WO2011148040A1 - Method for processing spodumene - Google Patents

Method for processing spodumene Download PDF

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Publication number
WO2011148040A1
WO2011148040A1 PCT/FI2011/050440 FI2011050440W WO2011148040A1 WO 2011148040 A1 WO2011148040 A1 WO 2011148040A1 FI 2011050440 W FI2011050440 W FI 2011050440W WO 2011148040 A1 WO2011148040 A1 WO 2011148040A1
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WO
WIPO (PCT)
Prior art keywords
fluidized bed
gas
bed reactor
spodumene
fed
Prior art date
Application number
PCT/FI2011/050440
Other languages
French (fr)
Inventor
Maija-Leena Metsärinta
Original Assignee
Outotec Oyj
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 Outotec Oyj filed Critical Outotec Oyj
Priority to BR112012029597A priority Critical patent/BR112012029597A2/en
Priority to EP11786184.9A priority patent/EP2576446A4/en
Priority to US13/643,502 priority patent/US9068240B2/en
Priority to CN201180025128.8A priority patent/CN102906022B/en
Priority to EA201291185A priority patent/EA201291185A1/en
Priority to AU2011257091A priority patent/AU2011257091B2/en
Priority to CA2796473A priority patent/CA2796473C/en
Publication of WO2011148040A1 publication Critical patent/WO2011148040A1/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/103—Cooling recirculating particles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/10001—Use of special materials for the fluidized bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07006—Control of the oxygen supply
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to a method for thermally processing a-spodumene, or lithium aluminum silicate, by which treatment it is rendered in a form more advantageous for further processing, i.e. soluble ⁇ -spodumene.
  • Lithium is typically used for instance in the batteries of videos, cameras and mobile phones. Natural lithium-containing minerals are mainly spodumene, petalite and lepidolite. In salt lakes, the hypolimnion may also contain lithium, but there the decisive factor with respect to industrial production is the lithium-magnesium ratio. Likewise, also sea water contains lithium. Lithium is produced by heating and further leaching for example ores or concentrates, such as spodumene, i.e.
  • lithium aluminum silicate LiAISi 2 O 6
  • petalite LiAISi 4 O 0
  • the a structure of spodumene is transformed into a soluble ⁇ structure. This can be carried out by thermal heating. It has been found out that the alpha structure is converted into a beta structure when the temperature is 850-1000° C.
  • the treatment of the concentrate generally includes transformation of the crystal structure at a high temperature, pressure leaching, carbon dioxide treatment, as well as filtering and cleaning of the created lithium bicarbonate LiHCO 3 . From the Canadian publication CA 1297265, there is known a process for producing lithium carbonate.
  • the material is thermally treated in a circulating fluidized bed reactor, which requires a high free-space velocity for the gas in the reactor.
  • the concentrate or ore is fed into the process as coarse material, with a grain size of 1 -10 millimeters approximately.
  • a large gas flow is required.
  • the heating of a large gas flow in turn demands a large quantity of energy.
  • oxygenous gas In order to maintain the temperature on the level required by the conversion throughout the whole process, oxygenous gas must be added on different levels. For keeping the gas temperature on a sufficiently high level, a large number of lances is needed for fuel supply.
  • the high energy demand and large quantity of fuel increase C0 2 emissions.
  • the object of the invention is to introduce a new, more efficient, more environmentally friendly and energy-efficient way for treating spodumene, particularly for processing it thermally in a fluidized bed reactor, so that a desired structure is obtained for spodumene with respect to further processing.
  • the invention relates to a method for thermally processing a-spodumene, i.e. lithium aluminum silicate, by which treatment it is transformed into ⁇ - spodumene, which is more advantageous for further processing; according to said method, concentrate or ore with a grain size of 20-1 ,000 ⁇ is processed in a fluidized bed reactor, at a temperature of 800-1 ,000 Q C, by using an oxygenous gas as the fluidizing gas. According to the invention, heat transfer to the nuclei of the particles to be processed takes place more rapidly in a fine-grained material than in a coarser material, in other words the delay caused by the heating of spodumene in the reactor is shorter with a finer material, i.e. when the concentrate grain size is advantageously 20- 1 ,000 ⁇ .
  • a-spodumene i.e. lithium aluminum silicate
  • oxygenous fluidizing gas is fed into the fluidized bed reactor, depending on the grain size of the feed, so that the free-space velocity of gas is 0.3-1 m/s.
  • the oxygen content of the oxygenous fluidizing gas to be fed in the fluidized bed reactor equals the oxygen quantity required by the oxidation of the fuel needed for heating the fluidized bed.
  • the fluidized bed is a bubbling bed.
  • heat transfer in the suspension bed is effective.
  • the energy consumption in the process is minimized in many different ways.
  • the energy from the hot exhaust gas is used for drying and preheating the feed, which reduces the quantity of fuel needed in the reactor.
  • the energy content of the hot product removed from the fluidized bed reactor is used for preheating the process gas, which reduces the quantity of fuel needed in the reactor.
  • the delay of spodumene in the fluidized bed is no more than one hour, preferably 15 minutes to 1 hour.
  • the energy contained in the hot gas discharged from the fluidized bed reactor is utilized in the drying and preheating of the material to be fed in the fluidized bed reactor.
  • at least part of the dust conveyed along with the gas discharged from the fluidized bed reactor, which dust is recovered by a cyclone and a fiber filter, is returned to the bubbling fluidized bed.
  • liquid, gaseous or solid fuel is fed to the bubbling fluidized bed by lances.
  • the energy contained in the hot product discharged from the fluidized bed reactor is utilized in the preheating of the combustion/fluidizing air to be fed in the fluidized bed reactor, in the fluidized bed cooler of the product.
  • Dust is recovered from the hot, oxygenous gas discharged from the fluidized bed cooler prior to feeding the gas to the fluidized bed reactor.
  • the dust obtained from the fluidized bed cooler is combined in the product.
  • the temperature of the fluidized bed is chosen according to the impurity contents of the spodumene and the fuel, by avoiding an excessive formation, i.e. over 15%, of molten phases in the bed.
  • Figure 1 illustrates the invention as a block diagram.
  • spodumene concentrate or ore i.e. lithium aluminum silicate
  • the filtered lithium concentrate (moisture in concentrates being generally -10 %) is conducted in the process line in countercurrent to the hot process gas to be removed from the fluidized bed reactor. Now the hot gas is in direct contact with the concentrate.
  • the concentrate is dried and heated while the gas is cooled, i.e. the concentrate is dried and preheated prior to being thermally processed in the fluidized bed reactor, in a bubbling fluidized bed.
  • the lithium concentrate is subjected to conversion, i.e. the a-spodumene is, owing to the effect of heat, converted to soluble ⁇ -spodumene.
  • This change takes place when the temperature is 800-1 ,000 °C, but yet so that the formation of molten phases formed by impurities is minimized by selecting the temperature.
  • the grain size of the lithium concentrate fed in the fluidized bed reactor is 20-1000 ⁇ .
  • the delay of the material in the fluidized bed is preferably less than 1 hour, when the free-space velocity of the gas is 0.3-1 m/s.
  • the fuel fed therein reacts with the oxygenous fluidizing/process gas.
  • the process gas in a fluidized bed reactor is composed of gas and air that was used for cooling the fluidized bed reactor product and preheated in the process.
  • the fuel When burning, the fuel must generate sufficient energy for heating both the spodumene and the gas in the fluidized bed reactor.
  • Dust is recovered in a cyclone from the gas exhausted from the fluidized bed reactor. The energy content of dust-free gas is utilized for drying and preheating the concentrate.
  • the thermal capacity of the product treated in the fluidized bed reactor is made use of in a fluidized bed cooler, where the energy contained in the product is transferred in the gas, and the cooled product is removed.
  • Air is fed as fluidizing gas into the multiblock fluidized bed cooler, and the hot spodumene product removed from the fluidized bed reactor is also fed in said cooler. Fluidizing air is heated as the spodumene is cooled. The hot oxygenous gas exhausted from the fluidized bed cooler is conducted to the process reactor as fluidizing and combustion gas. The products must be cooled in order to improve the wear of the conveyors and to make the processing easier.
  • the invention is discussed with reference to the energy balance in the conversion process of a-spodumene taking place in a fluidized bed reactor.
  • Spodumene concentrate is fed to be processed in a fluidized bed reactor.
  • energy is needed for raising the temperature.
  • the temperature is raised to 950 Q C, in which case the methane demand is 55 Nm 3 per ton of spodumene concentrate.
  • For burning the methane there is needed 1 10 NM 3 oxygen, which equals 524Nm 3 when calculated as air.
  • the size of the furnace is defined according to the feed quantity and spodumene grain size, so that the bed forms a bubbling bed (free-space velocity according to grain size 0.3-1 m/s), and there is sufficiently oxygen for oxidizing the fuel needed in the heating of spodumene.
  • the quantity of released energy s 156 kWh, which is made use of in the drying and preheating processes.
  • the quantity of released energy is 300 kWh, which is made use of in the preheating of the process gas.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • General Engineering & Computer Science (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Combustion & Propulsion (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Silicates, Zeolites, And Molecular Sieves (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Silicon Compounds (AREA)
  • Drying Of Solid Materials (AREA)

Abstract

The invention relates to a method for thermally processing α-spodumene, i.e. lithium aluminum silicate, by which treatment it is transformed into β-spodumene, which is more advantageous for further processing; in the method, concentrate or ore with a grain size of 20-1,000 μm is processed in a fluidized bed reactor, at a temperature of 800-1,000 °C, by using an oxygenous gas as the fluidizing gas.

Description

Method for processing spodumene
FIELD OF INVENTION The invention relates to a method for thermally processing a-spodumene, or lithium aluminum silicate, by which treatment it is rendered in a form more advantageous for further processing, i.e. soluble β-spodumene.
BACKGROUND OF INVENTION
The largest lithium users at present are glass and ceramic industry as well as battery industry, the share of which is constantly growing, because lithium batteries have a significant role in the development of electric automobiles, for example. Part of the lithium is used as lithium carbonate, or it is at least a commercial intermediate product. Lithium is typically used for instance in the batteries of videos, cameras and mobile phones. Natural lithium-containing minerals are mainly spodumene, petalite and lepidolite. In salt lakes, the hypolimnion may also contain lithium, but there the decisive factor with respect to industrial production is the lithium-magnesium ratio. Likewise, also sea water contains lithium. Lithium is produced by heating and further leaching for example ores or concentrates, such as spodumene, i.e. lithium aluminum silicate (LiAISi2O6) or petalite (LiAISi4O 0)- In the first recovery step of lithium, the a structure of spodumene is transformed into a soluble β structure. This can be carried out by thermal heating. It has been found out that the alpha structure is converted into a beta structure when the temperature is 850-1000° C. To summarize: in lithium recovery, lithium mineral is concentrated, whereafter the treatment of the concentrate generally includes transformation of the crystal structure at a high temperature, pressure leaching, carbon dioxide treatment, as well as filtering and cleaning of the created lithium bicarbonate LiHCO3. From the Canadian publication CA 1297265, there is known a process for producing lithium carbonate. According to said publication, the material is thermally treated in a circulating fluidized bed reactor, which requires a high free-space velocity for the gas in the reactor. The concentrate or ore is fed into the process as coarse material, with a grain size of 1 -10 millimeters approximately. In order to make said material circulate in a way characteristic for a circulating fluidized bed, a large gas flow is required. The heating of a large gas flow in turn demands a large quantity of energy. In order to maintain the temperature on the level required by the conversion throughout the whole process, oxygenous gas must be added on different levels. For keeping the gas temperature on a sufficiently high level, a large number of lances is needed for fuel supply. In addition, the high energy demand and large quantity of fuel increase C02 emissions. OBJECT OF INVENTION
The object of the invention is to introduce a new, more efficient, more environmentally friendly and energy-efficient way for treating spodumene, particularly for processing it thermally in a fluidized bed reactor, so that a desired structure is obtained for spodumene with respect to further processing.
SUMMARY OF INVENTION The essential novel features of the invention are apparent from the appended claims.
The invention relates to a method for thermally processing a-spodumene, i.e. lithium aluminum silicate, by which treatment it is transformed into β- spodumene, which is more advantageous for further processing; according to said method, concentrate or ore with a grain size of 20-1 ,000 μιτι is processed in a fluidized bed reactor, at a temperature of 800-1 ,000 QC, by using an oxygenous gas as the fluidizing gas. According to the invention, heat transfer to the nuclei of the particles to be processed takes place more rapidly in a fine-grained material than in a coarser material, in other words the delay caused by the heating of spodumene in the reactor is shorter with a finer material, i.e. when the concentrate grain size is advantageously 20- 1 ,000 μιτι.
According to an embodiment of the invention, oxygenous fluidizing gas is fed into the fluidized bed reactor, depending on the grain size of the feed, so that the free-space velocity of gas is 0.3-1 m/s.
The oxygen content of the oxygenous fluidizing gas to be fed in the fluidized bed reactor equals the oxygen quantity required by the oxidation of the fuel needed for heating the fluidized bed.
According to an embodiment of the invention, the fluidized bed is a bubbling bed. When operating according to the method of the invention, heat transfer in the suspension bed is effective. The energy consumption in the process is minimized in many different ways. When using a bubbling bed, where the gas velocity and at the same time the gas flow is small, the heated gas flow is not too large. According to the invention, the energy from the hot exhaust gas is used for drying and preheating the feed, which reduces the quantity of fuel needed in the reactor. The energy content of the hot product removed from the fluidized bed reactor is used for preheating the process gas, which reduces the quantity of fuel needed in the reactor.
According to an embodiment of the invention, the delay of spodumene in the fluidized bed is no more than one hour, preferably 15 minutes to 1 hour.
The energy contained in the hot gas discharged from the fluidized bed reactor is utilized in the drying and preheating of the material to be fed in the fluidized bed reactor. According to the invention, at least part of the dust conveyed along with the gas discharged from the fluidized bed reactor, which dust is recovered by a cyclone and a fiber filter, is returned to the bubbling fluidized bed. According to the invention, liquid, gaseous or solid fuel is fed to the bubbling fluidized bed by lances.
According to a preferred embodiment of the invention, the energy contained in the hot product discharged from the fluidized bed reactor is utilized in the preheating of the combustion/fluidizing air to be fed in the fluidized bed reactor, in the fluidized bed cooler of the product.
Dust is recovered from the hot, oxygenous gas discharged from the fluidized bed cooler prior to feeding the gas to the fluidized bed reactor. The dust obtained from the fluidized bed cooler is combined in the product. According to the invention, the temperature of the fluidized bed is chosen according to the impurity contents of the spodumene and the fuel, by avoiding an excessive formation, i.e. over 15%, of molten phases in the bed.
While using a bubbling fluidized bed according to the invention, where the employed feed is fine-grained concentrate or ore, and by making use of the energy flows contained in the hot exhaust gas and the hot product, there is advantageously achieved, with relatively low energy consumption, an effective thermal conversion of spodumene. LIST OF DRAWINGS
An arrangement according to the invention is described in more detail with reference to the appended drawing, where
Figure 1 illustrates the invention as a block diagram.
DETAILED DESCRIPTION OF INVENTION According to the invention, spodumene concentrate or ore, i.e. lithium aluminum silicate, is processed thermally in a fluidized bed reactor in order to convert it to a desired soluble form for separating lithium. The filtered lithium concentrate (moisture in concentrates being generally -10 %) is conducted in the process line in countercurrent to the hot process gas to be removed from the fluidized bed reactor. Now the hot gas is in direct contact with the concentrate. The concentrate is dried and heated while the gas is cooled, i.e. the concentrate is dried and preheated prior to being thermally processed in the fluidized bed reactor, in a bubbling fluidized bed.
In the bubbling bed of the fluidized bed reactor, the lithium concentrate is subjected to conversion, i.e. the a-spodumene is, owing to the effect of heat, converted to soluble β-spodumene. This change takes place when the temperature is 800-1 ,000 °C, but yet so that the formation of molten phases formed by impurities is minimized by selecting the temperature. According to the invention, the grain size of the lithium concentrate fed in the fluidized bed reactor is 20-1000 μιτι. The delay of the material in the fluidized bed is preferably less than 1 hour, when the free-space velocity of the gas is 0.3-1 m/s. In the fluidized bed, the fuel fed therein (can be gaseous, liquid or solid) reacts with the oxygenous fluidizing/process gas. The process gas in a fluidized bed reactor is composed of gas and air that was used for cooling the fluidized bed reactor product and preheated in the process. When burning, the fuel must generate sufficient energy for heating both the spodumene and the gas in the fluidized bed reactor. Dust is recovered in a cyclone from the gas exhausted from the fluidized bed reactor. The energy content of dust-free gas is utilized for drying and preheating the concentrate. The thermal capacity of the product treated in the fluidized bed reactor is made use of in a fluidized bed cooler, where the energy contained in the product is transferred in the gas, and the cooled product is removed. Air is fed as fluidizing gas into the multiblock fluidized bed cooler, and the hot spodumene product removed from the fluidized bed reactor is also fed in said cooler. Fluidizing air is heated as the spodumene is cooled. The hot oxygenous gas exhausted from the fluidized bed cooler is conducted to the process reactor as fluidizing and combustion gas. The products must be cooled in order to improve the wear of the conveyors and to make the processing easier.
EXAMPLE
In the example below, the invention is discussed with reference to the energy balance in the conversion process of a-spodumene taking place in a fluidized bed reactor. Spodumene concentrate is fed to be processed in a fluidized bed reactor. In order to facilitate the desired conversion from a-spodumene to β-spodumene, energy is needed for raising the temperature. The temperature is raised to 950 QC, in which case the methane demand is 55 Nm3 per ton of spodumene concentrate. For burning the methane, there is needed 1 10 NM3 oxygen, which equals 524Nm3 when calculated as air. In that case the size of the furnace is defined according to the feed quantity and spodumene grain size, so that the bed forms a bubbling bed (free-space velocity according to grain size 0.3-1 m/s), and there is sufficiently oxygen for oxidizing the fuel needed in the heating of spodumene. When, according to the example, 524 Nm3 air is cooled from 950 °C to 200 °C, the quantity of released energy s 156 kWh, which is made use of in the drying and preheating processes. As one ton of spodumene exhausted from the fluidized bed reactor at the temperature of 950 °C is cooled down to 70 °C, the quantity of released energy is 300 kWh, which is made use of in the preheating of the process gas.
For a person skilled in the art, it is obvious that along with the development of technology, the principal idea of the invention can be realized in many different ways. Thus the invention and its embodiments are not restricted to the above described examples, but they may vary within the scope of the appended claims.

Claims

A method for thermally processing a-spodumene, i.e. lithium aluminum silicate, by which treatment it is transformed into β- spodumene, which is more advantageous for further processing ; characterized in that concentrate or ore with a grain size of 20-1 ,000 μιτι is processed in a fluidized bed reactor, at a temperature of 800- 1 ,000 QC, by using an oxygenous gas as the fluidizing gas, when the temperature of the fluidized bed is chosen according to the impurity contents of the spodumene and the fuel, by avoiding an excessive formation, i.e. over 15%, of molten phases in the fluidized bed.
A method according to claim 1 , characterized in that oxygenous fluidizing gas is fed into the fluidized bed reactor, depending on the grain size of the feed, so that the free-space velocity of gas is 0.3-1 m/s.
A method according to claim 1 or 2, characterized in that the oxygen content of the oxygenous fluidizing gas to be fed in the fluidized bed reactor equals the oxygen quantity required by the oxidation of the fuel needed for heating the fluidized bed.
A method according to claim 1 , 2 or 3, characterized in that the fluidized bed is a bubbling bed.
A method according to any of the claims λ -Α, characterized in that the delay of spodumene in the fluidized bed is no more than one hour, preferably from 1 5 minutes to 1 hour.
A method according to claim 1 , characterized in that the energy contained in the hot gas discharged from the fluidized bed reactor is utilized in the drying and preheating of the material to be fed in the fluidized bed reactor.
7. A method according to claim 1 , characterized in that at least part of the dust that is recovered by a cyclone and a fiber filter from gas exhausted from the fluidized bed reactor is returned to the bubbling fluidized bed.
8. A method according to claim 4, characterized in that liquid, gaseous or solid fuel is fed to the bubbling fluidized bed by lances.
9. A method according to claim 1 , characterized in that the thermal energy contained in the hot product discharged from the fluidized bed reactor is made use of in the fluidized bed cooler of the product, in preheating the combustion/fluidizing air to be fed in the fluidized bed reactor.
10. A method according to claim 9, characterized in that dust is recovered from the hot, oxygenous gas discharged from the fluidized bed cooler prior to feeding the gas to the fluidized bed reactor.
1 1 . A method according to claim 9 or 10, characterized in that the dust obtained from the fluidized bed cooler is combined in the product.
PCT/FI2011/050440 2010-05-25 2011-05-12 Method for processing spodumene WO2011148040A1 (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
BR112012029597A BR112012029597A2 (en) 2010-05-25 2011-05-12 spodumene processing method
EP11786184.9A EP2576446A4 (en) 2010-05-25 2011-05-12 Method for processing spodumene
US13/643,502 US9068240B2 (en) 2010-05-25 2011-05-12 Method for processing spodumene
CN201180025128.8A CN102906022B (en) 2010-05-25 2011-05-12 The working method of triphane
EA201291185A EA201291185A1 (en) 2010-05-25 2011-05-12 METHOD TREATMENT SPIDEN
AU2011257091A AU2011257091B2 (en) 2010-05-25 2011-05-12 Method for processing spodumene
CA2796473A CA2796473C (en) 2010-05-25 2011-05-12 A method for transforming lithium aluminum silicate in .alpha.-spodumene form into .beta.-spodumene form by thermal processing

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10544512B2 (en) 2014-02-24 2020-01-28 Nemaska Lithium Inc. Methods for treating lithium-containing materials
US10597305B2 (en) 2015-08-27 2020-03-24 Nemaska Lithium Inc. Methods for treating lithium-containing materials
US10633748B2 (en) 2012-04-23 2020-04-28 Nemaska Lithium Inc. Processes for preparing lithium hydroxide
US10800663B2 (en) 2012-05-30 2020-10-13 Nemaska Lithium Inc. Processes for preparing lithium carbonate
WO2020206567A1 (en) * 2019-04-12 2020-10-15 Universidad De Concepcion Process for obtaining lithium carbonate from spodumene ore by sulphation with ferrous sulphate at high temperature
US11078583B2 (en) 2013-03-15 2021-08-03 Nemaska Lithium Inc. Processes for preparing lithium hydroxide
US11083978B2 (en) 2016-08-26 2021-08-10 Nemaska Lithium Inc. Processes for treating aqueous compositions comprising lithium sulfate and sulfuric acid
US11142466B2 (en) 2017-11-22 2021-10-12 Nemaska Lithium Inc. Processes for preparing hydroxides and oxides of various metals and derivatives thereof
WO2022032327A1 (en) * 2020-08-12 2022-02-17 Calix Ltd A method for the pyroprocessing of powders
US11697861B2 (en) 2013-10-23 2023-07-11 Nemaska Lithium Inc. Processes for preparing lithium carbonate
US12006231B2 (en) 2022-12-28 2024-06-11 Nemaska Lithium Inc. Processes for preparing hydroxides and oxides of various metals and derivatives thereof

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI126509B (en) * 2015-04-02 2017-01-13 Keliber Oy A process for preparing beta-spodumen from a raw material containing alpha-spodumen
CN106906359B (en) 2015-12-22 2018-12-11 理查德.亨威克 Lithium is collected from silicate mineral
RU2663021C1 (en) * 2017-07-17 2018-08-01 Акционерное общество "Ведущий научно-исследовательский институт химической технологии" Method of lithuania extraction from sphodumene
CN107628627A (en) * 2017-10-16 2018-01-26 福州大学 A kind of method of natural spodumene circulation roasting crystal formation conversion
KR102412474B1 (en) * 2019-12-20 2022-06-22 주식회사 포스코 Heat treatment method of spodumene

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2972517A (en) * 1958-03-24 1961-02-21 Dept Of Mines Method of producing lithium sulphate from alpha and beta spodumene
US3017243A (en) * 1958-08-11 1962-01-16 Dept Of Mines Method of producing lithium carbonate from spodumene
DE3622105A1 (en) * 1986-07-02 1988-01-07 Metallgesellschaft Ag Process for winning lithium carbonate
CN101224900A (en) * 2007-10-11 2008-07-23 钟辉 Novel method for spodumene calcining transformation

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2975217A (en) * 1958-06-10 1961-03-14 Goodyear Tire & Rubber Catalytic alkylation of phenol

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2972517A (en) * 1958-03-24 1961-02-21 Dept Of Mines Method of producing lithium sulphate from alpha and beta spodumene
US3017243A (en) * 1958-08-11 1962-01-16 Dept Of Mines Method of producing lithium carbonate from spodumene
DE3622105A1 (en) * 1986-07-02 1988-01-07 Metallgesellschaft Ag Process for winning lithium carbonate
CN101224900A (en) * 2007-10-11 2008-07-23 钟辉 Novel method for spodumene calcining transformation

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP2576446A4 *

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10633748B2 (en) 2012-04-23 2020-04-28 Nemaska Lithium Inc. Processes for preparing lithium hydroxide
US10800663B2 (en) 2012-05-30 2020-10-13 Nemaska Lithium Inc. Processes for preparing lithium carbonate
US11634336B2 (en) 2012-05-30 2023-04-25 Nemaska Lithium Inc. Processes for preparing lithium carbonate
US11254582B2 (en) 2012-05-30 2022-02-22 Nemaska Lithium Inc. Processes for preparing lithium carbonate
US11078583B2 (en) 2013-03-15 2021-08-03 Nemaska Lithium Inc. Processes for preparing lithium hydroxide
US11697861B2 (en) 2013-10-23 2023-07-11 Nemaska Lithium Inc. Processes for preparing lithium carbonate
US11519081B2 (en) 2014-02-24 2022-12-06 Nemaska Lithium Inc. Methods for treating lithium-containing materials
US11085121B2 (en) 2014-02-24 2021-08-10 Nemaska Lithium Inc. Methods for treating lithium-containing materials
US10544512B2 (en) 2014-02-24 2020-01-28 Nemaska Lithium Inc. Methods for treating lithium-containing materials
US10597305B2 (en) 2015-08-27 2020-03-24 Nemaska Lithium Inc. Methods for treating lithium-containing materials
US11083978B2 (en) 2016-08-26 2021-08-10 Nemaska Lithium Inc. Processes for treating aqueous compositions comprising lithium sulfate and sulfuric acid
US11542175B2 (en) 2017-11-22 2023-01-03 Nemaska Lithium Inc. Processes for preparing hydroxides and oxides of various metals and derivatives thereof
US11142466B2 (en) 2017-11-22 2021-10-12 Nemaska Lithium Inc. Processes for preparing hydroxides and oxides of various metals and derivatives thereof
WO2020206567A1 (en) * 2019-04-12 2020-10-15 Universidad De Concepcion Process for obtaining lithium carbonate from spodumene ore by sulphation with ferrous sulphate at high temperature
WO2022032327A1 (en) * 2020-08-12 2022-02-17 Calix Ltd A method for the pyroprocessing of powders
US12006231B2 (en) 2022-12-28 2024-06-11 Nemaska Lithium Inc. Processes for preparing hydroxides and oxides of various metals and derivatives thereof

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CL2012003278A1 (en) 2013-03-22
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EA201291185A1 (en) 2013-05-30
CA2796473C (en) 2017-03-28
US9068240B2 (en) 2015-06-30
CN102906022B (en) 2015-11-25
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EP2576446A4 (en) 2016-12-14
FI122831B (en) 2012-07-31
CA2796473A1 (en) 2011-12-01
FI20100215A (en) 2011-11-26
AU2011257091B2 (en) 2014-04-03
AU2011257091A1 (en) 2012-11-08
CN102906022A (en) 2013-01-30

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