EP0508542B1 - Procédé pour le traitement d'un minerai ayant des métaux recouvrables comprenant des composants contenant de l'arsenic - Google Patents

Procédé pour le traitement d'un minerai ayant des métaux recouvrables comprenant des composants contenant de l'arsenic Download PDF

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Publication number
EP0508542B1
EP0508542B1 EP92200989A EP92200989A EP0508542B1 EP 0508542 B1 EP0508542 B1 EP 0508542B1 EP 92200989 A EP92200989 A EP 92200989A EP 92200989 A EP92200989 A EP 92200989A EP 0508542 B1 EP0508542 B1 EP 0508542B1
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Prior art keywords
reactor
arsenic
ore
oxygen
roasting
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EP92200989A
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German (de)
English (en)
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EP0508542A3 (en
EP0508542A2 (fr
Inventor
Anthony L. Hannaford
Marc K. Le Vier
Rene R. Fernandez
Gopalan Ramadorai
Arno Dr. Fitting
Gurudas Dr. Samant
Bodo Peinemann
Gebhard Bandel
Hans Kofalck
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GEA Group AG
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Metallgesellschaft AG
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Priority claimed from US07/684,649 external-priority patent/US5123956A/en
Priority claimed from DE19914122894 external-priority patent/DE4122894C1/de
Priority claimed from DE19914122895 external-priority patent/DE4122895C1/de
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Publication of EP0508542A2 publication Critical patent/EP0508542A2/fr
Publication of EP0508542A3 publication Critical patent/EP0508542A3/de
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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
    • 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
    • C22B1/10—Roasting processes in fluidised form

Definitions

  • This invention relates to a process for treating ore particles containing gold and having arsenic-, carbon- and sulfur-containing components.
  • the ore particles include refractory ores, ore concentrates and ore tailings.
  • precious metals such as gold occur naturally in ores in different forms.
  • precious metal ores also frequently contain other materials which interfere with the recovery of these precious metal values, rendering these ores refractory to precious metal recovery.
  • the precious metal content may be at a relatively low level. This low level content compounds the effect of the refractory nature of these ores.
  • Many patents show attempts to deal with refractory components in precious metals recovery addressed to solving the arsenic contamination problems encountered when roasting precious metal and other metal ores having arsenic as an unwanted component present in the ore.
  • US-A-4 919 715 relates to the use of pure oxygen in roasting of refractory gold-bearing ores at temperatures between about 537°C and about 648°C.
  • This patent fails to address the problem of arsenic volatilization, is silent on the arsenic content in the ore, and does not address in that context the optimizing of gold recovery from refractory sulfidic, carbonaceous ores or separation of cyanide-consuming components before recovery of gold from the ore.
  • the disclosed method requires two fluid beds and stagewise roasting in these beds and the use of substantially pure oxygen (substantially pure oxygen being defined as at least about 80 % by weight).
  • any arsenic which is present is an undesired accompanying element and must be removed from the calcine and from the roaster gas. This is typically accomplished according to prior art by a so-called dearsenication roasting.
  • the arsenic content of the material is volatilized in a roasting zone having a low oxygen content and enters the gaseous effluent as arsenic vapor or arsenic oxide vapor and arsenic sulfide vapor.
  • arsenic and arsenic sulfides are oxidized to form arsenic oxide vapors under a relatively high oxygen partial pressure.
  • the dustlike solids contained in the roaster gas are removed at a temperature exceeding the sublimation temperature of the arsenic oxides, which are subsequently separated at lower gas temperatures, or the solids and the arsenic oxides are jointly removed at lower gas temperatures.
  • the first case contaminated arsenic oxides will be formed.
  • the arsenic which has been removed will be recycled in the process scheme.
  • the inventive process has the aim of roasting ores or refractory ores, ore concentrates or ore tailings of the type described herein for recovery of gold in an oxygen-enriched gaseous environment in order to minimize or eliminate arsenic volatilization, facilitate arsenic conversion to an insoluble, environmentally acceptable form immobilized in a waste product while reducing the effects of carbon- and sulfur-containing components on gold recovery.
  • This problem is solved by the process defined in claim 1.
  • the solubility of the stable arsenates formed in the process is so low that these may be dumped without special precautionary measures.
  • the water vapor content of the exhaust gas leaving the roasting reactor will result in a formation of stable arsenates having a particularly low solubility, e. g. such as scorodite or scorodite-like compounds.
  • free oxide indicates that said substance is not present as compound with arsenic or sulfur but in a form free of these. If calcium and magnesium as carbonates are available in a free form in the ore in a sufficient amount, it will be unnecessary to add said substances.
  • iron compounds are present, even in a large excess, an addition will always be required, i. e. if below a ratio of 3.5 to 4.0 moles iron to a mole of arsenic, because a major part of the iron will always be included in compounds with arsenic or sulfur.
  • the additives in the roasting reactor may consist of waste products, such as red mud from the alumina industry, filter salts and waste gypsum. Sulfates are particularly suitable. As seen from the data herein, iron compounds are preferred.
  • the use of an additive is preferable because the additive, in particle form will then be present close to the ore particles and will be able to combine immediately with arsenic which may have been vaporized from the ore particles at the higher temperatures discussed herein.
  • stable arsenates designates those arsenates which have only a low solubility in rainwater when stored in a waste dump of an exhausted calcine.
  • Water required for the water vapor may be fed to the roasting reactor by a suitable addition of steam, as moisture or water in the ore, of crystallization in the additives or as a water of crystallization in a component in the ore.
  • the exhaust gas may be processed for a production of sulfuric acid or may be scrubbed to remove the SO 2 or the SO 2 content may be liquified.
  • the ore is roasted in the reactor in the form of fluidized solids, and more preferably, the ore circulates as fluidized solids in a circulating fluidized bed or in an ebullating fluidized bed (which has a circulation feature to it).
  • a stationary fluidized bed having a defined upper surface may also be used.
  • a rotary kiln or a multiple-hearth furnace may be employed, provided the proper reactions may be obtained.
  • the advantage afforded by the process in accordance with this invention resides in that the calcine which is produced has a very good leachability, with e. g. cyanide, resulting in a high yield of gold and in a low consumption of cyanide.
  • the arsenic is bound in the form of stable arsenates, which do not disturb the leaching and which have an extremely low solubility in rainwater such that these calcines may be dumped without a need for special precautionary measures or further treatment.
  • the ores or concentrates may contain even up to 2 % of arsenic and more.
  • the temperature at which an undesirable molten phase is formed during roasting depends on the composition of the ore.
  • the percentages for the gases are stated in percent by volume.
  • the gas which is fed into the roasting reactor is adjusted to have a higher oxygen content.
  • the reaction temperature is achieved by a feeding of hot gases and/or by an addition of fuel. If fuel is added, oxygen in the amount required for the combustion of fuel must be added. If a reaction temperature is low, the required heat is introduced by feeding of suitable hot gases and/or by a sufficient preheating of the charged materials.
  • Roasting with two stage oxygen injection may be carried out particulary conveniently.
  • the roasting in the lower portion of a circulating fluid bed reactor is carried out as the first stage.
  • a fluidized gas contains an oxygen-containing atmosphere having an oxygen content below about 1 % by volume.
  • the second oxygen injection during this roasting stage is carried out in the upper portion of the reactor with a supply of secondary gas and optionally even with a supply of tertiary gas having yet more oxygen injected in that phase at a corresponding higher oxygen content.
  • the candidate ores may have the following levels of arsenic, carbon and sulfur components on a percent by weight basis: Arsenic up to 1.0 % or higher Carbon 2.5 % Maximum Sulfur 5.0 % Maximum (All percentages are on a weight-to-weight basis unless otherwise stated.)
  • a typical chemical analysis of the ore shows an average composition as follows: Arsenic 0.2 Percent Sulfur (Total) 4.0 Percent Carbon (Total) 1.0 Percent Iron 3.5 Percent Zinc 0.08 Percent Strontium 0.03 Percent Gold 4.3 g/t
  • gold recovery by using the process of the present invention yields from about 75 percent to about 90 percent (and even higher) gold recovery.
  • the roasting treatment is preceded by a first roasting stage, in which the roasting is effected at temperatures which are between 450°C and 900°C, preferably below 575°C, and below the temperature at which a molten phase is formed of an ore material and in an oxygen-containing atmosphere having an oxygen content below 1 % by volume.
  • a first roasting stage in which the roasting is effected at temperatures which are between 450°C and 900°C, preferably below 575°C, and below the temperature at which a molten phase is formed of an ore material and in an oxygen-containing atmosphere having an oxygen content below 1 % by volume.
  • Such roasting assures vaporization and an immediate reaction of the arsenic with the additive.
  • the additives and the water vapor need not be present in the first roasting stage but are preferably added already in the first roasting stage.
  • the water vapor content of the gas in the roasting reactor ranges from about 0.5 % to 10 % by weight.
  • Arsenates having a particularly low solubility such as scorodites will be formed if the water vapor content is in that range.
  • the roasting is effected at temperatures of 500°C to 750°C.
  • the formation of a molten phase may reliably be avoided, and the heat consumption may be low, the arsenic will effectively be bound and immobilized and the calcine will have a good leachability.
  • the substances are added in a particle size below 1 mm into the roasting reactor. That particle size will result in an effective contact and binding of arsenic present in the ore material. According to a preferred feature 80 % of these substances are added in a particle size of 10 to 50 ⁇ m.
  • the ore is comminuted, or ground, before roasting.
  • the ground ore is roasted in an oxygen-enriched gaseous atmosphere wherein the carbon and sulfur content is substantially completely oxidized from an initial roaster feed to a final calcine content as follows (% are percentages by weight):
  • greater than about 95 % of the arsenic is fixed in the calcine by the presence of a e.g. proper amount of iron. If desired, additional iron may be added to facilitate this conversion to an insoluble form.
  • ferricarsenate compounds formed during roasting render the arsenic in a fixed form in the calcine. Further, the ferricarsenate compound is insoluble in the subsequent leaching and from the tailings in dump storage after the gold values are extracted.
  • arsenic values not volatilized by the process of the present invention by retaining them in the calcine in a non-volatile form, but also these arsenic values can be retained in a form which is insoluble to the leaching and insoluble over a long period while in a dump.
  • reaction temperatures in the reactor apparatus must be sufficiently high to optimize the oxidation reaction, particularly the oxidation of carbon- and sulfur-containing components and formation of e.g. ferricarsenate compounds. It has been found that a reaction temperature in the reaction apparatus for the oxygen-enriched gaseous atmosphere of from about 475°C to about 600°C is desirable, while a preferred temperature range is from about 500°C to about 575°C.
  • the gaseous atmosphere in which the gold ore is roasted is an oxygen-enriched gaseous atmosphere, such as oxygen-enriched air, having a total initial oxygen content, after enrichment, of less than about 65 percent (by volume), and desirably from about 25 percent (by volume) to about 60 percent (by volume); industrially a range of oxygen of 35 % to 55 % by volume is indicated for the process.
  • oxygen-enriched gaseous atmosphere such as oxygen-enriched air
  • the ground ore is roasted preferably as fluidized solids in the oxygen-enriched gaseous environment.
  • the ore concentrates will have sufficient oxidizable content that there will be an autothermal oxidation reaction during roasting.
  • additional oxidizable content is provided by adding a comburant so that there will be a thermal reaction during roasting.
  • a low ignition point fuel is added, e. g. coal or butane/propane.
  • the ignition point should be that of propane or below.
  • an ebullating bed may be used with the overflow from the ebullating bed being constantly circulated.
  • the reaction velocity may be lower in an ebullating fluid bed.
  • Efficiency and control over the oxidation and reaction conditions are improved by circulating the ore as fluidized solids.
  • An advantage of a circulating fluid bed or an ebullating fluid bed is the precise control of the bed temperature.
  • the roasting is performed in a circulating fluidized bed.
  • the fluidized bed system consists of a fluidized bed reactor, a recycling cyclone and a recycling line.
  • the suspension discharged from the fluidized bed reactor is fed to the recycling cyclone(s) of the circulating fluidized bed and substantially all solids are removed from the suspension in said cyclone(s).
  • the solids which have been removed are returned to the fluidized bed reactor in such a manner that the solids circulated in the circulating fluidized bed systems amount to at least four times the weight of solids contained in the fluidized bed reactor.
  • the residence time of the ore in the oxygen-enriched gaseous atmosphere should be from about 8 to 12 minutes or more, but constrained by practical design considerations such as vessel size; pump size etc. It should be understood that residence time is a function of ore mineralogy. Control of residence time at temperature also controls silicate melting which is to be avoided. High porosity and low sintering is desirable for the subsequent leaching of gold.
  • the precious metal values are recovered from the thus-roasted ore, or calcine, by leaching.
  • leaching techniques are known in the art and are described in general in U.S. patents 4 902 345 and 4 923 510.
  • the roasted gold ore may be subjected to an oxygen or chlorine treatment after roasting and prior to leaching.
  • This treatment may be in the form of bubbling gaseous oxygen or chlorine through a suspension or a slurry of the thus-roasted ore either in a bath at ambient pressure or in a closed vessel at ambient or elevated pressure prior to leaching the ore.
  • FIG. 1 an embodiment showing a schematic industrial application of the process is illustrated.
  • a circulating fluid bed (CFB) reactor (100) is fed from an ore preheat stage with stream (200) and the ore is roasted in the reactor.
  • a start-up gas stream such as butane/propane has been shown entering the CFB reactor (100) at the bottom thereof through line (8).
  • a combined stream of oxygen-containing off-gas and fresh oxygen via preheater (102) is introduced into the CFB reactor (100).
  • the combined stream is identified as (201).
  • a preheated, oxygen-supplemented air stream (208) is introduced in the CFB reactor (100) and is coming from the post-finishing calcine treatment which will be discussed below.
  • a single cyclone (103) has been shown in Fig. 1, but more than one may be operated in parallel or in series to assure greater particulate removal from the off-gas.
  • Cyclone (103) bottoms i.e. underflow collections are partially reintroduced into the CFB reactor (100) via seal pot (104).
  • a slip stream (105) of calcined product is also taken from seal pot (104) and introduced into four preheaters (recuperators) (107) to (110) which are in a heat recovery unit (106). Air augmented with oxygen is brought up to about 450°C in heat recovery unit (106).
  • the unit (106) consists of four preheaters in the form of fluidized beds (107), (108), (109) and (110), respectively.
  • the CFB reactor (100) is operated at 550°C.
  • the resulting calcine (of retention time of 10 minutes in reactor (100)) is introduced into the first preheater (107).
  • the calcine is at a temperature of about 525°C and has a residence time of about 15 minutes in preheater (107); in the second preheater (108), the calcine temperature is about 475°C and residence time is about 10 minutes; in the third preheater (109) the calcine temperature is at about 420°C and the residence time is about 8 minutes; in the fourth preheater (110) the calcine temperature is about 350°C and the residence time is about 8 minutes. Air and oxygen enter these preheaters in parallel, fluidize in each the calcine and are cleaned in cyclone (112). After separation of particulates in cyclone (112), air and oxygen is introduced as stream (208) into the CFB reactor (100).
  • a second preheater unit (not shown) of the same type may be operated in parallel to the first preheater unit (106).
  • the seal pot (104) or a second seal pot (not shown) may feed the second preheater unit.
  • these are referred to two parallel cyclones such as (112), and two parallel seal pots such as (104).
  • Heated air and oxygen from all four preheaters is used and is at about 450°C as shown in Table 1.
  • ambient air is introduced via pump (113) into heating coils (114) immersed in the fluidized calcine in preheaters (109) and (110).
  • This air is used to preheat in a CFB type vessel (not shown) the ore introduced as stream (200) in the CFB reactor (100).
  • Hot air exits heating coils (114) at 200°C.
  • the balance of the energy requirement for roasting is made up by the addition of butane or pulverized coal to the CFB reactor (100).
  • Calcine in stream (209) is quenched in water in tank (115) to a 15 % solids content and further worked-up for subsequent leaching.
  • Off-gases i.e. cyclone (103) overflows are introduced through line (202) into a waste heat boiler (116) where the off-gas temperature is reduced to about 375°C, dust from the waste heat boiler (116) is introduced into the preheater unit in an appropriate place, e.g. preheater (108) and combined with calcine.
  • the off-gases are introduced via line (203) into an electrostatic precipitator (117), e.g. a five field, hot electrostatic precipitator, to remove substantially all residual dust in the off-gas.
  • the exit temperature of the off-gas from the electrostatic precipitator is at about 350°C and the off-gas comprises about 36 % by volume of oxygen.
  • Table 1 shows process data for a circulating fluid bed roasting plant shown in Fig. 1 with 160 t/h of ore, preheated to 200°C, being fed through line (200) into reactor (100), 4.1 t/h of said ore being water of crystallization in ore components. About 330 kg/h of coal calculated as carbon is added as fuel into reactor (100). The calcine withdrawn through line (209) in an amount of 154 t/h has a temperature of 350°C. Stream No.
  • the ore came from a random sampling of arsenic-, sulfidic-, organic carbon-containing, gold-bearing ores from the region around Carlin, Nevada. This ore, for the series of runs showed an average gold content of about 4.5 g/t of gold, an average content of 0.08 percent arsenic, 2.49 percent sulfide sulfur (2.81 percent total sulfur) and 0.79 percent organic carbon (0.84 percent total carbon).
  • the ore had the following mineralogical and chemical analysis: Quartz 68 Percent Kaolinite 10 Percent Sericite or Illites 8 Percent Pyrite 5 Percent Jarosite 4 Percent Alunite 3 Percent Fe x O y 1 Percent Barite 1 Percent Carbonates 0 Percent
  • a chemical analysis of the ore shows an average composition as follows: Arsenic 824 partas per million Carbon (Total) 0.84 Percent Sulfur (Total) 2.81 Percent Gold 4.5 g/t Iron 4.0 Percent Zinc 400 parts per million Strontium 0.02 Percent
  • the ore was ground in a small ball mill and it had a moisture content of about 1 percent by weight.
  • the ground ore was placed in a simple rotating tube reactor and roasted in a batch operation to evaluate various reaction conditions using a residence time of two hours for the sake of consistency.
  • the roasted ore, or calcine was leached by a carbon in leach cyanidation using a dosage of 2.5 kg of sodium cyanide per ton of roasted ore and 30 grams per liter of activated carbon.
  • the leaching was conducted in a continuously rolling bottle under the following conditions: 200 grams of calcine per leach test, 40 % solids and 24 hours leaching time.
  • Fig. 2 -A- is the regime for arsenate formation
  • -B- is the regime for stable arsenate
  • Fig. 3 -C- is the regime of arsenate volatilization in Fe 2 O 3 range
  • -D- is the regime of stable arsenates.
  • the first circulating fluidized bed system consists of the fluidized bed reactor (401), the recycling cyclone (402), and the recycling line (403).
  • the fluidized bed reactor (401) was 0.2 m in diameter and had a height of 6 m.
  • gold ore concentrate at a rate of 15 kg/h was charged through line (404) into the reactor.
  • the concentrate contained 2.1 % arsenic, 15 % sulfide sulfur and 45 g gold per 1000 kg.
  • the particle size was below 0.2 mm with a medium size (d 50 ) of 70 ⁇ m.
  • Air at a rate of 11 m 3 n/h was fed through line (405) into the heat exchanger (406) and was preheated therein to 600°C and then fed through line (407) into the reactor (401) as a fluidizing gas.
  • the reactor (401) was fed through line (408) with secondary air at a rate of 9 m 3 n/h and through line (409) at a rate of 3 m 3 n/h with tertiary air, which served to combust the residual sulfur in the reactor (401).
  • the oxygen potential was adjusted to be in the range in which arsenate is volatilized in the Fe 2 O 3 range, see -C- in Fig. 3, above the range in which iron arsenate is formed.
  • the temperature in the reactor was between 700°C and 750°C.
  • the calcine withdrawn through line (410) contained 0.02 % arsenic and 0.1 % sulfur.
  • the leaching of the calcine resulted in a recovery of gold with a yield of 96 %.
  • the solubility of arsenic during the leaching of gold was very low and amounted only to less than 2 mg/l.
  • a gas-solid suspension was fed from the reactor (401) through line (411) into the recycling cyclone (402).
  • the exhaust gas conducted in line (412) was dedusted in two cyclones (not shown) and in a candle filter (413) at about 600°C.
  • the collected dusts were returned to the reactor (401) through line (414).
  • the dust-free exhaust gas contained SO 2 and As 2 O 3 and was fed through line (415) to the fluidized bed reactor (416) of a second circulating fluidized bed system.
  • the reactor (416) was 0.16 m in diameter and had a height of 4 m. It was heated by indirect electric heating. Hematitic iron ore having a particle size below 0.5 mm, with a medium size of 30 ⁇ m, was charged through line (417) at a rate of 0.3 kg/h. Fluidizing air at a rate of 15 m 3 n/h was fed into the reactor (416).
  • the suspension leaving through line (419) was adjusted to contain 6 % oxygen and 4 % water vapor so that the conditions for a formation of stable arsenates (Fig. 2) were established.
  • a water vapor content of 4 % the moisture content of the iron ore charged through (417) was controlled in dependence or the water vapor content of the gas entering through line (415) and of the fluidizing air entering through line (418).
  • the solids collected in the recycling cyclone (420) were returned through the recycling line (421) into the reactor (416).
  • the arsenic-free roaster gas contained 9.1 % SO 2 and was fed through line 22 to a gas purifier and subsequently to a plant for producing sulfuric acid.
  • the solid material which was discharged through line (423) from the reactor (416) contained 17.3 % arsenic. Leaching tests with water showed that the solubility of arsenic was less then 1 mg/l.
  • the dust-containing gases which contain arsenic vapor and arsenic compound vapor are produced by roasting e.g. of sulfide materials which contain iron and arsenic.
  • sulfide materials which contain iron and arsenic.
  • Such materials are roasted in the Fe 2 O 3 range at temperatures of 500°C to 1100°C in a first stage, which is supplied with oxygen-containing gases.
  • arsenic is volatilized mainly as arsenic oxides and part of the sulfur content is volatilized as elementary sulfur. Solids are removed from the exhaust gas at temperatures above the condensation temperature of the volatilized components, and the solids are discharged as calcine.

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Claims (6)

  1. Procédé de traitement de particules de minerai contenant de l'or et ayant des constituants contenant de l'arsenic, du carbone et du soufre qui comprend les étapes qui consistent à :
    griller les particules de minerai dans un réacteur de grillage en présence d'au moins une substance choisie dans le groupe constitué d'un oxyde libre, d'un carbonate, d'un sulfate, d'un hydroxyde et d'un chlorure, de calcium, de magnésium, de fer ou de baryum, et du pyrite, à des températures dans le réacteur comprises entre 475°C et 900°C en présence de vapeur d'eau jusqu'à 10% en poids de minerai, sans formation d'une phase de fusion à la surface des particules de minerai, la substance étant présente dans le réacteur en une quantité hyperstoechiométrique pour réagir avec l'arsenic dans les particules de minerai pour former des arsenates stables,
    envoyer du gaz dans le réacteur ayant une teneur initiale en oxygène de 25% à 65% en volume, et
    maintenir une atmosphère contenant de l'oxygène à au moins 1% en volume d'oxygène, en référence à une quantité basique d'oxygène dans l'air, dans le réacteur,
    récupérer les particules de minerai ainsi grillées sous la forme de minerai grillé contenant de l'arsenate, le minerai grillé pouvant être soumis à une récupération d'or par lessivage, et
    éliminer du réacteur de grillage un gaz d'échappement contenant des arsenates stables et au moins 1% en volume d'oxygène.
  2. Procédé suivant la revendication 1, dans lequel on traite les particules de minerai dans le réacteur dans un lit fluidisé.
  3. Procédé suivant la revendication 2, dans lequel le lit fluidisé est un lit fluidisé circulant.
  4. Procédé suivant la revendication 1, dans lequel les températures dans le réacteur sont comprises entre 475°C et 600°C.
  5. Procédé suivant la revendication 1, dans lequel on maintient dans le réacteur un rapport fer à arsenic qui est suffisant pour former un ferricarsenate, mais pas inférieur à 3,5 moles de fer pour 1 mole d'arsenic.
  6. Procédé suivant la revendication 5, dans lequel le ferricarsenate formé est constitué de composés scorodites ou analogues à du scorodite.
EP92200989A 1991-04-12 1992-04-07 Procédé pour le traitement d'un minerai ayant des métaux recouvrables comprenant des composants contenant de l'arsenic Expired - Lifetime EP0508542B1 (fr)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US684649 1984-12-21
US07/684,649 US5123956A (en) 1991-04-12 1991-04-12 Process for treating ore having recoverable gold values and including arsenic-, carbon- and sulfur-containing components by roasting in an oxygen-enriched gaseous atmosphere
DE19914122894 DE4122894C1 (fr) 1991-07-11 1991-07-11
DE4122895 1991-07-11
DE4122894 1991-07-11
DE19914122895 DE4122895C1 (fr) 1991-07-11 1991-07-11

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EP0508542A2 EP0508542A2 (fr) 1992-10-14
EP0508542A3 EP0508542A3 (en) 1993-10-20
EP0508542B1 true EP0508542B1 (fr) 1998-06-24

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EP (1) EP0508542B1 (fr)
AU (1) AU656952B2 (fr)
BR (1) BR9201355A (fr)
CA (1) CA2065837C (fr)
DE (1) DE69225993T2 (fr)
ES (1) ES2117028T3 (fr)
MY (1) MY110328A (fr)
RU (1) RU2079562C1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5425799A (en) * 1993-04-30 1995-06-20 Metallgesellschaft Aktiengesellschaft Process for roasting refractory gold ores
US6248301B1 (en) * 1991-04-12 2001-06-19 Newmont Mining Corporation And Newmont Gold Company Process for treating ore having recoverable metal values including arsenic containing components
WO2001066811A1 (fr) * 2000-03-10 2001-09-13 Lakefield Research Limited Procedes de reduction de la consommation de cyanure lors de l'extraction de minerais de metaux precieux contenant du soufre
US6482373B1 (en) 1991-04-12 2002-11-19 Newmont Usa Limited Process for treating ore having recoverable metal values including arsenic containing components
CN108884514A (zh) * 2016-03-24 2018-11-23 奥图泰(芬兰)公司 用于含硫矿石热处理的方法和设备

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DE4329417C1 (de) * 1993-09-01 1994-08-18 Metallgesellschaft Ag Verfahren zum Rösten refraktärer Golderze
DE19546538A1 (de) * 1995-12-13 1997-06-19 Metallgesellschaft Ag Verfahren zur thermischen Behandlung refraktärer Golderze
CN1047801C (zh) * 1997-01-15 1999-12-29 核工业北京化工冶金研究院 从难浸矿石中提取金的方法
RU2479650C1 (ru) * 2012-02-14 2013-04-20 Федеральное государственное автономное образовательное учреждение высшего профессионального образования "Уральский федеральный университет имени первого Президента России Б.Н. Ельцина" Способ извлечения благородных металлов из руд и концентратов
RU2553706C2 (ru) * 2012-03-12 2015-06-20 Товарищество с ограниченной ответственностью "Фирма "Балауса" Способ рудоподготовки полиметаллических руд для выщелачивания
RU2485189C1 (ru) * 2012-05-10 2013-06-20 Федеральное государственное автономное образовательное учреждение высшего профессионального образования "Национальный исследовательский технологический университет "МИСиС" Способ переработки окисленных золотомышьяковистых руд
GB2513154B (en) * 2013-04-17 2015-10-28 Tetronics International Ltd Precious Metal Recovery
WO2016048750A1 (fr) * 2014-09-24 2016-03-31 Ecolab Usa Inc. Procédé de récupération d'or à partir de minerai réfractaire
RU2604551C1 (ru) * 2015-05-29 2016-12-10 Федеральное государственное бюджетное учреждение науки Байкальский институт природопользования Сибирского отделения Российской академии наук (БИП СО РАН) Способ переработки золотосодержащих скородитовых руд
BR112018014777B1 (pt) * 2016-01-26 2022-07-26 Outotec (Finland) Oy Método e aparelho para tratar um resíduo de lixiviação de um concentrado metálico contendo enxofre
JP6744981B2 (ja) * 2016-07-14 2020-08-19 コリア インスティチュート オブ ジオサイエンス アンド ミネラル リソースズ 貴金属の濃縮回収方法
WO2018091361A1 (fr) * 2016-11-15 2018-05-24 Tcm Research Ltd. Procédés d'extraction à partir de minerais réfractaires
WO2020132752A1 (fr) * 2018-12-27 2020-07-02 Compañia Minera Pargo Minerals Spa Installation moderne de production de trioxydes d'antimoine, d'arsénic, ainsi que de plomb métalliques
WO2020132751A1 (fr) * 2018-12-27 2020-07-02 Compañia Minera Pargo Minerals Spa Procédé d'obtention de trioxyde d'antimoine (sb203), de trioxyde d'arsénic (as203) et de plomb (pb)
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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6248301B1 (en) * 1991-04-12 2001-06-19 Newmont Mining Corporation And Newmont Gold Company Process for treating ore having recoverable metal values including arsenic containing components
US6482373B1 (en) 1991-04-12 2002-11-19 Newmont Usa Limited Process for treating ore having recoverable metal values including arsenic containing components
US5425799A (en) * 1993-04-30 1995-06-20 Metallgesellschaft Aktiengesellschaft Process for roasting refractory gold ores
WO2001066811A1 (fr) * 2000-03-10 2001-09-13 Lakefield Research Limited Procedes de reduction de la consommation de cyanure lors de l'extraction de minerais de metaux precieux contenant du soufre
CN108884514A (zh) * 2016-03-24 2018-11-23 奥图泰(芬兰)公司 用于含硫矿石热处理的方法和设备

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ES2117028T3 (es) 1998-08-01
BR9201355A (pt) 1992-12-01
EP0508542A3 (en) 1993-10-20
EP0508542A2 (fr) 1992-10-14
RU2079562C1 (ru) 1997-05-20
AU656952B2 (en) 1995-02-23
DE69225993D1 (de) 1998-07-30
DE69225993T2 (de) 1998-12-10
CA2065837A1 (fr) 1992-10-13
AU1482492A (en) 1992-10-15
CA2065837C (fr) 2005-06-07
MY110328A (en) 1998-04-30

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