US20070131058A1 - Process for recovering platinum group metals from ores and concentrates - Google Patents

Process for recovering platinum group metals from ores and concentrates Download PDF

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US20070131058A1
US20070131058A1 US10/564,735 US56473504A US2007131058A1 US 20070131058 A1 US20070131058 A1 US 20070131058A1 US 56473504 A US56473504 A US 56473504A US 2007131058 A1 US2007131058 A1 US 2007131058A1
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pgm
recited
salt
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temperature
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Mario Bergeron
Marc Richer-Lafleche
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Ressources Minieres Pro Or Inc
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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
    • 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
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet 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
    • C22B11/00—Obtaining noble metals
    • C22B11/06—Chloridising
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1204—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 preliminary treatment of ores or scrap to eliminate non- titanium constituents, e.g. iron, without attacking the titanium constituent
    • C22B34/1209—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 preliminary treatment of ores or scrap to eliminate non- titanium constituents, e.g. iron, without attacking the titanium constituent by dry processes, e.g. with selective chlorination of iron or with formation of a titanium bearing slag
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/30—Obtaining chromium, molybdenum or tungsten
    • C22B34/32—Obtaining chromium
    • 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 carbochlorination technique involves using gaseous chlorine in the presence of a reductant such as carbon monoxide, usually chosen for process development, or coke.
  • the chlorination technique involves the use of chlorine without the addition of a reductant agent.
  • the third technique, chlorination in the presence of a salt melt involves the addition of a large quantity of salt so as to form a molten bath of salt, with or without the generation of gaseous chorine.
  • the carbochlorination, chlorination and chlorination in the presence of a salt melt techniques differ in the chemical reactions that are involved in each of them.
  • U.S. Pat. No. 5,102,632 issued to Allen et al., 1992, relates to a method of recovering platinum, palladium and rhodium dispersed on ceramic support structures.
  • the process involves two steps. In a first step a reducing chlorination is carried out during which the palladium and platinum are volatilized as chlorides. In a second step only chlorine is used to volatilize rhodium trichloride.
  • the method described Involves mixing the ore with NaCl 10% wt/wt, dry chlorination of the mixture between 350° C. to 800° C. with gaseous chlorine, dissolution of PGM in concentrated hydrochloric acid solution, filtering and recovering the PGM from the solution.
  • PGM recoveries are reported to be in the order of 95 to 100%.
  • Canadian Patent application no. 2,314,581 in the name of Craig and Grant, 2000 describes a method for the removal of base metals, especially the amphoteric elements present in metallurgical concentrates containing 60 wt % and more of precious metals.
  • the presence of the base metals in the precious metals concentrates is considered to be detrimental to the down stream refining steps.
  • the method described comprises the following steps: a) a high temperature treatment of the concentrate with gaseous HCl; b) a treatment of the residue, if desirable, with chlorine gas, C) a high temperature treatment of the residue with oxygen, d) a high temperature treatment of the residue with hydrogen. This procedure minimizes losses of precious metals during the removal of the amphoteric elements.
  • This process would desirably be adaptable to a situation where a chromite is subjected to an enrichment process as described in co-pending no PCT/CA2004/000165 by Bergeron and Laflèche by which the iron is extracted as gaseous FeCl 3 .
  • This treatment could desirably be designed so that it could be performed simultaneously to the enrichment of chromites.
  • This method can thus be used to recover PGM from PGM concentrates and chromites products.
  • the production of a flotation concentrate is advantageously not required, so that ores previously discarded because not amenable to flotation or not presenting sufficient economical value to justify the cost of the production of a flotation concentrate can be brought into production.
  • the enrichment of chromites and the PGM extraction may be performed simultaneously, therefore increasing the total value of the ore.
  • the mineralogical phases carrying the PGM may be converted into chloride complexes highly soluble in a slightly acidic solution.
  • the PGM may be extracted from the chromites with assistance of a catalyst system, which increases the kinetic of the reaction and the solubility of the PGM chemical species obtained by the process.
  • the process includes steps to ensure the secure disposal of the residue.
  • the process includes, steps by which the majority of the employed reagents may be recycled.
  • the present invention is advantageously applicable to chromite ores and different types of concentrates including alluvial chromites and PGM concentrates. If concentrates are used as feed to the invention, the concentrates can be obtained, after grinding of the ore, by the use of standard mineral processing technologies such as jigs, spirals, flotation units and multi-gravity separator.
  • a method for recovering platinum group metals (PGM) from a feed material selected from the group consisting of chromite ore, chromite ore concentrate and PGM concentrate comprising a) carbochlorinating (Cl 2 ,CO) the material having a homogenous grain-size, In a reactor maintained at a temperature of between about 240° C. and about 800° C.
  • a method for recovering at least one platinum group metal (PGM) species from a feed product selected from the group consisting of chromite ore, chromite ore concentrate and PGM concentrate comprising the steps of: mixing the feed with at least one salt so as to produce a mixture, whereby the concentration of salt in the mixture is sufficient to convert at least one PGM species into a corresponding PGM chloride salt; and contacting the mixture with gaseous chlorine and CO at a temperature between about 240° C. and 800° C. to induce the conversion of at least one species of PGM into a corresponding PGM chloride salt, whereby said chloride salt of at least one PGM species can be recovered.
  • PGM platinum group metal
  • the temperature is between about 250° C. and about 800° C. In a more specific embodiment, the temperature is between about 350° C. and about 800° C. In a more specific embodiment, the temperature is between about 500° C. and about 800° C. In a more specific embodiment, the temperature is between about 500° C. and about 720° C. In a more specific embodiment, the temperature is between about 600° C. and about 800° C. In a more specific embodiment, the temperature is between about 620° C. and about 800° C. In a more specific embodiment, the temperature is between about 650° C. and about 800° C. In a more specific embodiment, the temperature is between about 660° C. and about 800 20 C.
  • the temperature is between about 500° C. and about 720° C.
  • the carbochlorination is performed at a flow rate of at least 20 ml/min.
  • the at least one salt is selected from the group consisting of NaCl, KCl and MgCl2 and a combination thereof.
  • the salt is NaCl.
  • NaCl forms at least about 5% w/w of the mixture.
  • NaCl forms about 5% to about 20% w/w of the mixture.
  • the at least one salt is selected from the group consisting of NaCl, KCl and MgCl2 and a combination thereof. In a more specific embodiment, the at least one salt is in a concentration of about 5% w/w to about 10% w/w in the mixture.
  • the at least one salt is NaCl in a concentration of about 5% w/w to about 10% w/w in the mixture. In a more specific embodiment, the at least one salt is NaCl in a concentration of about 5% w/w in the mixture. In a more specific embodiment, the step of chlorinating the mixture is performed with a chlorine flow rate of at least about 60 ml/min. In a more specific embodiment, the step of chlorinating the mixture is performed with a chlorine flow rate of at least about 200 ml/min. In a more specific embodiment, the temperature is between about 250° and about 720° C. In a more specific embodiment, the temperature is between about 670° and about 720° C. In a more specific embodiment, the Cl 2 /CO ratio is between about 0.5 and about 1.5.
  • the methods further comprises one or more of the following steps or characteristics: the mixture is dried before chlorination; N 2 is used as a carrier gas during chlorination; the duration of the chlorination is about 30 minutes to about 2 hours, or more specifically, the duration is about 2 hours.
  • the method of the present invention may comprise the following steps.
  • a feed material selected from the group consisting of chromite ore, chromite ore concentrate and PGM concentrate The size of the feed material used depends on the degree of liberation of the chromite ore or concentrate or PGM concentrate grain-size in the matrix from which it is extracted;
  • the feed with at least one salt to yield a mixture having a salt concentration of about 5% (w/w) to about 10% (w/w), the at least one salt acting as a catalyst for the chlorination reactions.
  • the NaCl concentration used is also sufficient to convert PGM species into soluble PGM chloride salts;
  • drying step can be carried out at different temperatures and time periods. In specific embodiments, this step is conducted at about 180° C. for about 30 minutes to about 2 hours to yield a dried feed containing salt. In a specific embodiment, the drying step is conducted about 180° C. for 30 minutes.;
  • the chlorination reactor is desirably a furnace built with material resistant to chlorine. In specific embodiments, for the chlorination is conducted for a period of time varying from about 30 minutes to about two hours.
  • PGM phases present in the chromites react with Cl 2 , CO and NaCl to produce PGM chlorides salts that are soluble in water and HCl solutions; and FeCl 3 is produced by the reaction FeO.Cr 2 O 3 +1.5Cl 2 (g)+CO(g) Cr 2 O 3 +FeCl 3 (g)+CO 2 (g) and carried outside the reactor by the flow thru of the gaseous phase, and a portion of the PGM chlorine salts are contained in said solid residue, and an other portion of the PGM chlorine salts are contained in the gaseous phase;
  • FeCl 3 can be recovered from the FeCl 3 concentrate by washing with water or a solution of HCl and yield aqueous FeCl 3 —FeCl 3 being highly soluble in water;
  • the HCl has a molarity varying between about 0.1 an about 3 M HCl.
  • This step may optimally be conducted under agitation. This extraction of PGMs from the gaseous phase may be conducted simultaneously and in the same tank as the extraction of PGMs from the solid phase;
  • CO can desirably be burned with air to yield gaseous CO 2 ;
  • step j) advantageously, the Cl 2 and NaOH generated in step j) may be recycled as reactants for the chlorination and neutralization reactions, and H 2 generated in step k) may be recycled as additional combustible for the chlorination reactor;
  • HCl may vary between about 0.1 to about 3 M HCl. This contact may suitably be performed for about 10 to about 20 minutes under agitation.
  • the agitation step may include heating or boiling of the mixture.
  • the digestion is conducted at a temperature of 70° C.
  • the ratios (w/w) of water/enriched solid material or HCl/enriched solid material vary between about 2.5 to about 50.
  • step m) separating the mixture of step m) to obtain: i) a solid residue showing an increase in its chromium to iron ratio as compared to that of the starting feed and; ii) a leached solution containing dissolved PGM species;
  • the HCl solution may be recycled or a HCl 6 M solution regenerated by distillation, this latter solution being used to prepare the HCl solution having a molarity of about 0.1 to about 3 M.
  • a method for the extraction of PGM from a starting feed selected from the group consisting of chromite ore, chromite ore concentrate and PGM concentrate wherein even when the feed is a chromite product, the extraction of FeCl 3 is minimized or is not occurring.
  • This method differs from the above-presented method at least in that: 1) In addition to chromite ore and concentrates, PGM concentrates can be used; 2) There is no reason to believe that there is an upper concentration limit (w/w) for the salt when the Cr/Fe ratio increase is not desirable: there is no reason to believe that salt could be detrimental at certain concentrations to PGMs; 3)
  • the upper temperature limit may be as high as 800° C.
  • the leaching solution of the gaseous phase is used instead of HCl to digest the solid residue and the digestion was performed at 70° C.;
  • the starting feed is a chromite ore.
  • the starting feed is a chromite concentrate obtained by a suitable mineral processing technology.
  • the starting feed is a PGM concentrate obtained by a suitable mineral or metallurgical processing technology such as a flotation concentrates and metallurgical mattes.
  • FIG. 1 illustrates a flow diagram of a specific embodiment of the present invention in which the PGM are collected in two separate leaching solutions.
  • FIG. 2 illustrates a flow diagram of a specific embodiment of the present invention in which the PGM are collected in one leaching solution.
  • the feed to the process can be the direct ore or an ore concentrate obtained from an appropriate mineral processing technology.
  • the feed used Is from a massive chromite layer obtained from the Menarik deposit (James Bay, Quebec).
  • the average mineralogy of 29 massive chromite layers of the Menarik Complex is: chromite 45%, chlorite 32%, serpentine 13%, magnetite 3%, talc 1%, hornblende 4%, and traces of sulfides.
  • the sample was hand-picked from the chromite mineralized zone Cr-3 and subsequently ground to 125 ⁇ m.
  • the ore or concentrate was mixed with a solution of NaCl to obtain, after drying, a feed containing 5% NaCl (w/w) by weight.
  • the combined action of NaCl and FeCl 3 created during the carbochlorination step, caused the formation of a eutectic point in the system NaCl—FeCl 3 .
  • This mixture acted as a catalyst for the chlorination reactions.
  • the salt addition produces a thin liquid film around each grain.
  • This liquid film contains a strong chlorination agent such as: 1) NaFeCl 4 resulting from the reaction of FeCl 3 with NaCl or 2) dissolved iron species acting as chlorine supplier to the chlorination sites.
  • PGM chloride salts of the type Na 2 PtCl 6 , Na 2 PdCl 4 , Na 3 RhCl 6 , Na 2 IrCl 6 , etc., which are highly soluble in water or in diluted hydrochloric acid (Pascal, 1958, Wunsch traité de chimie minérale, Masson et Cie, Tome 19, pp. 949). It is understood from the person of ordinary skill in the art that other types of salts such as KCl and MgCl 2 can be used to produce a catalytic system for the carbochlorination of feed materials such as chromite ores or concentrates of PGM concentrates.
  • the drying step ensures a complete removal of water resulting from the salt addition and can be carried out at different temperatures and time periods.
  • the mixture was dried at 180° C. for 30 minutes. After cooling, the charge was transferred in the chlorination reactor and pre-heated at the selected reaction temperature.
  • Pascal 1958 reports that all PGM in their pure metallic forms react with gaseous chlorine to form chlorides compounds at temperature generally above 240° C. He reports that that the pure metallic forms of platinum forms a PtCl 2 at 240° C., palladium forms PdCl 2 at 300° C., rhodium forms RhCl 3 at 300° C., iridium forms IrCl 3 at 600° C., ruthenium forms RuCl 3 at 350° C. and osmium forms OsCl 4 at 650° C. Highly soluble metallic salts of PGM metals can then be derived from the chlorides compounds when these are contacted with NaCl.
  • the catalytic system previously described in the present application involving a molten salt bath of NaCl/FeCl 3 containing dissolved gaseous Cl 2 was surprisingly found to form metallic salts of PGM.
  • the formation of PGM chloride salts from PGM species found in ores and concentrates was found to be desirable to avoid the formation of volatile chloride such as PtCl 2 and PdCl 2 and their escape in different process streams.
  • the presence of a salt therefore during the carbochlorination step desirably ensures the conversion of PGM species into corresponding PGM chloride salts rather than their conversion into Insoluble species.
  • the examples presented below indicate that, except for osmium, the metallic salts of PGM do not escape from the molten salt bath and therefore are not present in other process streams.
  • the feed is contacted with chlorine, CO and NaCl so as to promote the formation of the PGM metallic salts.
  • the carbochlorination step is conducted in a horizontal static furnace at temperature varying from 240° C. to 800° C. According to the present invention, the chlorination reactions enabling PGM recovery can advantageously be performed according to two modes.
  • the PGM are converted into metallic salts with simultaneous extraction of gaseous FeCl 3 .
  • the carbochlorination conditions are set to optimize the rate of FeCl 3 removal. optimally these conditions involve temperature in the range of about 670° C., Cl 2 /CO ratio of about one and a relatively high flow rate of about 60 ml/min to about 220 ml/min for both Cl 2 and CO. It is to be noted that a flow rate lower than 60 ml/min may also achieve a certain increase in the Cr/Fe ratio but it is not optimal. It has been shown that this increase is close to zero when a flow rate of 20 ml/min is used.
  • the precise flow rate at which the Cr/Fe remains stable may be determined routinely in the art in each specific reactor in which the carbochlorination is performed. It is also to be noted that there is no known risk of increasing the chlorine flow rate. Of course, it is advantageous to keep the flow rate (i.e. the quantity of chlorine used) as low as possible to decrease costs. See also co-pending application no PCT/CA2004/000165 for more details on optimal conditions for increasing Cr/Fe ratio of chromites.
  • the chemical reaction desirably occurring during carbochlorination is the following: FeO.Cr 2 O 3 +1.5Cl 2 (g)+CO(g) Cr 2 O 3 +FeCl 3 (g)+CO 2 (g)
  • the ⁇ G 0 T versus temperature of this reaction was calculated using the HSCTM software of Outokumpu. They are presented at FIG. 3 of co-pending application no. PCT/CA2004/000165.
  • the ⁇ G 0 T values were inferior to ⁇ 150 Kjoules. This demonstrates the thermodynamic feasibility of the reaction.
  • the iron contained in the chromite product reacts with Cl 2 to form FeCl 3 .
  • FeCl 3 is in a vapour state. Because of the continuous flow of gas passing through the reactor, FeCl 3 Is carried outside the reactor, where it is condensed.
  • An acceptor such as CO(g) for the oxygen liberated during the chlorination reaction may be added to maintain reducing conditions.
  • the addition of CO(g) limits the probability that the reaction 2FeCl 3 +3/2O 2 ⁇ Fe 2 O 3 +3Cl 2 will occur. Thereby, no detectable precipitation of unwanted solid hematite takes place in the reactor.
  • ferrous chloride FeCl 2 Another significant reaction occurring according to an embodiment of the present invention is the formation of ferrous chloride FeCl 2 during the carbochlorination phase.
  • Ferrous chloride (FeCl 2 ) having a high melting point of 670° C., hence a temperature higher than that used during the carbochlorination according to certain embodiments of the present invention, a rapid chlorination of FeCl 2 into ferric chloride (FeCl 3 ) according to the reaction 2FeCl 2 +Cl 2 2FeCl 3 (g) may be desirable in these specific embodiments in order to avoid the production of a diffusion barrier by the formed solid ferrous chloride. This barrier may decrease the chlorine access to the reaction sites.
  • carbochlorination is performed with a salt such as NaCl, KCl and MgCl 2 to produce a catalytic melt when NaCl combines with FeCl 2 and/or FeCl 3 so as to Increase the volatilization (the removal) of iron as gaseous FeCl 3 from the carbochlorination reactor.
  • a salt such as NaCl, KCl and MgCl 2
  • the carbochlorination conditions are optimized for the conversion of PGM to metallic salts.
  • the expulsion of FeCl 3 outside the reactor was minimised by using a low flow rate of about 20 ml/min for both Cl 2 and CO.
  • the feed was maintained in contact with Cl 2 and CO for about 2 hours.
  • the carbochlorination temperature is varied from about 240° C. up to about 800° C. depending on the nature of the ores or concentrates, although there is no known advantage for using a temperature higher than that at which all PGM species are dissolved, namely about 660° C. Indeed PGM species recovery was observed to be equivalent at temperatures of 660° C. and 720° C. (see Examples 1 to 4 below).
  • chlorination reactions for all Examples presented below were conducted in a simple horizontal static furnace.
  • chlorination is realized in fluidized bed reactors constructed of acid resistant bricks enclosed in a metal shell. Since the salt addition results in the formation of a thin liquid film layer around the chromite grains, which increases their adherence properties, it may be desirable to avoid fluidized reactor in order to avoid problems associated with grains agglomeration and bed sedimentation.
  • Alternatives to fluidized bed reactor include a vertical static reactor and a horizontal rotating reactor.
  • inventions of the present invention may include the use of solid reducing agents like coal or coke instead of CO which may be onerous for industrial scale methods.
  • solid reducing agents like coal or coke
  • CO may be onerous for industrial scale methods.
  • coal and coke react with oxygen to form CO so that the end result is similar to that obtained when CO is directly introduced in the chlorination reactor.
  • Pelletizing-sintering procedures similar to the ones employed in the ferrochromium industry, can be performed before the chlorination step.
  • the solid upgraded chromites minerals ( 6 ) contained in the reactor were dumped.
  • the gas flow rate, the salt additives, the Cl 2 /CO ratio, the chlorinated solid residue showed an increase in its chrome to iron ratios and variable proportions of PGM species have been converted into metallic salts.
  • the chlorinated solid residue was then placed in contact with water or a HCl solution having a molarity of about 0.1 to about 3 M in a digester ( 38 ).
  • the pulp was agitated for about 15 minutes.
  • the solution was heated or boiled during the agitation period and the digester was equipped with a condensing system.
  • the HCl solution was alternatively replaced by water.
  • the carbochlorination step the osmium value was transported in the vapor phase and was not affected by the condensation of FeCl 3 .
  • the digester pulp was filtered.
  • the solution containing the dissolved PGM salts was subjected to Zn cementation or an ion exchange procedure ( 44 ) to recover a PGM concentrate ( 46 ).
  • the solid phase ( 48 ) isolated from the filtration process showed an increase in its chromium to iron ratio and could be commercialized, among other things, as an enriched chromite feed for a ferrochromium furnace.
  • the Os contained in the quenching solution was recovered by Zn cementation or an ion exchange procedure ( 50 ).
  • the solution containing the quenched Os was used to digest the solid residue obtained at the end of the carbochlorination step ( 52 ).
  • the process used diluted HCl. Only a slight quantity of HCl was consumed in the process. Hence, the HCl digesting solution could be recycled to the digester ( 38 ). The HCl solution was re used until pH rose to a value diminishing the PGM solubility. A 6 M HCl solution ( 58 ) was regenerated by distillation ( 56 ). The pH of the digesting solution was adjustable to the required value by water dilution ( 60 ).
  • the solid amorphous iron oxides were isolated from the liquid phase by an appropriate solid-liquid separation such as centrifugation or press filtration ( 31 ).
  • the filtration cake was discharged to the tailings.
  • the aqueous NaCl solution ( 32 ) was directed to an electrolysis cell ( 34 ).
  • the NaCl solution ( 32 ), obtained from the neutralization step of the process, is electrolyzed by a chlor-alkali membrane cell process.
  • the reaction involved is: 2NaCl(aq)+2H 2 O H 2 (g)+Cl 2 (g)+2NaOH(aq)
  • the gaseous Cl 2 and aqueous NaOH generated by the reaction are recycled in the process.
  • the Cl 2 is returned ( 36 ) to the carbochlorination reactor ( 5 ) and the aqueous NaOH is directed ( 31 ) in the neutralization reservoir ( 28 ).
  • the H 2 (g) produced (not shown) by this reaction can be employed as the main energy source or an additional energy source for the carbochlorination reactor ( 5 ). External supplies of NaCl can be used if needed.
  • the experiments were performed on a massive chromitite layer obtained from the Menarik deposit (James Bay, Quebec).
  • the average mineralogy of 29 massive chromite layers of the Menarik Complex is: chromite 45%, chlorite 32%, serpentine 13%, magnetite 3%, talc 1%, hornblende 4% and traces of sulfides.
  • the sample was hand-picked from the chromite mineralized zone Cr-1 and subsequently grinded to about 125 ⁇ m and homogenized.
  • the individual concentrations of Pd, Pt, Ir, Rh, Ru and Os contained in the samples were analyzed by a nickel sulfide fire-assay procedure adapted to chromite followed by a finish by inductively coupled plasma mass spectrometry, ICP-MS. These concentrations were used as a reference point for the calculation of the PGM recovery during the carbochlorination experiments.
  • the major and complementary trace elements were analyzed by inductively coupled plasma atomic emission spectroscopy, ICP-AES, after a fusion procedure specifically applicable to chromite ore.
  • the solid contained in furnace (the residue) and the condensate were digested in either water or 0.1 M to 3 M HCl solutions.
  • the residue, representing the solid present in the furnace after the experiment, the condensate, representing the gas condensed on the side of the tube and the gas phase, representing the vapor reaching the quenching vessel were analyzed separately for the PGM, see Table 1 and FIGS. 1 and 2 .
  • H ppb ppb ppb ppb ppb ppb ppb ppb CR-1a NiS Nickel sulphide fire-assay 1019 274 17 15 79 55 CR-1b, NiS Nickel sulphide fire-assay 1208 317 20 18 87 61 CR-1d, NiS Nickel sulphide fire-assay 1281 314 22 20 96 68 CR-1 average Nickel sulphide fire-assay 1169 301.7 19 18 87 61 PGM-1, residue 5% NaCl, 3 M HCl 220 220 1 720 2 1122 248 31 2.9 94 114 PGM-1, condensate 5% NaCl, 3 M HCl 220 220 1 720 2 ND ND ND ND PGM-1, gas 5% NaCl, 3 M HCl 220 220 1 720 2 47 17 ⁇ 1 69 ⁇ 1 ⁇ 0.6 PGM-1, TOTAL 5% NaCl, 3 M HCl 220
  • a ten-gram sample of the chromite CR-1 was mixed with a NaCl solution. After drying, the salt content of the mixture was 5% by weight. This material was loaded in the reactor and the temperature was raised to 720° C. in the presence of N 2 . Once the reaction temperature was reached, 200 ml/min of Cl 2 and 200 ml/min of CO were flow through the reactor. The mixture of gas was maintained in contact with the solid for 2 hours. Ten minutes after the introduction of the gas mixture, the evolution of FeCl 3 exiting the reactor and condensing outside the reactor in the condenser area was noted. The gas phase escaping the condenser area was quenched in a 3 M HCl solution.
  • the reactor was cooled down to room temperature. Nitrogen was flushed In to the reactor during the cooling period. The solid left in the reactor, the residue, was transferred in a glass beaker and on a hot plate. One hundred ml of a 3 M HCl solution was added to the residue. The mixture was agitated for 15 minutes at 70° C. After the agitation period, the mixture was filtered and the resulting clear solution was analysed for PGM by ICP-MS. The solid condensate (mostly FeCl 3 ) was recovered from the condenser area by washing with 3 M HCl. The condensate was digested using exactly the same digesting procedure as the one used for the residue. The quenching 3 M HCl solution used as a trap for the PGM contained in the gas phase was analysed directly for the PGM.
  • the distribution of the PGM in the residue and in the gas phase are presented at the Table 1 for the sample noted PGM-1.
  • the sums of the PGM for the residue and the gas phase were: Pd 1169 ppb, Pt 265 ppb, Ir 31 ppb, Os 72 ppb, Rh 94 ppb and Ru 114 ppb.
  • the PGM concentrations obtained from the nickel sulphide fire-assay, reported at the Table 1 can be used as the 100% recovery mark.
  • the sums of PGM values in the residue and the gas phases were recalculated as per cent recovery at Table 2.
  • the experimental error, including sample homogeneity, is in the order of ⁇ 15%.
  • the recoveries are within 100 ⁇ 15% limits and are considered here as complete.
  • Ru and Os the recoveries exceeded 100 ⁇ 15% limits. Os is considered as being loss as OsO 4 during the fusion stage in the NiS fire-assay method. Therefore, it is not surprising that the recovered value by carbochlorination exceeded by a factor 4 the expected value in the starting ore.
  • the carbochlorination process appears to be a superior approach to NiS fire-assay for achieving complete dissolution of these two specific PGM in chromites. Losses of Ru as RuO 4 are also reported during the fusion stage. Nickel sulphide fire-assay shows limits when applied to chromite and often the slag must be refused to achieve complete recovery of PGM.
  • the process is able to achieve complete extraction of substantially all PGM from the feed.
  • PGM are leached from the residue and gas phase streams, losses of PGM to the condensate stream appear to be negligible.
  • One application of the present invention is a situation in which a simultaneous extraction of PGM is sought out with an increase in the chromium to iron ratio of the reacted chromite.
  • the economic value of the PGM is combined to the value of a chromite showing a high chromium to iron ratio.
  • the carbochlorination conditions used in this example produces a high increase in the chromium to iron ratio of the reacted chromite.
  • the Cr to iron ratio of the chromite was determined at 1.9 after the carbochlorination step, the chromium to iron ratio reached 16.9, see Table 3 for major elements analysis.
  • Tables 1 to 3 demonstrate that the process, according to specific embodiments is able to recover substantially all the PGM from a chromite ore.
  • the PGM are only present in the residue and the gas phase (Os only) streams.
  • the process can be run concurrently with a large removal of FeCl3.
  • the removal of FeCl3 produces an increase in the chromium to iron ratio of the chromite used as a feed to the process.
  • Example 1 The conditions used and steps followed in this experiment differed from those disclosed in Example 1 only in that the reactor and the temperature was raised to 660° C. in the presence of N 2 instead of 720° C.; and in that once the reaction temperature was reached, 20 ml/min of Cl 2 , and 20 ml/min of CO were flown through the reactor instead of the 200 ml/min. Contrary to Example 1, only the formation of a very small quantity of FeCl 3 was noted during the length of the experiment.
  • the distribution of the PGM in the residue and the gas phase are presented in Table 1 for the sample noted PGM-2.
  • the sums of the PGM for the residue and the gas phases are: Pd 1102 ppb, Pt 328 ppb, Ir 21 ppb, Os 47 ppb, Rh 84 ppb and Ru 85 ppb.
  • the PGM concentrations obtained from the nickel sulphide fire-assay, reported in Table 1, can be used as the 100% recovery mark.
  • the sums of PGM values in the residue and the gas phases were recalculated as per cent recovery in Table 2.
  • the experimental error is in the order of ⁇ 15%.
  • Example 2 The conditions used and steps followed in this experiment differed from those disclosed in Example 2 only in that water was used instead of HCl for 1) quenching the gas phase escaping the condenser; 2) for adding (100 ml) to the residue after the cooling period in the chlorination reactor.
  • the water used as a trap for the PGM contained in the gas phase was analysed directly for the PGM.; and 3) for washing the solid condensate from the condenser area.
  • the distribution of the PGM in the residue and the gas phases are presented in Table 1 for the sample noted PGM-3.
  • Table 1 the sums of the PGM for the residue and the gas phases were: Pd 652 ppb, Pt 153 ppb, Ir 25 ppb, Os 7.3 ppb, Rh 69 ppb and Ru 45 ppb.
  • the PGM concentrations obtained from the nickel sulphide fire-assay, reported at the Table 1, can be used as the 100% recovery mark.
  • the sums of PGM values in the residue and the gas phases were recalculated as per cent recovery in table 2. It is to note that the analytical error is in the order of ⁇ 15%.

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WO2014091456A1 (fr) * 2012-12-14 2014-06-19 Fer-Min-Ore (Proprietary) Limited Procédé pour la récupération de métaux du groupe du platine
CN104302793A (zh) * 2012-05-09 2015-01-21 Inter-Euro科技有限公司 金回收
CN113278803A (zh) * 2021-05-11 2021-08-20 贵研资源（易门）有限公司 一种处理贵金属铁捕集料的方法
US11473168B2 (en) 2016-10-30 2022-10-18 Yeda Research And Development Co. Ltd. Method for platinum group metals recovery from spent catalysts
US11718893B2 (en) 2017-11-01 2023-08-08 Yeda Research And Development Co. Ltd. Method for gold recovery and extraction from electronic waste or gold containing minerals, ores and sands
US11898220B2 (en) * 2014-06-19 2024-02-13 Yeda Research And Development Co. Ltd. Apparatus for platinum group metals recovery from spent catalysts

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CA2552292C (fr) * 2006-07-12 2008-12-09 Reprotech Limited Purification de metaux du groupe du platine a partir de melanges de ces metaux
DE102007020142A1 (de) * 2007-04-26 2008-10-30 Bayer Materialscience Ag Verfahren zur Rückgewinnung von Ruthenium aus einem rutheniumhaltigen geträgerten Katalysatormaterial
AU2012231686B2 (en) 2011-03-18 2015-08-27 Orbite Aluminae Inc. Processes for recovering rare earth elements from aluminum-bearing materials
EP3141621A1 (fr) 2011-05-04 2017-03-15 Orbite Aluminae Inc. Procédés de récupération de terres rares dans divers minerais
EP2755918A4 (fr) 2011-09-16 2015-07-01 Orbite Aluminae Inc Procédés de préparation d'alumine et de divers autres produits
US9023301B2 (en) 2012-01-10 2015-05-05 Orbite Aluminae Inc. Processes for treating red mud
CA2891427C (fr) 2012-11-14 2016-09-20 Orbite Aluminae Inc. Procede de purification d'ions aluminium
KR101323754B1 (ko) * 2013-04-29 2013-10-31 한국지질자원연구원 폐촉매의 침출용액으로부터 산 및 백금족 금속의 회수방법
CN104630500A (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红土镍矿中回收镍、钴、铁和硅的方法
WO2020188527A1 (fr) * 2019-03-21 2020-09-24 Anglo American Services (Uk) Ltd Récupération de pgm et de chromite à partir de minerais pgm/cr mixtes
CA3192359A1 (fr) * 2020-08-18 2022-02-24 Enviro Metals, LLC Affinage de metaux
WO2024022582A1 (fr) * 2022-07-26 2024-02-01 Kronos International, Inc. Récupération de chlore à partir de chlorure d'hydrogène généré dans des procédés de carbochloration

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104302793A (zh) * 2012-05-09 2015-01-21 Inter-Euro科技有限公司 金回收
WO2014091456A1 (fr) * 2012-12-14 2014-06-19 Fer-Min-Ore (Proprietary) Limited Procédé pour la récupération de métaux du groupe du platine
US11898220B2 (en) * 2014-06-19 2024-02-13 Yeda Research And Development Co. Ltd. Apparatus for platinum group metals recovery from spent catalysts
US11473168B2 (en) 2016-10-30 2022-10-18 Yeda Research And Development Co. Ltd. Method for platinum group metals recovery from spent catalysts
US11718893B2 (en) 2017-11-01 2023-08-08 Yeda Research And Development Co. Ltd. Method for gold recovery and extraction from electronic waste or gold containing minerals, ores and sands
CN113278803A (zh) * 2021-05-11 2021-08-20 贵研资源（易门）有限公司 一种处理贵金属铁捕集料的方法

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US20100257978A1 (en) 2010-10-14
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