EP4540427A1 - Procédé et dispositif de traitement de résidus fins - Google Patents

Procédé et dispositif de traitement de résidus fins

Info

Publication number
EP4540427A1
EP4540427A1 EP22946688.3A EP22946688A EP4540427A1 EP 4540427 A1 EP4540427 A1 EP 4540427A1 EP 22946688 A EP22946688 A EP 22946688A EP 4540427 A1 EP4540427 A1 EP 4540427A1
Authority
EP
European Patent Office
Prior art keywords
roaster
underflow
cyclone
gas
overflow
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.)
Pending
Application number
EP22946688.3A
Other languages
German (de)
English (en)
Inventor
Jörg HAMMERSCHMIDT
Marcus Runkel
Roberto VALERY
Maciej WROBEL
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.)
Metso Metals Oy
Original Assignee
Metso Metals Oy
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 Metso Metals Oy filed Critical Metso Metals Oy
Publication of EP4540427A1 publication Critical patent/EP4540427A1/fr
Pending legal-status Critical Current

Links

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
    • C22B1/04—Blast 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B15/00—Other processes for the manufacture of iron from iron compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present disclosure relates to a method for handling fine tailings from mineral treatment processes .
  • the present disclosure further relates to an arrangement for handling fine tailings from mineral treatment processes .
  • flotation In the field of metallurgy, flotation can be used for separating minerals from gangue by taking advantage of differences in their hydrophobicity . Hydrophobicity differences between valuable minerals and waste gangue are increased through the use of surfactants and wetting agents . The selective separation of the minerals makes processing complex (that is , mixed) ores economically feasible .
  • the flotation process is used for the separation of a large range of sulfides , carbonates and oxides prior to further refinement .
  • tailings that comprise a mixture of materials such as chemicals , organics , and process water as wel l as metals and minerals in amounts that are too small to be efficiently and economically recovered using conventional methods .
  • the tailings materials are commonly viewed as waste and stored or piled .
  • a method for producing handling fine tailings from mineral treatment processes is disclosed .
  • the method may comprise :
  • the method of the present disclosure is characteri zed in that the underflow from the heat recovery boiler i s fed into the second roaster and the roasted material flow from the second roaster is fed into a cooler to form a cooler underflow in the form of calcine and a cooler overflow .
  • the arrangement may comprise :
  • a first roaster configured to roast the fine tailings from the mineral treatment process to form a first roaster off-gas comprising dust and a first roaster underflow and the roaster is configured to feed the first roaster off-gas comprising dust into a first cyclone and to feed the first roaster underflow into a second roaster
  • At least one cyclone configured to receive the first roaster off-gas comprising dust and separating it to form a cyclone overflow and a cyclone underflow and the cyclone is configured to feed the cyclone underflow into a second roaster and the cyclone overflow into a heat recovery boiler
  • a heat recovery boiler configured to receive the primary cyclone overflow and forming a heat recovery boiler overflow and heat recovery boiler underflow and feeding the heat recovery boiler underflow as into a second roaster, a second roaster configured to receive the first roaster underflow and cyclone underflow, and roasting them to form a roasted material flow and feeding it into a cooler, and a cooler configured to receive the roasted material flow and forming a cooler overflow and a cooler underflow in the form of calcine .
  • Figs . 1 to 3 present schematic representations of a method or arrangement for handl ing tai lings material from a mineral treatment process according to embodiments of the present disclosure .
  • Fig . 4 presents a schematic representation of a method for handling fine tailings from primary flotation treatment arranged to receive underflow from a mineral flotation line and separating them into cleaner underflow of recovered valuable material and cleaner overflow arranged to flow into the first roaster as infeed.
  • Fig. 5 presents a schematic representation of a method for handling fine tailings from primary flotation treatment arranged to receive underflow from a mineral flotation line and separating them into cleaner overflow of recovered valuable material and cleaner underflow arranged to flow into the first roaster as in- feed .
  • a method for handling fine tailings from mineral treatment processes is disclosed.
  • the method may comprise :
  • the first roaster may be a stationary fluidized bed roaster or a circulating fluidized bed roaster.
  • the second roaster may be a stationary fluidized bed roaster.
  • a stationary fluidized bed roaster may also be called a bubbling fluidized bed roaster, the terms are used synonymously in this description.
  • off-gas (17) from the second roaster (9) may be separated in a cyclone (19) to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) , see Fig. 1.
  • the cooler (23) used to cool the roasted material is a fluid bed cooler or a drum cooler.
  • cooler (23) is a fluid bed cooler
  • additional gas and/or air (35) is fed into the cooler together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) , see Fig. 2.
  • the cooler (23) is a drum cooler
  • no additional gas and/or air is fed into the cooler together with the roasted material flow (18) .
  • off-gas (17) from the second roaster (9) is fed into the cooler together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) , see Fig. 2.
  • off-gas (17) from the second roaster (9) may be separated in a cyclone (19) to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) .
  • the cooler (23) is a fluid bed cooler
  • additional gas and/or air (35) is fed into the cooler together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster ( 3 ) , see Fig . 3.
  • off-gas (17) from the second roaster (9) may be separated in a cyclone (19) to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) , see Fig. 3.
  • the tailings material from mineral treatment processes may comprise, e.g., cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, and/or sulfur.
  • the tailings material may comprise materials such as of I2O3, SiCy, FeS, FeS2-
  • the calcine leaving the cooler may be subjected to further treatments to increase the recovery of valuable materials.
  • the calcine is subjected to hydrometallurgical treatment such as leaching to extract valuable metals from it for further processing .
  • the calcine leaving the cooler may be fed into a direct reduction treatment to obtain reduced iron which may be further utili zed in steel production .
  • the calcine leaving the cooler may be fed into a smelting process to extract valuable metals or alloys .
  • roasting refers to the proces s of treating an ore or ore concentrate with very hot roasting gas .
  • the term “roasting gas” refers to the gas present in the roaster during the roasting .
  • “Roasting gas” may in certain embodiments be used synonymously with "fluidi zing gas” .
  • the roasting gas may be air or other gas mixtures comprising oxygen .
  • the roasting gas comprises recycled air or gas recycle from other parts of the method or arrangement .
  • an ore or ore concentrate comprising sulfur is heated to a high temperature in the presence of an oxygen-containing gas , thereby oxidi zing the sulfur .
  • roasting refers to decreasing the sulfur content in solid materials by oxidation of sulfur in the form of sulfides , mainly metal sulfides (e . g . FeS , FeS2 ) , into oxides such as sulfate or sulfite that may be recovered .
  • roasting gas ( 2 ) is fed into the first and/or second roaster .
  • roasting in a method according to the present disclosure occurs mainly in the roasters , it is obvious to a skilled person that the oxidation reactions of roasting may occur also in other stages or parts of the method .
  • the only pre-requisite for roasting to occur is that a sufficient portion of oxygen is present in the atmosphere and that the temperature is high enough for the oxidation to occur.
  • roasting will also happen e.g. in the cyclones before the material has cooled down sufficiently.
  • the recovery of valuable materials from tailings recovered from various processes such as metallurgical processes.
  • the recovery of sulfur (e.g. in the form of sulfuric acid) from pyrite material may be improved by roasting the tailings material while simultaneously lowering the amount of sulfur present in the calcine formed in the process.
  • tailings material or “fine tailings” refer to a concentrate of materials formed and recovered as tailings in metallurgical processes.
  • the tailings material comprises sulfur- containing materials also containing metals such as cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, or any combination thereof.
  • the tailings material may be overflow material from a flotation treatment.
  • tailings material (1) from the flotation has a d50 particle size of 250 pm or less, or 200 pm or less, or 150 pm or less, or 125 pm or less, or 100 pm or less, or 75 pm or less, or 50 pm or less, or 30 pm or less.
  • tailings material (1) from the flotation has a d50 particle size of 20 pm or more, or 25 pm or more, or 30 pm or more.
  • tailings material (1) from the flotation has a d50 particle size of 20 - 200 pm, or 20 - 150 pm, or 20 - 125 pm, or 20 - 100 pm, or
  • the tailings material may be classified as fine tailings.
  • very fine tailings material with a d50 particle size of 30 pm or less may be granulated prior to treatment with the method of the present disclosure.
  • the d50 particle size of the granulated material is approximately 50 - 250 pm.
  • the overflow material may comprise, e.g., cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, and/or sulfur. In certain embodiments, the overflow material may comprise copper, iron, gold, and/or sulfur.
  • At least one roasting is performed in an oxygen-enriched atmosphere.
  • Oxidizing roasting is performed in an atmosphere that comprises oxygen
  • general oxidizing roastings are performed in an atmosphere of air, i.e. in an atmosphere comprising approximately 21 % oxygen. If the roasting is performed in an oxygen-enriched atmosphere, the oxidationefficiency is improved.
  • oxygen-enriched atmosphere refers to an atmosphere that contains more oxygen than air, i.e. more than 21 % oxygen.
  • the oxygen-enriched atmosphere consist of a gas mixture comprising 22 % , or 24 % , or 26 % , or 28 % , or 30 % , or 40 % , or 45 % , or 50 % , or 55 % , or up to 60 % oxygen. In certain embodiments, the oxygen- enriched atmosphere consist of a gas mixture comprising
  • the first roaster off-gas comprising dust is separated to form a cyclone overflow and a cyclone underflow by passing it through at least two, at least three, at least four, or at least five consecutive cyclones configured to feed the cyclone offgas from one cyclone into the next cyclone and feeding the cyclone overflow from the final cyclone into the recovery boiler .
  • the first roaster offgas comprising dust is separated to form a cyclone overflow and a cyclone underflow by passing through two or more primary cyclones arranged parallel to each other .
  • the cyclone off-gas from the two or more primary cyclones are combined into one stream of off-gas that is fed into a following cyclone passing it through at least one , at least two , at least three , at least four, or at least five consecutive cyclones configured to feed the cyclone off-gas from one cyclone into the next cyclone and feeding the cyclone overflow from the final cyclone into the recovery boiler .
  • the first roaster offgas comprising dust is separated to form a cyclone overflow and a cyclone underflow by passing it through at least two , at least three , at least four, or at least five parallel arranged consecutively so in series of at least two , at least three , at least four, or at least five consecutive setups of parallel cyclones configured to feed the cyclone off-gas from one cyclone into the next cyclone and feeding the cyclone overf low from the final cyclone into the recovery boiler .
  • the first roaster offgas may be separated to form an overflow and an underflow using any suitable de-dusting device .
  • the underflow ( 27 ) from the at least one primary cyclone ( 6 ) may be fed back into the first roaster to increase the retention time of the calcine in the roaster as illustrated in Fig . 2 .
  • the first roaster off-gas comprising dust is separated in a separation process comprising using a multiclone .
  • a multiclone refers to a dust collector system comprising multiple smaller cyclones in one device to efficiently separate dust from a gas stream .
  • the off-gas formed in the one or more cyclones or multiclone is fed into a dedusting device .
  • a dedusting device By feeding the off-gas from the cyclones and/or multiclone into a de-dusting device , it is possible to recover dust contained in the off-gas .
  • the off-gas ( 28 ) formed in the one or more cyclones , multiclone , and/or de-dusting device is fed into the first roaster .
  • the off-gas from the cyclones , multiclone , cooler, sealing device , and/or de-dusting device into the first roaster, it is possible to recycle air within the process , thus reducing the requirement for clean air fed into the process as well as reducing the requirement for purification of air before being released into the atmosphere .
  • the sulfur-containing material contained in the heat recovery boiler overflow ( 12 ) is fed into a de-dusting device ( 13 ) to separate remaining dust ( 15 ) from the off-gas ( 14 ) .
  • the dust may be collected, granulated or pelleti zed ( 20 ) , and returned to the first roaster ( 26 ) .
  • the dust collected from the de-dusting device may be combined (25) with the calcine (22) .
  • the off-gas (14) from the de-dusting device is fed into a wet gas cleaning device (16) .
  • the wet gas cleaning device may be a wet scrubber.
  • the wet gas cleaning device may comprise several steps for cleaning said gas.
  • the sulfur-containing material contained in the heat recovery boiler overflow (12) is fed into a hot ESP (electrostatic precipitator) to separate remaining dust (15) from the off-gas (14) .
  • the dust may be collected, granulated or pelletized (20) , and returned to the first roaster (26) .
  • the dust collected from the hot ESP may be combined (25) with the calcine (22) .
  • sulfur is oxidized in the first and/or second roasting.
  • roasting the sulfur contained in the tailings material by oxidizing it it is possible to recover the sulfur and utilize it e.g. for the production of sulfuric acid.
  • the tailings material (1) comprises tailings formed in a primary flotation treatment (30) of underflow material (31) from a mineral flotation line.
  • a primary flotation treatment (30) of underflow material (31) from a mineral flotation line.
  • the valuable materials contained in the tailings material and recovered using the process of the present disclosure may be cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, and/or sulfur.
  • the primary flotation treatment arranged to receive underflow (31) from a mineral flotation line as slurry infeed, for the separation of slurry into cleaner underflow of recovered valuable material (33) and cleaner overflow (29) arranged to flow into the first roaster as infeed.
  • the recovered valuable material comprises cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, and/or sulfur. In one embodiment, the recovered valuable material comprises iron.
  • the primary flotation treatment arranged to receive underflow (31) from a mineral flotation line as slurry infeed, for the separation of slurry into cleaner overflow of recovered valuable material (33) and cleaner underflow (34) arranged to flow into the first roaster as infeed.
  • the recovered valuable material comprises cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, and/or sulfur which can be oxidized and used e.g. in the production of sulfuric acid.
  • the recovered valuable material comprises copper.
  • the amount of water in the tailings material is reduced using a thickener prior to roasting .
  • the amount of water in the tailings material is reduced by filtering prior to roasting .
  • the amount of water in the tailings material is reduced by filtering using a pressure filter prior to roasting .
  • the tailings material is roasted in a roasting according to the present disclosure ( 32 ) .
  • Reducing the amount of water included in the tailings material fed into the roaster will generally improve the energy efficiency as evaporation of water in the roaster consumes significant amounts of energy .
  • the method described in the current specification has the added util ity of improving the recovery of valuable materials from the tailings produced in various metallurgical processes .
  • the valuable materials recovered from the process may be metals such as cobalt , nickel , gold, platinum group metals ( ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, iron, and/or sulfur which can be oxidi zed and used e . g . in the production of sulfuric acid .
  • An additional added advantage of the method of the present disclosure is that it increases the amount of sul furic acid that may be recovered from the tailings material by reducing the content of sulfur in the calcine formed in the roasting proces s whi le at the same time producing a calcine with a lowered sulfur content .
  • the arrangement may comprise : - a first roaster (3) configured to roast tailings material (1) from a mineral treatment process to form a first roaster off-gas comprising dust (5) and a first roaster underflow (4) and the roaster in configured to feed the first roaster offgas comprising dust (5) into a first cyclone (6) and to feed the first roaster underflow (4) into a second roaster (9) ,
  • At least one primary cyclone (6) configured to receive the first roaster off-gas comprising dust (5) and separating it to form a cyclone overflow (7) and a cyclone underflow (8) and the cyclone is configured to feed the cyclone underflow (8) into a second roaster (9) and the cyclone overflow (7) into a heat recovery boiler (10) ,
  • a heat recovery boiler (10) configured to receive the primary cyclone overflow (7) and forming a heat recovery boiler overflow (12) and heat recovery boiler underflow (11) and feeding the heat recovery boiler underflow (11) into a second roaster (9) ,
  • a second roaster configured to receive the first roaster underflow (4) and cyclone underflow (8) , and roasting them to form a roasted material flow (18) and feeding it into a cooler (23) , and
  • a cooler configured to receive the roasted material flow (18) and forming a cooler underflow in the form of calcine (22) .
  • tailings material By roasting the tailings material and separating solids from the off-gas of the roasted materials it is possible to improve the recovery of valuable materials from tailings recovered from various processes such as metallurgical processes. Following collecting the valuable material or desired product from various processes, they leave a tailings fraction that will inevitably also contain some of the valuable material that would normally be discarded as waste.
  • the first roaster may be a stationary fluidized bed roaster or a circulating fluidized bed roaster.
  • the second roaster may be a stationary fluidized bed roaster .
  • roasting gas (2) is fed into the first and/or second roaster.
  • the underflow from the at least one primary cyclone can be arranged to be fed back (27) into the first roaster to increase the retention time of the calcine in the roaster.
  • off-gas (17) from the second roaster (9) may be separated in a cyclone (19) to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) .
  • At least one roaster is an oxidizing roaster.
  • all roasters are oxidizing roasters .
  • the cooler (23) used to cool the roasted material is a fluid bed cooler or a drum cooler.
  • cooler (23) when the cooler (23) is a fluid bed cooler, additional gas and/or air (35) is fed into the cooler (23) together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) , see Figs. 2 and 3.
  • off-gas (17) from the second roaster (9) is fed into the cooler together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) , see Fig. 3.
  • off-gas (17) from the second roaster (9) may be separated in a cyclone (19) to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) .
  • the cooler (23) is a fluid bed cooler
  • additional gas and/or air (35) is fed into the cooler (23) together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster ( 3 ) , see Fig . 3.
  • off-gas (17) from the second roaster (9) may be separated in a cyclone (19) to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster (3) .
  • the cooler (23) is a fluid bed cooler
  • additional gas and/or air (35) is fed into the cooler together with the roasted material flow (18) .
  • the cooler off-gas (24) may be fed into a cyclone (36) and separated to form dust (21) that is combined with the calcine (22) and secondary air (28) that may be fed into the upper part of the first roaster ( 3 ) , see Fig . 3.
  • roasting the tailings in oxidizing conditions enables recovery of sulfur contained in the tailings.
  • sulfur is oxidized to sulfate which may be recovered as sulfuric acid.
  • the second roaster is part of a fluid bed cooler or a drum cooler .
  • the off-gas from the second roaster may be separated in a cyclone to form dust that is combined with the calcine and secondary air that may be fed into the upper part of the first roaster .
  • the arrangement comprises at least two , at least three , at least four, or at least five primary cyclones arranged consecutively after each other .
  • the arrangement comprises at least two primary cyclones arranged parallel to each other .
  • the arrangement comprises a multiclone .
  • a “multiclone” refers to a dust collector system comprising multiple smaller cyclones in one device to efficiently separate dust from a gas stream .
  • the sulfur is oxidi zed in the first and/or second roasting .
  • the sulfur is oxidi zed in the first and/or second roasting .
  • the arrangement comprises a de-dusting device ( 13 ) arranged to receive the heat recovery boiler overflow ( 12 ) to separate remaining dust ( 15 ) in the recovery boiler overflow from the off-gas ( 14 ) .
  • the dust may be collected, granulated or pelleti zed, and returned to the first roaster .
  • the de-dusting device may be a hot ESP (electrostatic precipitator) .
  • the arrangement comprises a hot ESP (electrostatic precipitator) arranged to receive the recovery boiler overflow to separate remaining dust in the recovery boiler overflow from the off-gas.
  • the dust may be collected, granulated or pelletized (20) , and returned (26) to the first roaster. By pelletizing or granulating the sulfur-containing material in the cyclone overflow, the smaller particles can be returned to roasting enabling the recovery of more of the valuable material.
  • the dust collected from the de-dusting device may be combined (25) with the calcine (22) .
  • the off-gas (14) from the de-dusting device is fed into a wet gas cleaning device (16) .
  • the wet gas cleaning device may be a wet scrubber.
  • the wet gas cleaning device may comprise several steps for cleaning said gas.
  • the tailings material comprises tailings formed in a primary flotation treatment (30) of underflow material (31) from a mineral flotation line.
  • a primary flotation treatment (30) of underflow material (31) from a mineral flotation line.
  • the primary flotation treatment arranged to receive underflow (31) from a mineral flotation line as slurry infeed, for the separation of slurry into cleaner underflow of recovered valuable material (33) and cleaner overflow (29) arranged to flow into the first roaster as infeed (Fig.4) .
  • the recovered valuable material comprises iron.
  • the primary flotation treatment arranged to receive underflow (31) from a mineral flotation line as slurry infeed, for the separation of slurry into cleaner overflow of recovered valuable material (33) and cleaner underflow (34) arranged to flow into the first roaster as infeed (Fig.5) .
  • the tailings material is roasted in a roasting according to the present disclosure ( 32 ) .
  • the valuable materials contained in the tailings material and recovered using the process of the present disclosure may be cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, and/or iron which may be recovered following further treatment of the calcine, and/or sulfur.
  • the recovered valuable material comprises cobalt, nickel, gold, platinum group metals (ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, and/or iron which may be recovered following further treatment of the calcine, and/or sulfur.
  • the recovered valuable material comprises copper.
  • the mineral flotation line comprises at least three flotation units.
  • at least three flotation units it is possible to ensure that all valuable materials that can be recovered by flotation have been recovered prior to feeding the tailings into an arrangement according to the present disclosure . In essence , only the very last fines collected after several flotation treatments are collected and fed into an arrangement according to the present disclosure .
  • the arrangement described in the current specification has the added util ity of improving the recovery of valuable materials from the tailings produced in various metallurgical processes .
  • the valuable materials recovered from the process may be metals such as cobalt , nickel , gold, platinum group metals ( ruthenium, rhodium, palladium, osmium, iridium, and platinum) , copper, zinc, silver, and/or iron which may be recovered following further treatment of the calcine , and/or sulfur which can be oxidi zed and used e . g . in the production of sulfuric acid .
  • a flow of approximately 31 . 6 t/h of fine pyrite tailings from a mineral flotation line was fed into a roaster and roasted at approximately 850 ° C .
  • the roaster off-gas was fed into a cyclone to separate the dust contained in the off-gas into a cyclone underflow which was combined with the bed discharge from the first roaster and fed into the second roaster .
  • the cyclone overflow was fed into a heat recovery boiler and separated into a boiler overflow containing gas and fine dust that was fed into a hot ESP and a boiler underflow containing most of the solids that was fed into the second roaster .
  • the dust collected from the hot ESP was granulated and returned to the first roaster while the off-gas from the hot ESP was treated in wet gas cleaning .
  • the roasted material collected from the second roaster was fed into a fucid bed cooler from which the cooled calcine was collected .
  • a flow of approximately 31 . 6 t/h of fine pyrite tailings from a mineral flotation line was fed into a roaster and roasted at approximately 850 ° C .
  • the roasted material was fed into a heat recovery boiler from which the off-gas was fed into a hot ES P and the bed discharge into a fluid bed cooler .
  • the dust collected from the hot ESP was granulated and returned to the f irst roaster whi le the off-gas from the hot ESP was treated in wet gas cleaning .
  • the roasted material collected from fluid bed cooler was collected as a cooled calcine .
  • a method according to the present disclosure produced a calcine containing a lower amount of sul fur and consequently also produced more sulfuric acid .
  • the amount of sulfur contained in the calcine was lower, the relative content of valuable products , in this case iron, was higher .
  • the method according to the present disclosure also required less process water as the amount of calcine needed to be cooled was lower than in the comparative example .
  • the embodiments described hereinbefore may be used in any combination with each other . Several of the embodiments may be combined together to form a further embodiment .
  • a method or an arrangement , disclosed herein, may comprise at least one of the embodiments described hereinbefore . It will be understood that the benefits and advantages described above may relate to one embodiment or may relate to several embodiments. The embodiments are not limited to those that solve any or all of the stated problems or those that have any or all of the stated benefits and advantages. It will further be understood that reference to 'an' item refers to one or more of those items.
  • the term "comprising" is used in this specification to mean including the feature (s) or act(s) followed thereafter, without excluding the presence of one or more additional features or acts.

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  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
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Abstract

L'invention concerne également un procédé de manipulation de résidus fins (1) issus de processus de traitement de minéraux. L'invention concerne en outre un dispositif pour manipuler des résidus fins (1) issus de processus de traitement de minéraux.
EP22946688.3A 2022-06-17 2022-06-17 Procédé et dispositif de traitement de résidus fins Pending EP4540427A1 (fr)

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AU (1) AU2022464781A1 (fr)
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SE346703B (fr) 1969-01-09 1972-07-17 Boliden Ab
US3984229A (en) 1970-04-20 1976-10-05 Boliden Aktiebolag Method for producing coarse powder, hardened iron oxide material from finely divided raw material substantially consisting of hematite and/or magnetite
CA1217060A (fr) * 1982-11-11 1987-01-27 John R.H. Shaw Extractopm des elements metalliques
SE8303184L (sv) 1983-06-06 1984-12-07 Boliden Ab Forfarande for beredning av kopparsmeltmaterial och liknande ravaror innehallande hoga halter arsenik och/eller antimon
DE102008033558A1 (de) * 2008-07-11 2010-01-14 Outotec Oyj Verfahren und Anlage zur Herstellung von Calcine-Produkten
FI20145949A (fi) * 2014-10-29 2016-04-30 Outotec Finland Oy Menetelmä kullan talteenottamiseksi
FI127945B (en) * 2014-11-10 2019-05-31 Outotec Finland Oy Treatment of complex sulfide concentrate
MX2018008747A (es) 2016-01-26 2018-11-29 Outotec Finland Oy Metodo y aparato para tratar un residuo de lixiviacion de un concentrado de metal que contiene azufre.
EA038634B1 (ru) * 2017-03-07 2021-09-27 Оутотек (Финлэнд) Ой Способ и установка для обжига золотосодержащего сульфидного концентрата
CN111589563B (zh) * 2020-05-29 2021-07-27 东北大学 一种铁尾矿悬浮焙烧提铁的装置及方法

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SE2251350A1 (en) 2023-12-18
WO2023242465A1 (fr) 2023-12-21
SE546668C2 (en) 2025-01-14
CA3259803A1 (fr) 2023-12-21
AU2022464781A1 (en) 2025-01-09
PE20251097A1 (es) 2025-04-15

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