt, which allowed regenerating 91% of the HCI used initially for lixiviation.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)

Abstract

L'invention porte sur un processus essentiellement en circuit ouvert de récupération d'espèces métalliques de valeur dans des minerais latéritiques, comportant les étapes suivantes, séquentielles ou non: fractionnement du minerais en une première et une deuxième fraction; réaction d'un acide avec un chlorure dans un premier compartiment pour produire du HCl gazeux; chloration de la première fraction avec le HCl gazeux dans un deuxième compartiment pour produire une fraction chlorée, le HCI en excès étant récupéré, puis dissous dans de l'eau pour donner une solution concentrée de HCl; mélange de la fraction chlorée et de la deuxième fraction; lixivation du mélange par la solution concentrée de HCl dans un troisième compartiment pour doner un mélange réactionnel; soumission du mélange réactionnel à une séparation de phases donnant un résidu insoluble et une solution de tête; et récupération sélective des espèces métalliques de valeur dans la solution de tête.
PCT/CA2006/001352 2006-03-17 2006-08-24 Processus de récupération de d'espèces métalliques de valeur dans des minerais latéritiques Ceased WO2007106969A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CA2,538,962 2006-03-17
CA 2538962 CA2538962C (fr) 2006-03-17 2006-03-17 Processus de recuperation d'espece metallique de valeur a partir de matiere premiere du type laterite

Publications (1)

Publication Number Publication Date
WO2007106969A1 true WO2007106969A1 (fr) 2007-09-27

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PCT/CA2006/001352 Ceased WO2007106969A1 (fr) 2006-03-17 2006-08-24 Processus de récupération de d'espèces métalliques de valeur dans des minerais latéritiques

Country Status (7)

Country Link
AU (1) AU2006203772B2 (fr)
BR (1) BRPI0601562B1 (fr)
CA (1) CA2538962C (fr)
CO (1) CO5700172A1 (fr)
DO (1) DOP2006000123A (fr)
GT (1) GT200600140A (fr)
WO (1) WO2007106969A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8961649B2 (en) 2007-08-29 2015-02-24 Vale Canada Limited System and method for extracting base metal values from oxide ores
CN105648238A (zh) * 2014-12-08 2016-06-08 张家彦 一种获取镍基料的制备方法
JP2017520687A (ja) * 2014-07-18 2017-07-27 アライアンス・マグネシウム 純マグネシウム金属及び様々な副産物を生産するための方法
CN109385539A (zh) * 2018-10-09 2019-02-26 钢控股集团有限公司 一种针对印尼当地的红土镍矿湿法冶炼方法
CN113042201A (zh) * 2021-03-30 2021-06-29 酒泉钢铁(集团)有限责任公司 一种高磷赤铁矿提铁除磷工艺
WO2021196773A1 (fr) * 2020-03-30 2021-10-07 中南大学 Procédé de lixiviation sous pression de minerai de nickel latéritique au moyen d'acide phosphorique

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BRPI0612374B1 (pt) 2006-11-10 2015-08-11 Vale Sa Processo de recuperação de níquel e cobalto a partir de minérios lateríticos empregando resina de troca iônica e produto contendo níquel ou cobalto
WO2012126092A1 (fr) 2011-03-18 2012-09-27 Orbite Aluminae Inc. Procédés permettant de récupérer des éléments de terres rares à partir de matériaux renfermant de l'aluminium
EP2705169A4 (fr) 2011-05-04 2015-04-15 Orbite Aluminae Inc Procédés d'extraction d'éléments de terres rares dans divers minerais
AU2012308068B2 (en) 2011-09-16 2015-02-05 Aem Technologies Inc. Processes for preparing alumina and various other products
CA2857574C (fr) 2012-01-10 2015-03-24 Orbite Aluminae Inc. Procedes de traitement de boue rouge
RU2633579C9 (ru) 2012-03-29 2017-12-25 Орбит Алюминэ Инк. Способы обработки летучей золы
BR112015000626A2 (pt) 2012-07-12 2017-06-27 Orbite Aluminae Inc processos para preparação de óxido de titânio e outros produtos variados
US9353425B2 (en) 2012-09-26 2016-05-31 Orbite Technologies Inc. Processes for preparing alumina and magnesium chloride by HCl leaching of various materials
US9534274B2 (en) 2012-11-14 2017-01-03 Orbite Technologies Inc. Methods for purifying aluminium ions

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3661564A (en) * 1969-11-19 1972-05-09 Nickel Le Extraction of cobalt and nickel from laterite
US4269817A (en) * 1979-07-27 1981-05-26 Battelle Memorial Institute Production of chlorine from chloride salts
WO2002008477A1 (fr) * 2000-07-21 2002-01-31 Nichromet Extraction Inc. Récupération du nickel et du cobalt dans les minerais latéritiques
WO2002053788A1 (fr) * 2000-12-29 2002-07-11 Nichromet Extraction Inc. Procede de recuperation de metaux de base et de metaux precieux par chloruration extractive
US6767528B2 (en) * 1997-07-01 2004-07-27 John E. Stauffer Manufacture of hydrogen chloride from salt and sulfuric acid

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3661564A (en) * 1969-11-19 1972-05-09 Nickel Le Extraction of cobalt and nickel from laterite
US4269817A (en) * 1979-07-27 1981-05-26 Battelle Memorial Institute Production of chlorine from chloride salts
US6767528B2 (en) * 1997-07-01 2004-07-27 John E. Stauffer Manufacture of hydrogen chloride from salt and sulfuric acid
WO2002008477A1 (fr) * 2000-07-21 2002-01-31 Nichromet Extraction Inc. Récupération du nickel et du cobalt dans les minerais latéritiques
WO2002053788A1 (fr) * 2000-12-29 2002-07-11 Nichromet Extraction Inc. Procede de recuperation de metaux de base et de metaux precieux par chloruration extractive

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8961649B2 (en) 2007-08-29 2015-02-24 Vale Canada Limited System and method for extracting base metal values from oxide ores
JP2017520687A (ja) * 2014-07-18 2017-07-27 アライアンス・マグネシウム 純マグネシウム金属及び様々な副産物を生産するための方法
US10563314B2 (en) 2014-07-18 2020-02-18 Alliance Magnésium Inc. Hydrometallurgical process to produce pure magnesium metal and various by-products
CN105648238A (zh) * 2014-12-08 2016-06-08 张家彦 一种获取镍基料的制备方法
CN105648238B (zh) * 2014-12-08 2018-07-13 张家彦 一种获取镍基料的制备方法
CN109385539A (zh) * 2018-10-09 2019-02-26 钢控股集团有限公司 一种针对印尼当地的红土镍矿湿法冶炼方法
WO2021196773A1 (fr) * 2020-03-30 2021-10-07 中南大学 Procédé de lixiviation sous pression de minerai de nickel latéritique au moyen d'acide phosphorique
CN113042201A (zh) * 2021-03-30 2021-06-29 酒泉钢铁(集团)有限责任公司 一种高磷赤铁矿提铁除磷工艺

Also Published As

Publication number Publication date
AU2006203772A1 (en) 2007-10-04
DOP2006000123A (es) 2007-11-15
BRPI0601562B1 (pt) 2013-12-31
AU2006203772B2 (en) 2010-08-26
CA2538962A1 (fr) 2007-09-17
CA2538962C (fr) 2013-10-29
GT200600140A (es) 2006-11-22
BRPI0601562A (pt) 2007-11-06
CO5700172A1 (es) 2006-11-30

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