WO2019015519A1 - 处理稀土精矿的方法和系统 - Google Patents

处理稀土精矿的方法和系统 Download PDF

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Publication number
WO2019015519A1
WO2019015519A1 PCT/CN2018/095309 CN2018095309W WO2019015519A1 WO 2019015519 A1 WO2019015519 A1 WO 2019015519A1 CN 2018095309 W CN2018095309 W CN 2018095309W WO 2019015519 A1 WO2019015519 A1 WO 2019015519A1
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Prior art keywords
rare earth
fluorine
outlet
inlet
earth concentrate
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PCT/CN2018/095309
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English (en)
French (fr)
Inventor
唐建文
杜国山
羡鹏飞
邱爽
周文龙
覃波
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中国恩菲工程技术有限公司
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Application filed by 中国恩菲工程技术有限公司 filed Critical 中国恩菲工程技术有限公司
Priority to RU2019136415A priority Critical patent/RU2746867C1/ru
Priority to KR1020197033564A priority patent/KR102364012B1/ko
Priority to AU2018303510A priority patent/AU2018303510B2/en
Priority to JP2020517260A priority patent/JP6941229B2/ja
Priority to BR112019025160-0A priority patent/BR112019025160B1/pt
Publication of WO2019015519A1 publication Critical patent/WO2019015519A1/zh
Priority to ZA2019/07015A priority patent/ZA201907015B/en
Priority to US16/663,964 priority patent/US11773467B2/en

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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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • 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
    • C22B59/00—Obtaining rare earth metals
    • 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
    • C22B1/06—Sulfating 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/02—Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
    • 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
    • C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
    • C22B60/02—Obtaining thorium, uranium, or other actinides
    • C22B60/0291—Obtaining thorium, uranium, or other actinides obtaining thorium
    • 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 is in the field of rare earth production, and in particular, the present disclosure relates to methods and systems for processing rare earth concentrates.
  • Baotou mixed ore [mixed ore of fluorocarbon strontium rare earth and monazite (phosphorite/phosphorite)] and bastnasite are important components of rare earth ore in China.
  • the current industrial method for treating such ore is mainly concentrated sulfuric acid roasting. The process is continuous and easy to control, and is easy to be mass-produced.
  • the strontium in the ore enters the slag in the form of strontium pyrophosphate, which causes radioactive pollution and also causes waste of strontium resources. And the recycling of fluorine and sulfur waste gas is difficult.
  • the current industrial acid hydrolysis method is mainly oxidative roasting-hydrochloric acid.
  • This method is characterized by small investment, but there are problems such as discontinuous process, difficulty in recycling strontium and fluorine in slag and wastewater, and pollution to the environment. It can be seen that the treatment of mixed ore and bastnasite in high temperature conditions is likely to cause waste of waste resources and environmental pollution of exhaust gas.
  • the present disclosure aims to solve at least one of the technical problems in the related art to some extent. To this end, it is an object of the present disclosure to provide a method and system for processing rare earth concentrates.
  • the method can treat fluorocarbon lanthanum rare earth or mixed mineral containing fluorocarbon lanthanum rare earth or monazite, has low energy consumption, can realize continuous production, can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrate.
  • the REO decomposition rate can reach 96%.
  • the present disclosure provides a method of treating a rare earth concentrate, according to an embodiment of the present disclosure, the method comprising:
  • the leaching slurry is subjected to solid-liquid separation treatment to obtain a filtrate and leaching slag, and the leaching slag is returned to the step (2) for the acid hydrolysis treatment.
  • the method for treating system concentrate according to an embodiment of the present disclosure can achieve rapid forced mixing of concentrated sulfuric acid and rare earth concentrate by arranging a stirrer in the mixing device, so that the rare earth concentrate and the concentrated sulfuric acid are sufficiently wetted, thereby avoiding the subsequent acid
  • the agglomeration phenomenon occurs during the solution process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is kept constant.
  • the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening the rare earth essence.
  • the time of the acid hydrolysis reaction, and during the acid hydrolysis process the viscosity of the internal material changes greatly, from the fluid state to the semi-dry state, and finally becomes dry, and the clinker is obtained.
  • the acid hydrolysis device can effectively cope with the above material properties. The change.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO. Therefore, the method has wide adaptability of raw materials, low energy consumption, and can realize continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the decomposition rate of REO can reach 96%.
  • the method of processing rare earth concentrate according to the above embodiment of the present disclosure may further have the following additional technical features:
  • the method before the mixing the rare earth concentrate with the concentrated sulfuric acid, the method further comprises: (5) ball milling the rare earth concentrate to obtain rare earth concentrate particles; (6) The rare earth concentrate particles are subjected to a sieving treatment to obtain a screen top material and a screen blank, and the screen material is returned to the ball milling treatment, and the screen blank is mixed with the concentrated sulfuric acid. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the above method and system for processing rare earth concentrate further comprises: (7) spraying the first fluorine-containing gas and the second fluorine-containing gas under the action of a spray liquid Treatment to obtain a fluorine-containing slurry.
  • the rare earth concentrate in step (1), has a particle size of 80-320 mesh. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the mass ratio of the rare earth concentrate to the concentrated sulfuric acid is 1: (1.2-1.5). Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (1) the temperature of the mixing process is no higher than 30 degrees Celsius and the time is 5-15 minutes. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the concentrated sulfuric acid has a mass concentration of not less than 93% by weight. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (2) the temperature of the acid hydrolysis treatment is 150-300 degrees Celsius and the time is 1-4 hours. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the initiator liquid is at least one selected from the group consisting of industrial water or a filtrate in a subsequent process. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (3) the time of the leaching process is 0.5-1 h. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (3) the mass ratio of the water to the clinker is (8-12):1. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the shower liquid is at least one selected from the group consisting of water and alkali.
  • the present disclosure provides a system for implementing the above method of treating a rare earth concentrate, according to an embodiment of the present disclosure, the system comprising:
  • a mixing device having a rare earth concentrate inlet, a concentrated sulfuric acid inlet, a mixed slurry outlet, and a first fluorine-containing gas outlet, and an agitator disposed in the mixing device, the mixing device being disposed on an outer wall Water-cooled jacket;
  • An acid hydrolysis device having a mixed slurry inlet, an initiator inlet, a clinker outlet, and a second fluorine-containing gas outlet, the mixed slurry inlet being connected to the mixed slurry outlet, and arranged in the acid hydrolysis device There is a stirring paddle, and a heating device is arranged on the outer wall of the acid dissolving device;
  • a leaching device having a clinker inlet, a water inlet, and a leaching slurry outlet, the clinker inlet being connected to the clinker outlet;
  • a solid-liquid separation device having a leaching slurry inlet, a filtrate outlet, and a leaching slag outlet, the leaching slurry inlet being connected to the leaching slurry outlet, the leaching slag outlet being connected to the acid hydrolysis device.
  • the system for treating rare earth concentrate by rapidly arranging a stirrer in the mixing device, rapid forced mixing of the concentrated sulfuric acid and the rare earth concentrate can be achieved, so that the rare earth concentrate and the concentrated sulfuric acid are sufficiently wetted, thereby avoiding subsequent
  • the agglomeration phenomenon occurs during the acid hydrolysis process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is maintained at Within a certain range, in this way, the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening the rare earth
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO.
  • the system has wide adaptability, low energy consumption, and continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the REO decomposition rate can reach 96%.
  • system for processing rare earth concentrate may further have the following additional technical features:
  • the system for treating a rare earth concentrate further includes: a ball milling device having a rare earth concentrate inlet and a rare earth concentrate particle outlet; a screening device having a rare earth concentrate a mineral particle inlet, a sieve upper material outlet and a sieve lower material outlet, wherein the rare earth concentrate particle inlet is connected to the rare earth concentrate particle outlet, and the sieve upper material outlet is connected to the ball milling device, and the sieve blank outlet Connected to the rare earth concentrate inlet.
  • a ball milling device having a rare earth concentrate inlet and a rare earth concentrate particle outlet
  • a screening device having a rare earth concentrate a mineral particle inlet, a sieve upper material outlet and a sieve lower material outlet, wherein the rare earth concentrate particle inlet is connected to the rare earth concentrate particle outlet, and the sieve upper material outlet is connected to the ball milling device, and the sieve blank outlet Connected to the rare earth concentrate inlet.
  • the system for treating a rare earth concentrate further includes: an exhaust gas treatment device having a fluorine-containing gas inlet, a spray liquid inlet, and a fluorine-containing slurry outlet, the fluorine-containing gas inlet And connected to the first fluorine-containing gas outlet and the second fluorine-containing gas outlet, respectively.
  • the rare earth concentrate inlet, the concentrated sulfuric acid inlet, and the first fluorine-containing gas outlet are each independently located at an upper portion of the agitator, A mixed slurry outlet is located at a lower portion of the agitator.
  • the mixed slurry inlet and the second fluorine-containing gas outlet are respectively independently located at an upper portion of the acid hydrolysis device, and the clinker outlet is located at the The lower part of the acid hydrolysis device.
  • FIG. 1 is a schematic flow chart of a method of processing a rare earth concentrate according to an embodiment of the present disclosure
  • FIG. 2 is a schematic flow chart of a method of processing rare earth concentrate according to still another embodiment of the present disclosure
  • FIG. 3 is a schematic flow chart of a method for treating rare earth concentrate according to still another embodiment of the present disclosure.
  • FIG. 4 is a schematic structural diagram of a system for carrying out a method of processing a rare earth concentrate according to an embodiment of the present disclosure
  • FIG. 5 is a schematic structural diagram of a system for carrying out a method of processing a rare earth concentrate according to still another embodiment of the present disclosure
  • FIG. 6 is a schematic diagram of a system configuration for carrying out a method of processing a rare earth concentrate according to still another embodiment of the present disclosure.
  • first and second are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated.
  • features defining “first” and “second” may include at least one of the features, either explicitly or implicitly.
  • the meaning of "a plurality” is at least two, such as two, three, etc., unless specifically defined otherwise.
  • the terms “installation”, “connected”, “connected”, “fixed”, and the like, are to be understood broadly, and may be either a fixed connection or a detachable connection, unless explicitly stated or defined otherwise. , or integrated; can be mechanical or electrical connection; can be directly connected, or indirectly connected through an intermediate medium, can be the internal communication of two elements or the interaction of two elements, unless otherwise specified Limited.
  • the specific meanings of the above terms in the present disclosure can be understood by those skilled in the art on a case-by-case basis.
  • the first feature "on” or “under” the second feature may be a direct contact of the first and second features, or the first and second features may be indirectly through an intermediate medium, unless otherwise explicitly stated and defined. contact.
  • the first feature "above”, “above” and “above” the second feature may be that the first feature is directly above or above the second feature, or merely that the first feature level is higher than the second feature.
  • the first feature “below”, “below” and “below” the second feature may be that the first feature is directly below or obliquely below the second feature, or merely that the first feature level is less than the second feature.
  • the present disclosure provides a method of processing a rare earth concentrate, according to an embodiment of the present disclosure, with reference to FIG. 1, the method comprising:
  • the rare earth concentrate is mixed with concentrated sulfuric acid to obtain a mixed slurry and a first fluorine-containing gas.
  • the mixing device is a mixture of rare earth concentrate and concentrated sulfuric acid. When mixed with acid, a small amount of CO 2 , HF and SiF 4 gas are generated, and CO 2 and HF are derived from some carbonates in the rare earth concentrate. The substance reacts with concentrated sulfuric acid and is accompanied by some solid dust in the first fluorine-containing gas.
  • the rare earth concentrate of suitable particle size is added to the mixing device through a quantitative feeder and the metered concentrated sulfuric acid according to a certain ratio, and after stirring for a certain period of time, a mixed mixed slurry is formed, and the circulating cooling water is turned on.
  • the above rare earth concentrate may be a fluorocarbon lanthanum rare earth or a Baotou mixed ore (a fluorocarbon lanthanum rare earth and a monazite).
  • the particle size of the rare earth concentrate is not particularly limited, and those skilled in the art may select according to actual needs.
  • the rare earth concentrate may have a particle diameter of 80. -320 mesh.
  • the inventors have found that if the particle size of the rare earth concentrate is too large, it is not conducive to the reaction between the rare earth concentrate and the concentrated sulfuric acid, while the small particle size can increase the contact area between the rare earth concentrate and the concentrated sulfuric acid, but the reaction is too intense, making the reaction impossible. Control, thereby not only causing excessive energy consumption in grinding, but also reducing the decomposition rate of rare earth concentrate.
  • the particle size of the rare earth concentrate proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate while saving energy consumption.
  • the mixing mass ratio of the rare earth concentrate to the concentrated sulfuric acid is not particularly limited, and those skilled in the art can select according to actual needs.
  • the rare earth concentrate and the rare earth concentrate The mixed mass ratio of concentrated sulfuric acid may be 1: (1.2-1.5). The inventors found that the low mass ratio of rare earth concentrate to concentrated sulfuric acid would cause insufficient reaction between rare earth concentrate and concentrated sulfuric acid, resulting in low decomposition rate of rare earth concentrate, and also caused the bismuth in rare earth concentrate to be difficult to decompose.
  • the enrichment is in the leaching slag to form radioactive slag; and if the mass ratio of the rare earth concentrate to the concentrated sulphuric acid is too high, the concentrated sulfuric acid is excessively consumed, the mixing time is prolonged, and the residual acid in the subsequent process is high. Therefore, the mixing ratio of the rare earth concentrate and the concentrated sulfuric acid proposed by the present disclosure can further increase the decomposition rate of the rare earth concentrate, and at the same time increase the mixing rate and save energy.
  • the conditions of the mixing process are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the mixing process may be no higher than 30 degrees Celsius.
  • the time can be 5-15min.
  • the inventors have found that the excessive temperature of the mixed treatment causes the rare earth concentrate to produce a local reaction in advance with the concentrated sulfuric acid, and the mixing effect is poor; the mixing time is too short to reach the condition that the rare earth concentrate is in full contact with the concentrated sulfuric acid, and the mass transfer effect is affected. Therefore, if the mixing treatment temperature is too high and the mixing time is too long or too short, the decomposition rate of the rare earth element oxide in the rare earth concentrate is lowered.
  • the mass concentration of concentrated sulfuric acid is not particularly limited, and those skilled in the art may select according to actual needs. According to a specific embodiment of the present disclosure, the mass concentration of concentrated sulfuric acid may be not lower than 93wt%. The inventors have found that the use of concentrated sulfuric acid at this concentration can significantly improve the infiltration efficiency of the rare earth concentrate, and at the same time improve the quality of the mixed slurry and thereby increase the decomposition rate of the rare earth element oxide.
  • the mixed slurry and the initiator are mixed for acid hydrolysis to obtain clinker and a second fluorine-containing gas.
  • the mixed slurry is added to the acid hydrolysis device through the mixed slurry outlet of the mixing device, and the inlet liquid inlet valve is opened, the concentrated sulfuric acid in the mixed slurry is diluted, and the acid solution is adjusted by the auxiliary heating device.
  • the acid hydrolysis reaction is completed in the acid hydrolysis device to form a bulk clinker.
  • the inventors have found that in the acid hydrolysis device, the two processes of maturation and roasting can be completed, the time for the acid hydrolysis reaction of the rare earth concentrate is significantly shortened, and in the acid hydrolysis process, the viscosity of the internal material changes greatly, and gradually changes from the fluid state. In the semi-dry state, it eventually becomes dry and clinker is obtained, and the acid hydrolysis device can effectively cope with the change of the characteristics of the above materials.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can effectively avoid concentrated sulfuric acid due to the low temperature in the whole acid hydrolysis process.
  • the decomposition of the generated sulfur-containing gas makes it possible to recycle the generated second fluorine-containing gas, and at the same time, it can effectively prevent the waste from entering the slag and causing radioactive pollution and waste of cesium resources.
  • the conditions of the acid hydrolysis treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the acid hydrolysis treatment may be 150-300. Celsius, the time can be 1-4h.
  • the inventors have found that the excessive temperature of the acid hydrolysis treatment causes the concentrated sulfuric acid to decompose to produce a sulfur-containing gas, and at the same time, the bismuth in the subsequent clinker is not easily leached into the solution and remains in the leaching slag to form a radioactive solid waste; Too low and too short acid hydrolysis time will lead to low decomposition rate of rare earth element oxides; too long acid hydrolysis time can not further increase the decomposition rate of rare earth concentrates, but increase energy consumption and prolong the whole process time.
  • the temperature and time of the acid hydrolysis treatment proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate, increase the leaching rate of the ruthenium, and save energy.
  • the specific type of the initiating liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the initiating liquid may be selected from an extraction process.
  • rare earth concentrate is mixed with concentrated sulfuric acid and heated to a certain temperature
  • REO, ThO 2 and the like in the concentrate react with sulfuric acid to form soluble sulfate.
  • CaF 2 , Fe 2 O 3 and the like also react to varying degrees to sulfate.
  • Rare earth sulfate, barium sulfate, iron sulfate or the like can be dissolved in an aqueous solution.
  • Fluorine enters the calcination off-gas in the form of HF or SiF 4 and can be reacted with ammonia in the presence of steam to form solid ammonium hydrogen fluoride (NH 4 HF 2 ), which is sold as a product.
  • ThO 2 +2H 2 SO 4 Th(SO 4 ) 2 +2H 2 O
  • SiO 2 +4HF SiF 4 ⁇ +2H 2 O
  • the clinker and water are mixed and subjected to a leaching treatment to obtain a leaching slurry.
  • the clinker in the acid hydrolysis device is sent to the leaching device through the clinker through the quantitative screw machine, and a certain proportion of water is added to carry out the leaching reaction. After the reaction for a period of time, the leaching slurry is formed.
  • the inventors have found that, due to the bismuth in the rare earth concentrate during the acid hydrolysis process, the bismuth citrate enters the leaching slurry during leaching, thus realizing the recycling of strontium resources and avoiding the radioactive hazard of strontium.
  • the conditions of the leaching treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the leaching treatment may be normal temperature, and the time may be 0.5-1h. The inventors have found that the leaching temperature is normal temperature, and the sulphate in the clinker can be dissolved in water without heating, thereby avoiding waste of external heat source, and the appropriate leaching time can ensure complete dissolution of the sulphate.
  • the mass ratio of water to clinker is not particularly limited, and those skilled in the art can select according to actual needs.
  • S400 The leaching slurry is subjected to solid-liquid separation treatment, and the leaching slag is returned to S200 for acid hydrolysis treatment.
  • the leaching slurry is subjected to solid-liquid separation treatment to obtain a filtrate and leaching slag, and the leaching slag is returned to S200 for acid hydrolysis treatment.
  • the leaching slurry obtained by the leaching device is sent to the solid-liquid separation device for solid-liquid separation treatment, the filtrate and the leaching slag are obtained, and the leaching slag is quantitatively returned to the acid hydrolysis device in batches, and the filtrate is fed.
  • the next extraction process Thereby, the decomposition rate of the rare earth element oxide can be remarkably improved, and the recovery rate of ruthenium can be improved.
  • the method and system for processing rare earth concentrate can achieve rapid forced mixing of concentrated sulfuric acid and rare earth concentrate by arranging a stirrer in the mixing device, so that the rare earth concentrate and concentrated sulfuric acid are sufficiently wetted, thereby avoiding The agglomeration phenomenon occurs in the subsequent acid hydrolysis process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is maintained.
  • the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening
  • the time of acid hydrolysis of rare earth concentrates, and the viscosity of internal materials changes greatly during the acid hydrolysis process, gradually changing from a fluid state to a semi-dry state, eventually becoming dry, obtaining clinker, and the acid hydrolysis device can effectively cope with the above Changes in material properties.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO. Therefore, the method has wide adaptability of raw materials, low energy consumption, and can realize continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the decomposition rate of REO can reach 96%.
  • the method before the treatment of mixing the rare earth concentrate with concentrated sulfuric acid, the method further includes:
  • the rare earth concentrate is subjected to a ball milling treatment to obtain rare earth concentrate particles.
  • a ball milling treatment to obtain rare earth concentrate particles.
  • the rare earth concentrate particles obtained above are subjected to sieving treatment to obtain a sieve top material and a sieve blank, and the sieve material is returned to a ball milling treatment, and the sieve blank is mixed with concentrated sulfuric acid.
  • the decomposition rate of the rare earth element oxide can be further improved.
  • the inventors have found that by returning the sieve material having an unqualified particle size after sieving to the ball mill for ball milling, the raw material cost and time cost of the process can be significantly saved, and the sieved material obtained after sieving can be sent to Mixing with concentrated sulfuric acid in the mixing device can further increase the decomposition rate of the rare earth element oxide.
  • the size of the undersize material may be 80-320 mesh.
  • the above method and system for processing a rare earth concentrate further includes:
  • the first fluorine-containing gas and the second fluorine-containing gas are sprayed under the action of the shower liquid to obtain a fluorine-containing slurry.
  • the recycling of the fluorine-containing gas can be realized, and the problem that the exhaust gas pollutes the environment can be avoided.
  • the inventors have found that both the mixing device and the acid hydrolysis device have temperature control devices, which significantly reduce the content of impurities in the first fluorine-containing gas and the second fluorine-containing gas, so that the first fluorine-containing gas and the second fluorine-containing gas are The dust content is small.
  • the fluorine-containing gas can be directly sprayed by the spray liquid without providing a dust removing device before the spray treatment, and the fluorine-containing gas and the dust therein are dissolved in the spray liquid, and after filtering,
  • the filter residue can be returned to the acid hydrolysis unit for recycling, and the filtrate can be used to prepare a fluoride salt. It is beneficial to realize the recovery and utilization of fluorine-containing gas and avoid the problem of exhaust gas polluting the environment.
  • the specific type of the spray liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the spray liquid may be selected from water and At least one of the alkali liquids, wherein the alkali liquid may be ammonia water.
  • the present disclosure provides a system for implementing the above method of treating a rare earth concentrate, according to an embodiment of the present disclosure, referring to FIG. 4, the system includes: a mixing device 100, an acid hydrolysis device 200, leaching device 300 and solid-liquid separation device 400.
  • the mixing device 100 has a rare earth concentrate inlet 101, a concentrated sulfuric acid inlet 102, a mixed slurry outlet 103, and a first fluorine-containing gas outlet 104, and a stirrer 11 is disposed in the mixing device, the mixing device A water-cooling jacket 12 is disposed on the outer wall and is adapted to mix the rare earth concentrate with concentrated sulfuric acid to obtain a mixed slurry and a first fluorine-containing gas.
  • the mixing device is a mixture of rare earth concentrate and concentrated sulfuric acid. When mixed with acid, a small amount of CO 2 , HF and SiF 4 gas are generated, and CO 2 and HF are derived from some carbonates in the rare earth concentrate.
  • the substance reacts with concentrated sulfuric acid and is accompanied by some solid dust in the first fluorine-containing gas.
  • the rare earth concentrate of suitable particle size is added to the mixing device through a quantitative feeder and the metered concentrated sulfuric acid according to a certain ratio, and after stirring for a certain period of time, a mixed mixed slurry is formed, and the circulating cooling water is turned on. , control the temperature inside the mixing device within a certain range.
  • the inventors have found that by arranging the agitator in the mixing device, the rapid forced mixing of the concentrated sulfuric acid and the rare earth concentrate can be achieved, so that the rare earth concentrate and the concentrated sulfuric acid are fully wetted, thereby avoiding the agglomeration phenomenon in the subsequent acid hydrolysis process.
  • the favorable conditions for the mass transfer of the acid hydrolysis process are created.
  • the water-cooled jacket in the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is kept within a certain range.
  • the above-mentioned rare earth concentrate is not particularly limited, and may be, for example, a fluorocarbon lanthanum rare earth or a Baotou mixed ore (a fluorocarbon lanthanum rare earth and a monazite); the concentrated sulfuric acid can be pumped to a mixture by metering.
  • the agitator in the mixing device is not particularly limited, and those skilled in the art can select according to actual needs, for example, it can be a double-layer stirring paddle, that is, two layers are arranged on the stirring shaft, and can be used for rare earth. Intense mixing of concentrate with concentrated sulfuric acid.
  • the rare earth concentrate inlet 101, the concentrated sulfuric acid inlet 102, and the first fluorine-containing gas outlet 104 are independently located at the upper portion of the agitator 11, respectively, and the mixed slurry outlet 103 is located at the agitator.
  • the particle size of the rare earth concentrate is not particularly limited, and those skilled in the art may select according to actual needs.
  • the particle size of the rare earth concentrate may be 80-320 mesh. The inventors have found that if the particle size of the rare earth concentrate is too large, it is not conducive to the reaction between the rare earth concentrate and the concentrated sulfuric acid, while the small particle size can increase the contact area between the rare earth concentrate and the concentrated sulfuric acid, but the reaction is too intense, making the reaction impossible. Control, thereby not only causing excessive energy consumption in grinding, but also reducing the decomposition rate of rare earth concentrate.
  • the particle size of the rare earth concentrate proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate while saving energy consumption.
  • the mixing mass ratio of the rare earth concentrate to the concentrated sulfuric acid is not particularly limited, and those skilled in the art can select according to actual needs.
  • the rare earth concentrate and the rare earth concentrate The mixed mass ratio of concentrated sulfuric acid may be 1: (1.2-1.5). The inventors found that the low mass ratio of rare earth concentrate to concentrated sulfuric acid would cause insufficient reaction between rare earth concentrate and concentrated sulfuric acid, resulting in low decomposition rate of rare earth concentrate, and also caused the bismuth in rare earth concentrate to be difficult to decompose.
  • the enrichment is in the leaching slag to form radioactive slag; and if the mass ratio of the rare earth concentrate to the concentrated sulphuric acid is too high, the concentrated sulfuric acid is excessively consumed, the mixing time is prolonged, and the residual acid in the subsequent process is high. Therefore, the mixing ratio of the rare earth concentrate and the concentrated sulfuric acid proposed by the present disclosure can further increase the decomposition rate of the rare earth concentrate, and at the same time increase the mixing rate and save energy.
  • the conditions of the mixing process are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the mixing process may be no higher than 30 degrees Celsius.
  • the time can be 5-15min.
  • the inventors have found that the excessive temperature of the mixed treatment causes the rare earth concentrate to produce a local reaction in advance with the concentrated sulfuric acid, and the mixing effect is poor; the mixing time is too short to reach the condition that the rare earth concentrate is in full contact with the concentrated sulfuric acid, and the mass transfer effect is affected. Therefore, if the mixing treatment temperature is too high and the mixing time is too long or too short, the decomposition rate of the rare earth element oxide in the rare earth concentrate is lowered.
  • the mass concentration of concentrated sulfuric acid is not particularly limited, and those skilled in the art may select according to actual needs. According to a specific embodiment of the present disclosure, the mass concentration of concentrated sulfuric acid may be not lower than 93wt%. The inventors have found that the use of concentrated sulfuric acid at this concentration can significantly improve the infiltration efficiency of the rare earth concentrate, and at the same time improve the quality of the mixed slurry and thereby increase the decomposition rate of the rare earth element oxide.
  • the acid hydrolysis device 200 has a mixed slurry inlet 201, an initiator liquid inlet 202, a clinker outlet 203, and a second fluorine-containing gas outlet 204, and the mixed slurry inlet 201 is connected to the mixed slurry outlet 103, and the acid hydrolysis device
  • a stirring paddle 21 is disposed in the 200
  • a heating device 22 is disposed on the outer wall of the acid hydrolysis device, and is adapted to mix the mixed slurry and the initiator liquid for acid hydrolysis treatment to obtain clinker and a second fluorine-containing gas.
  • the mixed slurry is added to the acid hydrolysis device through the mixed slurry outlet of the mixing device, and the inlet liquid inlet valve is opened, the concentrated sulfuric acid in the mixed slurry is diluted, and the acid solution is adjusted by the auxiliary heating device.
  • the acid hydrolysis reaction is completed in the acid hydrolysis device to form a bulk clinker.
  • the inventors have found that in the acid hydrolysis device, the two processes of maturation and roasting can be completed, the time for the acid hydrolysis reaction of the rare earth concentrate is significantly shortened, and in the acid hydrolysis process, the viscosity of the internal material changes greatly, and gradually changes from the fluid state.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can effectively avoid concentrated sulfuric acid due to the low temperature in the whole acid hydrolysis process.
  • the decomposition of the generated sulfur-containing gas makes it possible to recycle the generated second fluorine-containing gas, and at the same time, it can effectively prevent the waste from entering the slag and causing radioactive pollution and waste of cesium resources.
  • the above-mentioned acid hydrolysis device is not particularly limited, and those skilled in the art may select according to actual needs, for example, may be a horizontal reactor, and the stirring paddle may be a spiral type side-by-side arrangement of agitating paddles, a heating device.
  • the heating method can be electric heating or steam heating.
  • the mixed slurry inlet 201 and the second fluorine-containing gas outlet 204 are independently located at the upper portion of the acid hydrolysis device 200, respectively, and the clinker outlet 203 is located at the lower portion of the acid hydrolysis device 200.
  • the conditions of the acid hydrolysis treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the acid hydrolysis treatment may be 150- 300 degrees Celsius, the time can be 1-4h.
  • the inventors have found that the excessive temperature of the acid hydrolysis treatment causes the concentrated sulfuric acid to decompose to produce a sulfur-containing gas, and at the same time, the bismuth in the subsequent clinker is not easily leached into the solution and remains in the leaching slag to form a radioactive solid waste; Too low and too short acid hydrolysis time will lead to low decomposition rate of rare earth element oxides; too long acid hydrolysis time can not further increase the decomposition rate of rare earth concentrates, but increase energy consumption and prolong the whole process time.
  • the temperature and time of the acid hydrolysis treatment proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate, increase the leaching rate of the ruthenium, and save energy.
  • the specific type of the initiator liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the initiator liquid may be selected from an extraction process. A waste acid or a type of industrial water. The inventors have found that the acid hydrolysis reaction needs to reach a certain temperature before the use of the initiator liquid can dilute the exothermic heat of the concentrated sulfuric acid, increase the temperature of the mixed slurry, and promote the progress of the acid hydrolysis reaction, so that the dilution heat can be utilized to reduce the external heat source. Supply.
  • rare earth concentrate is mixed with concentrated sulfuric acid and heated to a certain temperature
  • REO, ThO 2 and the like in the concentrate react with sulfuric acid to form soluble sulfate.
  • CaF 2 , Fe 2 O 3 and the like also react to varying degrees to sulfate.
  • Rare earth sulfate, barium sulfate, iron sulfate or the like can be dissolved in an aqueous solution.
  • Fluorine enters the calcination off-gas in the form of HF or SiF 4 and can be reacted with ammonia in the presence of steam to form solid ammonium hydrogen fluoride (NH 4 HF 2 ), which is sold as a product.
  • ThO 2 +2H 2 SO 4 Th(SO 4 ) 2 +2H 2 O
  • SiO 2 +4HF SiF 4 ⁇ +2H 2 O
  • the leaching device 300 has a clinker inlet 301, a water inlet 302, and a leaching slurry outlet 303, and the clinker inlet 301 is connected to the clinker outlet 203 and is adapted to mix the clinker and water for leaching treatment, In order to obtain a leaching slurry.
  • the clinker in the acid hydrolysis device is sent to the leaching device through the clinker through the quantitative screw machine, and a certain proportion of water is added to carry out the leaching reaction. After the reaction for a period of time, the leaching slurry is formed.
  • the inventors have found that, due to the bismuth in the rare earth concentrate during the acid hydrolysis process, the bismuth citrate enters the leaching slurry during leaching, thus realizing the recycling of strontium resources and avoiding the radioactive hazard of strontium.
  • the conditions of the leaching treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the leaching treatment may be normal temperature, and the time may be 0.5-1h. The inventors have found that the leaching temperature is normal temperature, and the sulphate in the clinker can be dissolved in water without heating, thereby avoiding waste of external heat source, and the appropriate leaching time can ensure complete dissolution of the sulphate.
  • the mass ratio of water to clinker is not particularly limited, and those skilled in the art can select according to actual needs.
  • the solid-liquid separation device 400 has a leaching slurry inlet 401, a filtrate outlet 402, and a leaching slag outlet 403, and the leaching slurry inlet 401 is connected to the leaching slurry outlet 303, and the leaching slag outlet 403 is connected to the acid eliminating device 200. And suitable for the solid-liquid separation treatment of the leach slurry to obtain the filtrate and the leach residue, and return the leach residue to the acid hydrolysis device for acid hydrolysis treatment.
  • the leaching slurry obtained by the leaching device is sent to the solid-liquid separation device for solid-liquid separation treatment, the filtrate and the leaching slag are obtained, and the leaching slag is quantitatively returned to the acid hydrolysis device in batches, and the filtrate is fed.
  • the next extraction process Thereby, the decomposition rate of the rare earth element oxide can be remarkably improved, and the recovery rate of ruthenium can be improved.
  • the system for treating rare earth concentrate can realize rapid forced mixing of concentrated sulfuric acid and rare earth concentrate by arranging a stirrer in the mixing device, so that the rare earth concentrate and the concentrated sulfuric acid are sufficiently wetted, thereby avoiding the subsequent acid
  • the agglomeration phenomenon occurs during the solution process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is kept constant.
  • the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening the rare earth essence.
  • the time of the acid hydrolysis reaction, and during the acid hydrolysis process the viscosity of the internal material changes greatly, from the fluid state to the semi-dry state, and finally becomes dry, and the clinker is obtained.
  • the acid hydrolysis device can effectively cope with the above material properties. The change.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO.
  • the system has wide adaptability, low energy consumption, and continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the REO decomposition rate can reach 96%.
  • the above-described system for processing rare earth concentrate further includes: a ball milling device 500 and a screening device 600.
  • the ball milling apparatus 500 has a rare earth concentrate inlet 501 and a rare earth concentrate particle outlet 502, and is adapted to perform ball milling treatment on the rare earth concentrate before the rare earth concentrate is mixed with the concentrated sulfuric acid to obtain a rare earth. Concentrate particles. Thereby, it is advantageous to increase the decomposition rate of the rare earth element oxide.
  • the screening device 600 has a rare earth concentrate particle inlet 601, a screen upper material outlet 602, and a sieve lower material outlet 603, and the rare earth concentrate particle inlet 601 is connected to the rare earth concentrate particle outlet 502.
  • 602 is connected to the ball milling device 500
  • the undersize outlet 603 is connected to the rare earth concentrate inlet 101, and is adapted to sieve the rare earth concentrate particles obtained above to obtain the sieve material and the sieve material, and to sieve the sieve.
  • the material is returned to the ball milling treatment, and the sieve blank is mixed with concentrated sulfuric acid.
  • the inventors have found that by returning the sieve material having an unqualified particle size after sieving to the ball mill for ball milling, the raw material cost and time cost of the process can be significantly saved, and the sieved material obtained after sieving can be sent to Mixing with concentrated sulfuric acid in the mixing device can further increase the decomposition rate of the rare earth element oxide.
  • the screen discharge outlet of the screening device can be connected to the rare earth concentrate inlet of the above mixing device through a metering device.
  • the size of the undersize material may be 80-320 mesh.
  • the above-described system for processing rare earth concentrate further includes: an exhaust gas treatment device 700.
  • the exhaust gas treatment device 700 has a fluorine-containing gas inlet 701, a spray liquid inlet 702, a fluorine-containing slurry outlet 703, and a fluorine-containing gas inlet 701, respectively, and a first fluorine-containing gas outlet 104 and a second fluorine-containing gas outlet.
  • the 204 is connected and adapted to spray the first fluorine-containing gas and the second fluorine-containing gas under the action of the spray liquid to obtain a fluorine-containing slurry.
  • both the mixing device and the acid hydrolysis device have temperature control devices, which significantly reduce the content of impurities in the first fluorine-containing gas and the second fluorine-containing gas, so that the first fluorine-containing gas and the second fluorine-containing gas are The dust content is small.
  • the fluorine-containing gas can be directly sprayed by the spray liquid without providing a dust removing device before the spray treatment, and the fluorine-containing gas and the dust therein are dissolved in the spray liquid, and after filtering,
  • the filter residue can be returned to the acid hydrolysis device for recycling, and the filtrate can be used for preparing the fluorine salt, which is beneficial to the recovery and utilization of the fluorine-containing gas, and avoids the problem that the exhaust gas pollutes the environment.
  • the specific type of the spray liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the spray liquid may be selected from water and At least one of the alkali liquids, wherein the alkali liquid may be ammonia water.
  • the fluorocarbon lanthanum rare earth ore is ball milled by a ball mill and sieved to obtain fluorocarbon cerium rare earth concentrate particles with a particle size of 80-320 mesh; the fluorocarbon slag rare earth concentrate is metered and then pre-measured.
  • the mixing device with 98wt% concentrated sulfuric acid the mass ratio of concentrated sulfuric acid to fluorocarbon cerium rare earth concentrate particles is 1.4:1, the circulating cooling water of the mixing device is turned on, and the temperature in the mixing device is controlled to be less than 30 degrees Celsius.
  • the loose clinker is quantitatively sent to the leaching device through the clinker outlet of the acid hydrolysis device, and in the leaching device, the water and the clinker are metered according to the mass ratio of 8:1.
  • Dip The tank is mechanically stirred for 1 hour to form a leaching slurry, and then the leaching slurry is pumped to a plate and frame filter press to obtain a filtrate and a leaching slag.
  • the leaching slag rate is 8 wt%, and the chemical composition of the leaching slag is analyzed, and the leaching slag is analyzed.
  • the aliquots are returned to the acid hydrolysis unit in batches, and the leachate is sent to the next extraction step.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 95.18%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
  • the fluorocarbon lanthanum rare earth ore is ball milled by a ball mill and sieved to obtain fluorocarbon cerium rare earth concentrate particles with a particle size of 80-320 mesh; the fluorocarbon lanthanum rare earth concentrate particles are metered and put into pre-measurement
  • the mixing device with 98wt% concentrated sulfuric acid the mass ratio of concentrated sulfuric acid to fluorocarbon cerium rare earth concentrate particles is 1.5:1
  • the circulating cooling water of the mixing device is turned on, and the temperature in the mixing device is controlled to be less than 30 degrees Celsius, fully Stir for 8min to form a mixed slurry with uniform acid mixing, and at the same time produce a first fluorine-containing gas; then discharge the mixed slurry through the mixed slurry outlet of the mixing device, add to the acid hydrolysis device, and open the inlet liquid (waste acid) inlet valve Diluting the concentrated sulfuric acid in the mixed slurry, releasing the heat, and adjusting the temperature in the acid hydrolysis device through the auxiliary heating
  • the leaching slag rate is 6.3wt%, analyzing the chemical composition of the leaching slag, and leaching the upper leaching
  • the slag is returned to the acid hydrolysis unit in batches, and the leachate is sent to the next extraction step.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 96%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
  • the mixed ore containing fluorocarbon lanthanum rare earth or monazite having a particle size of 80-320 mesh is metered into a mixing device pre-metered with 98 wt% concentrated sulfuric acid, and the mass ratio of concentrated sulfuric acid to mixed ore is 1.5. :1, the circulating cooling water of the mixing device is turned on, the temperature in the mixing device is controlled to be less than 30 degrees Celsius, and the mixture is stirred for 10 minutes to form a mixed slurry with uniform acid mixing, and the first fluorine-containing gas is generated; and the mixed slurry is mixed.
  • the mixed slurry outlet of the device is discharged, added to the acid hydrolysis device, the inlet liquid (mixture containing industrial water and waste acid) is opened, the concentrated sulfuric acid in the mixed slurry is diluted, the heat is released, and the auxiliary device is assisted by the acid hydrolysis device.
  • the clinker outlet is quantitatively fed to the leaching device.
  • the water and clinker are metered according to the mass ratio of 12:1, and then placed in a leaching tank, mechanically stirred for 1 hour to form a leaching slurry, and then the leaching slurry is pumped to The plate and frame filter press is filter-filtered to obtain the filtrate and the leaching slag, and the leaching slag rate is 6.8 wt%.
  • the chemical composition of the leaching slag is analyzed, and the upper leaching slag is quantitatively returned to the acid hydrolysis device in batches, and the leaching solution is sent to the next stage extraction. Process.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 96%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
  • the mixed ore containing fluorocarbon lanthanum rare earth or monazite having a particle size of 80-320 mesh is metered into a mixing device pre-metered with 98 wt% concentrated sulfuric acid, and the mass ratio of concentrated sulfuric acid to mixed ore is 1.4.
  • the internal temperature is stirred at 100 ° C for 30 min, followed by acid hydrolysis at 280 ° C for 2 h to form a loose clinker, while producing a second fluorine-containing gas; the loose clinker is quantitatively fed through the clinker outlet of the acid hydrolysis device
  • the water and clinker are metered in a mass ratio of 10:1, placed in a leaching tank, mechanically stirred for 1 hour to form a leaching slurry, and the leaching slurry is pumped to a plate and frame filter press for pressure filtration. Too leaching residue and the filtrate, the residue leaching residue was 7.2wt%, the chemical composition analysis of leach residue, the leach residue quantitatively batches return means acidolysis, and the lower section of the extraction liquid into the leaching step.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 96%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.

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Abstract

处理稀土精矿的方法和系统，方法包括：(1)将稀土精矿与浓硫酸进行混合处理，以便得到混合浆液和第一含氟气体；(2)将混合浆液和引发液混合进行酸解处理，以便得到熟料和第二含氟气体；(3)将熟料和水混合后进行浸出处理，以便得到浸出浆液；(4)将浸出浆液进行固液分离处理，以便得到过滤液和浸出渣，并将浸出渣返回步骤(2)进行酸解处理。

Description

处理稀土精矿的方法和系统 技术领域
本公开属于稀土生产领域，具体而言，本公开涉及处理稀土精矿的方法和系统。
背景技术
包头混合矿【氟碳铈稀土和独居石(磷铈镧矿/磷镧铈石)的混合矿】和氟碳铈矿是我国稀土矿的重要组成部分。针对包头混合矿的特点，目前处理此类矿的工业方法主要是浓硫酸焙烧法。该法工艺连续易控制，易于大规模生产，但该法由于在高温下对混合矿进行分解，矿中的钍以焦磷酸钍形态进入渣中，会造成放射性污染，也会造成钍资源浪费，且含氟和硫的废气回收利用难度大。针对氟碳铈矿的特点，目前工业酸解方法主要是氧化焙烧-盐酸优溶。此法特点是投资小，但存在工艺不连续，钍和氟分散在渣和废水中难以回收，对环境造成污染等问题。由此可知，在高温条件下处理混合矿和氟碳铈矿均容易造成钍资源浪费，尾气环境污染的问题。基于此，国内相关科研院所提出采用浓硫酸低温焙烧技术分解稀土矿，在低温(150～300℃)条件下焙烧稀土精矿，稀土分解率可达95％以上，大于90％的钍进入浸出液，能有效回收稀土精矿中的钍。但该工艺技术尚未成熟，难以进行连续化动态生产。
因此，现有处理稀土精矿的技术有待进一步改进。
公开内容
本公开旨在至少在一定程度上解决相关技术中的技术问题之一。为此，本公开的一个目的在于提出一种处理稀土精矿的方法和系统。该方法可以处理氟碳铈稀土矿和含有氟碳铈稀土矿和独居石的混合矿，能耗低，且可实现连续化生产，同时可有效回收钍资源，并显著提高稀土精矿的分解率，REO分解率可达96％。
在本公开的一个方面，本公开提出了一种处理稀土精矿的方法，根据本公开的实施例，该方法包括：
(1)将稀土精矿与浓硫酸进行混合处理，以便得到混合浆液和第一含氟气体；
(2)将所述混合浆液和引发液混合进行酸解处理，以便得到熟料和第二含氟气体；
(3)将所述熟料和水混合后进行浸出处理，以便得到浸出浆液；
(4)将所述浸出浆液进行固液分离处理，以便得到过滤液和浸出渣，并将所述浸出渣返回步骤(2)进行所述酸解处理。
根据本公开实施例的处理系统精矿的方法通过在混料装置中布置搅拌器，可实现浓硫 酸与稀土精矿的快速强制混合，使稀土精矿与浓硫酸浸润充分，从而避免在后续酸解过程中出现结团现象，为酸解过程的传质创造了有利的条件，并且混料装置外壁上的水冷夹套可通过循环水冷却混料装置，使得混料装置内部的温度保持在一定的范围内，如此，可有效避免高温下稀土矿的分解，从而可以实现钍资源的回收；同时，本申请中在酸解装置中即可实现熟化和焙烧两大工序，从而显著缩短了稀土精矿酸解反应的时间，且在酸解过程中，内部物料的粘度变化大，由流体态逐渐变为半干状态，最终变为干性，得到熟料，酸解装置可有效应对上述物料特性的变化。并且酸解装置中的搅拌桨可加速酸解反应的进行，酸解装置外壁上的加热装置可提供酸解反应所需的合适温度，且因整个酸解过程中的温度低，可以进一步避免钍进入渣中而造成放射性污染和钍资源的浪费，并且可有效避免浓硫酸分解产生的含硫气体，从而使得产生的第二含氟气体的回收利用成为可能；酸解过程中稀土精矿中的钍变为钍酸盐，钍酸盐在浸出的时候会进入浸出浆液中，如此，可实现钍资源的回收利用，避免钍的放射性危害；浸出浆液经固液分离后所得的浸出渣可继续返回至酸解装置中进行酸解处理，可进一步提高钍的回收率和REO的分解率。由此，该方法原料适应性广、能耗低，且可实现连续化生产，同时可有效回收钍资源，并显著提高稀土精矿的分解率，REO分解率可达96％。
另外，根据本公开上述实施例的处理稀土精矿的方法，还可以具有如下附加的技术特征：
在本公开的一些实施例中，在将所述稀土精矿与浓硫酸混合处理之前进一步包括：(5)将所述稀土精矿进行球磨处理，以便得到稀土精矿颗粒；(6)将所述稀土精矿颗粒进行筛分处理，以便得到筛上料和筛下料，并将所述筛上料返回进行所述球磨处理，将所述筛下料与所述浓硫酸进行混合处理。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，上述处理稀土精矿的方法和系统进一步包括：(7)将所述第一含氟气体和所述第二含氟气体在喷淋液的作用下进行喷淋处理，以便得到含氟浆液。由此，可实现含氟气体的回收利用，避免尾气污染环境的问题。
在本公开的一些实施例中，在步骤(1)中，所述稀土精矿的粒径为80-320目。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(1)中，所述稀土精矿与所述浓硫酸的混合质量比为1：(1.2-1.5)。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(1)中，所述混合处理的温度不高于30摄氏度，时间为5-15min。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(1)中，所述浓硫酸的质量浓度不低于93wt％。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(2)中，所述酸解处理的温度为150-300摄氏度，时间为1-4h。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(2)中，所述引发液为选自工业水或后续工序中的过滤液中的至少之一。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(3)中，所述浸出处理的时间为0.5-1h。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(3)中，所述水与所述熟料的质量比为(8-12)：1。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在步骤(7)中，所述喷淋液为选自水和碱液中的至少之一。由此，有利于提高含氟气体的回收利用率。
在本公开的再一个方面，本公开提出了一种用于实施上述处理稀土精矿的方法的系统，根据本公开的实施例，该系统包括：
混料装置，所述混料装置具有稀土精矿入口、浓硫酸入口、混合浆液出口和第一含氟气体出口，并且所述混料装置内布置有搅拌器，所述混料装置外壁上布置有水冷夹套；
酸解装置，所述酸解装置具有混合浆液入口、引发液入口、熟料出口和第二含氟气体出口，所述混合浆液入口与所述混合浆液出口相连，并且所述酸解装置内布置有搅拌桨，所述酸解装置外壁上布置有加热装置；
浸出装置，所述浸出装置具有熟料入口、水入口和浸出浆液出口，所述熟料入口与所述熟料出口相连；
固液分离装置，所述固液分离装置具有浸出浆液入口、过滤液出口和浸出渣出口，所述浸出浆液入口与所述浸出浆液出口相连，所述浸出渣出口与所述酸解装置相连。
根据本公开实施例的处理稀土精矿的系统，通过在混料装置中布置搅拌器，可实现浓硫酸与稀土精矿的快速强制混合，使稀土精矿与浓硫酸浸润充分，从而避免在后续酸解过程中出现结团现象，为酸解过程的传质创造了有利的条件，并且混料装置外壁上的水冷夹套可通过循环水冷却混料装置，使得混料装置内部的温度保持在一定的范围内，如此，可有效避免高温下稀土矿的分解，从而可以实现钍资源的回收；同时，本申请中在酸解装置中即可实现熟化和焙烧两大工序，从而显著缩短了稀土精矿酸解反应的时间，且在酸解过程中，内部物料的粘度变化大，由流体态逐渐变为半干状态，最终变为干性，得到熟料，酸解装置可有效应对上述物料特性的变化。并且酸解装置中的搅拌桨可加速酸解反应的进行，酸解装置外壁上的加热装置可提供酸解反应所需的合适温度，且因整个酸解过程中的温度低，可以进一步避免钍进入渣中而造成放射性污染和钍资源的浪费，并且可有效避免浓硫酸分解产生的含硫气体，从而使得产生的第二含氟气体的回收利用成为可能；酸解过 程中稀土精矿中的钍变为钍酸盐，钍酸盐在浸出的时候会进入浸出浆液中，如此，可实现钍资源的回收利用，避免钍的放射性危害；浸出浆液经固液分离后所得的浸出渣可继续返回至酸解装置中进行酸解处理，可进一步提高钍的回收率和REO的分解率。由此，该系统原料适应性广、能耗低，且可实现连续化生产，同时可有效回收钍资源，并显著提高稀土精矿的分解率，REO分解率可达96％。
另外，根据本公开上述实施例的处理稀土精矿的系统还可以具有如下附加的技术特征：
在本公开的一些实施例中，上述处理稀土精矿的系统进一步包括：球磨装置，所述球磨装置具有稀土精矿进口和稀土精矿颗粒出口；筛分装置，所述筛分装置具有稀土精矿颗粒入口、筛上料出口和筛下料出口，所述稀土精矿颗粒入口与所述稀土精矿颗粒出口相连，所述筛上料出口与所述球磨装置相连，所述筛下料出口与所述稀土精矿入口相连。由此，可进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，上述处理稀土精矿的系统进一步包括：尾气处理装置，所述尾气处理装置具有含氟气体入口、喷淋液入口和含氟浆液出口，所述含氟气体入口分别与所述第一含氟气体出口和所述第二含氟气体出口相连。由此，可实现含氟气体的回收利用，避免尾气污染环境的问题。
在本公开的一些实施例中，在所述混料装置中，所述稀土精矿入口、所述浓硫酸入口和所述第一含氟气体出口分别独立地位于所述搅拌器上部，所述混合浆液出口位于所述搅拌器的下部。由此，可显著提高混合浆液的品质，进而进一步提高稀土元素氧化物的分解率。
在本公开的一些实施例中，在所述酸解装置中，所述混合浆液入口和所述第二含氟气体出口分别独立地位于所述酸解装置的上部，所述熟料出口位于所述酸解装置的下部。由此，有利于酸解反应的进行，进而进一步提高稀土元素氧化物的分解率。
本公开的附加方面和优点将在下面的描述中部分给出，部分将从下面的描述中变得明显，或通过本公开的实践了解到。
附图说明
本公开的上述和/或附加的方面和优点从结合下面附图对实施例的描述中将变得明显和容易理解，其中：
图1是根据本公开一个实施例的处理稀土精矿的方法流程示意图；
图2是根据本公开再一个实施例的处理稀土精矿的方法流程示意图；
图3是根据本公开又一个实施例的处理稀土精矿的方法流程示意图；
图4是根据本公开一个实施例的用于实施处理稀土精矿的方法的系统结构示意图；
图5是根据本公开再一个实施例的用于实施处理稀土精矿的方法的系统结构示意图；
图6是根据本公开又一个实施例的用于实施处理稀土精矿的方法的系统结构示意图。
公开详细描述
下面详细描述本公开的实施例，所述实施例的示例在附图中示出，其中自始至终相同或类似的标号表示相同或类似的元件或具有相同或类似功能的元件。下面通过参考附图描述的实施例是示例性的，旨在用于解释本公开，而不能理解为对本公开的限制。
在本公开的描述中，需要理解的是，术语“中心”、“纵向”、“横向”、“长度”、“宽度”、“厚度”、“上”、“下”、“前”、“后”、“左”、“右”、“竖直”、“水平”、“顶”、“底”、“内”、“外”、“顺时针”、“逆时针”、“轴向”、“径向”、“周向”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本公开和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本公开的限制。
此外，术语“第一”、“第二”仅用于描述目的，而不能理解为指示或暗示相对重要性或者隐含指明所指示的技术特征的数量。由此，限定有“第一”、“第二”的特征可以明示或者隐含地包括至少一个该特征。在本公开的描述中，“多个”的含义是至少两个，例如两个，三个等，除非另有明确具体的限定。
在本公开中，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”、“固定”等术语应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或成一体；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通或两个元件的相互作用关系，除非另有明确的限定。对于本领域的普通技术人员而言，可以根据具体情况理解上述术语在本公开中的具体含义。
在本公开中，除非另有明确的规定和限定，第一特征在第二特征“上”或“下”可以是第一和第二特征直接接触，或第一和第二特征通过中间媒介间接接触。而且，第一特征在第二特征“之上”、“上方”和“上面”可是第一特征在第二特征正上方或斜上方，或仅仅表示第一特征水平高度高于第二特征。第一特征在第二特征“之下”、“下方”和“下面”可以是第一特征在第二特征正下方或斜下方，或仅仅表示第一特征水平高度小于第二特征。
在本公开的一个方面，本公开提出了一种处理稀土精矿的方法，根据本公开的实施例，参考图1，该方法包括：
S100：将稀土精矿与浓硫酸进行混合处理
该步骤中，将稀土精矿与浓硫酸进行混合处理，以便得到混合浆液和第一含氟气体。具体的，混料装置内为稀土精矿与浓硫酸的混合，在混合拌酸时，会产生微量的CO 2、HF和SiF 4气体，CO 2、HF来自稀土精矿内的一些碳酸盐类物质与浓硫酸反应，且在第一含氟 气体中还会伴随一些固体粉尘。具体的，将适宜粒径的稀土精矿通过定量给料器和经计量后的浓硫酸按照一定比例加入到混料装置中，搅拌一定时间后，形成混合均匀的混合浆液，期间开启循环冷却水，控制混料装置内的温度在适宜范围内。发明人发现，通过在混料装置中布置搅拌器，可实现浓硫酸与稀土精矿的快速强制混合，使稀土精矿与浓硫酸浸润充分，从而避免在后续酸解过程中出现结团现象，为酸解过程的传质创造了有利的条件，混料装置中的水冷夹套可通过循环水冷却混料装置，使得混料装置内部的温度保持在一定的范围内。需要说明的是，上述稀土精矿可以为氟碳铈稀土矿，也可以为包头混合矿(氟碳铈稀土和独居石)。
根据本公开的一个实施例，稀土精矿的粒径并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，稀土精矿的粒径可以为80-320目。发明人发现，若稀土精矿的粒径太大不利于稀土精矿与浓硫酸的反应，而粒径小虽然能够增加稀土精矿与浓硫酸的接触面积，但反应会过于激烈，使得反应不可控，由此不仅造成磨矿能耗过高，而且还会降低稀土精矿的分解率。由此，采用本公开提出的稀土精矿的粒径可显著提高稀土精矿的分解率，同时节约能耗。
根据本公开的再一个实施例，稀土精矿与浓硫酸的混合质量比并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，稀土精矿与浓硫酸的混合质量比可以为1：(1.2-1.5)。发明人发现，稀土精矿与浓硫酸的混合质量比过低会造成稀土精矿与浓硫酸反应不充分，造成稀土精矿的分解率低，还会造成稀土精矿中的钍较难分解而富集在浸出渣中，形成放射性渣；而若稀土精矿与浓硫酸的混合质量比过高则会导致浓硫酸消耗过多，混料时间延长，且后续工序残酸高。由此，采用本公开提出的稀土精矿与浓硫酸的混合质量比可以进一步提高稀土精矿的分解速率，同时提高混料的速率，节约能耗。
根据本公开的又一个实施例，混合处理的条件并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，混合处理的温度可以不高于30摄氏度，时间可以为5-15min。发明人发现，混合处理的温度过高会使得稀土精矿与浓硫酸提前产生局部反应，混合效果差；混合时间过短达不到稀土精矿与浓硫酸充分接触的条件，影响传质效果。因此，混合处理温度过高、混合时间过长过短都会降低稀土精矿中稀土元素氧化物的分解率。
根据本公开的又一个实施例，浓硫酸的质量浓度并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，浓硫酸的质量浓度可以不低于93wt％。发明人发现，采用该质量浓度的浓硫酸可以显著提高稀土精矿的浸润效率，同时可提高混合浆液的品质，进而提高稀土元素氧化物的分解率。
S200：将混合浆液和引发液混合进行酸解处理
该步骤中，将混合浆液和引发液混合进行酸解处理，以便得到熟料和第二含氟气体。具体的，将上述混合浆液通过混料装置的混合浆液出口加入到酸解装置中，同时打开引发液进液阀门，稀释混合浆液中的浓硫酸放热，并通过辅助加热装置调节酸解装置内的温度，在酸解装置内完成酸解反应，形成散状熟料。发明人发现，在酸解装置内，可完成熟化和焙烧两大工序，显著缩短了稀土精矿酸解反应的时间，且在酸解过程中，内部物料的粘度变化大，由流体态逐渐变为半干状态，最终变为干性，得到熟料，酸解装置可有效应对上述物料特性的变化。酸解装置中的搅拌桨可加速酸解反应的进行，酸解装置外壁上的加热装置可提供酸解反应所需的合适温度，且因整个酸解过程中的温度低，可有效避免浓硫酸分解产生的含硫气体，从而使得产生的第二含氟气体的回收利用成为可能，同时可以有效避免钍进入渣中而造成放射性污染和钍资源的浪费。
根据本公开的一个实施例，酸解处理的条件并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，酸解处理的温度可以为150-300摄氏度，时间可以为1-4h。发明人发现，酸解处理的温度过高会使得浓硫酸分解产生含硫气体，同时也会造成后续熟料中的钍不易浸出进入溶液而留在浸出渣中形成放射性固废；而酸解温度太低和酸解时间过短时均会导致稀土元素氧化物分解率低；酸解时间过长不能进一步提高稀土精矿的分解率，反而增加了能耗，延长了整个工序时间。由此，采用本公开提出的酸解处理的温度和时间可以显著提高稀土精矿的分解率，提高钍的浸出率，同时节约能耗。
根据本公开的再一个实施例，引发液的具体类型并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，引发液可以为选自萃取工序产生的废酸或工业水中的一种。发明人发现，酸解反应需要达到一定温度才进行，利用引发液可使得浓硫酸稀释放热，提高混合浆液的温度，促进酸解反应的进行，这样可以将稀释热利用起来，减少了外部热源的供应。
该过程中，稀土精矿与浓硫酸混合后被加热到一定温度后，精矿中的REO、ThO 2等组分与硫酸反应生成可溶的硫酸盐。CaF 2、Fe 2O 3等也不同程度的反应为硫酸盐。硫酸稀土、硫酸钍、硫酸铁等可溶解于水溶液。氟以HF或SiF 4的形式进入焙烧尾气中，可在水蒸汽存在条件下与氨反应生成固体氟化氢铵(NH 4HF 2)，作为产品出售。同时该过程中(150-300摄氏度)，硫酸不会发生分解，且硫酸蒸发量很小。烟气中仅有HF、SiF 4以及少量的硫酸酸雾，这为以副产品的形式回收烟气中的氟创造了条件。具体的，以稀土精矿为氟碳铈稀土和独居石的混合矿为例，该过程的化学反应如下：
(1)氟碳铈稀土精矿酸解过程主要反应如下：
2REFCO 3+3H 2SO 4＝RE 2(SO 4) 3+2HF↑+2CO 2↑+2H 2O
ThO 2+2H 2SO 4＝Th(SO 4) 2+2H 2O
(2)独居石矿分解：
2REPO 4+3H 2SO 4＝RE 2(SO 4) 3+2H 3PO 4
Th 3(PO 4) 4+6H 2SO 4＝3Th(SO 4) 2+H 3PO 4
其他副反应
CaF 2+H 2SO 4＝CaSO 4+2HF↑
Fe 2O 3+3H 2SO 4＝Fe 2(SO 4) 3+3H 2O
SiO 2+4HF＝SiF 4↑+2H 2O
S300：将熟料和水混合后进行浸出处理
该步骤中，将熟料和水混合后进行浸出处理，以便得到浸出浆液。具体的，酸解装置中的散状熟料经熟料出口通过定量螺旋机送入浸出装置，加入一定比例的水进行浸出反应，反应一段时间后，形成浸出浆液。发明人发现，因酸解过程中稀土精矿中的钍变为钍酸盐，钍酸盐在浸出的时候会进入浸出浆液中，如此，可实现钍资源的回收利用，避免钍的放射性危害。
根据本公开的一个实施例，浸出处理的条件并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，浸出处理的温度可以为常温，时间可以为0.5-1h。发明人发现，浸出温度为常温，无需加热即可将熟料中的硫酸盐溶解于水中，避免外部热源的浪费，同时适宜的浸出时间可保证硫酸盐溶解完全。
根据本公开的再一个实施例，水与熟料的质量比并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，水与熟料的质量比可以为(8-12)：1。发明人发现，水与熟料的质量比过低会造成硫酸盐过饱和而结晶析出，且水与熟料的质量比不宜过大，过大会造成系统物料流通量大，后续废液处理难度大。
S400：将浸出浆液进行固液分离处理，并将浸出渣返回S200进行酸解处理
该步骤中，将浸出浆液进行固液分离处理，以便得到过滤液和浸出渣，并将浸出渣返回S200进行酸解处理。具体的，用泵将浸出装置所得的浸出浆液送至固液分离装置进行固液分离处理，获得过滤液和浸出渣，并将浸出渣定量分批次返回酸解装置中，而过滤液送入下一段萃取工序。由此，可显著提高稀土元素氧化物的分解率，同时提高钍的回收率。
根据本公开实施例的处理稀土精矿的方法和系统通过在混料装置中布置搅拌器，可实现浓硫酸与稀土精矿的快速强制混合，使稀土精矿与浓硫酸浸润充分，从而避免在后续酸解过程中出现结团现象，为酸解过程的传质创造了有利的条件，并且混料装置外壁上的水冷夹套可通过循环水冷却混料装置，使得混料装置内部的温度保持在一定的范围内，如此， 可有效避免高温下稀土矿的分解，从而可以实现钍资源的回收；同时，本申请中在酸解装置中即可实现熟化和焙烧两大工序，从而显著缩短了稀土精矿酸解反应的时间，且在酸解过程中，内部物料的粘度变化大，由流体态逐渐变为半干状态，最终变为干性，得到熟料，酸解装置可有效应对上述物料特性的变化。并且酸解装置中的搅拌桨可加速酸解反应的进行，酸解装置外壁上的加热装置可提供酸解反应所需的合适温度，且因整个酸解过程中的温度低，可以进一步避免钍进入渣中而造成放射性污染和钍资源的浪费，并且可有效避免浓硫酸分解产生的含硫气体，从而使得产生的第二含氟气体的回收利用成为可能；酸解过程中稀土精矿中的钍变为钍酸盐，钍酸盐在浸出的时候会进入浸出浆液中，如此，可实现钍资源的回收利用，避免钍的放射性危害；浸出浆液经固液分离后所得的浸出渣可继续返回至酸解装置中进行酸解处理，可进一步提高钍的回收率和REO的分解率。由此，该方法原料适应性广、能耗低，且可实现连续化生产，同时可有效回收钍资源，并显著提高稀土精矿的分解率，REO分解率可达96％。
另外，根据本公开的实施例，参考图2，在将稀土精矿与浓硫酸混合处理之前进一步包括：
S500：将稀土精矿进行球磨处理
该步骤中，将稀土精矿进行球磨处理，以便得到稀土精矿颗粒。由此，有利于提高稀土元素氧化物的分解率。
S600：将稀土精矿颗粒进行筛分处理，并将筛上料返回进行球磨处理，将筛下料与浓硫酸进行混合处理
该步骤中，将上述得到的稀土精矿颗粒进行筛分处理，以便得到筛上料和筛下料，并将筛上料返回进行球磨处理，将筛下料与浓硫酸进行混合处理。由此，可进一步提高稀土元素氧化物的分解率。发明人发现，通过将筛分之后粒径不合格的筛上料返回至球磨装置中进行球磨处理，可显著节约本工艺的原材料成本和时间成本，将经筛分之后得到的筛下料送至混料装置中与浓硫酸进行混合可进一步提高稀土元素氧化物的分解率。具体的，筛下料的粒径可以为80-320目。
根据本公开的实施例，参考图3，上述处理稀土精矿的方法和系统进一步包括：
S700：将第一含氟气体和第二含氟气体在喷淋液的作用下进行喷淋处理
该步骤中，将第一含氟气体和第二含氟气体在喷淋液的作用下进行喷淋处理，以便得到含氟浆液。由此，可实现含氟气体的回收利用，避免尾气污染环境的问题。发明人发现，因混料装置和酸解装置都有温控装置，显著降低了第一含氟气体和第二含氟气体中的杂质含量，使得第一含氟气体和第二含氟气体中的粉尘含量少，因此，含氟气体在进行喷淋处理前可无需设置除尘装置而直接采用喷淋液喷淋处理，含氟气体和其中的粉尘会溶于喷淋 液中，经过滤后，滤渣可返回至酸解装置循环使用，滤液可用于制备氟盐。有利于实现含氟气体的回收和利用，避免尾气污染环境的问题。
根据本公开的一个实施例，喷淋液的具体类型并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，喷淋液可以为选自水和碱液中的至少之一，其中，碱液可以为氨水。由此，有利于实现含氟气体的回收和利用，避免尾气污染环境的问题。
在本公开的再一个方面，本公开提出了一种用于实施上述处理稀土精矿的方法的系统，根据本公开的实施例，参考图4，该系统包括：混料装置100、酸解装置200、浸出装置300和固液分离装置400。
根据本公开的实施例，混料装置100具有稀土精矿入口101、浓硫酸入口102、混合浆液出口103和第一含氟气体出口104，并且混料装置内布置有搅拌器11，混料装置外壁上布置有水冷夹套12，且适于将稀土精矿与浓硫酸进行混合处理，以便得到混合浆液和第一含氟气体。具体的，混料装置内为稀土精矿与浓硫酸的混合，在混合拌酸时，会产生微量的CO 2、HF和SiF 4气体，CO 2、HF来自稀土精矿内的一些碳酸盐类物质与浓硫酸反应，且在第一含氟气体中还会伴随一些固体粉尘。具体的，将适宜粒径的稀土精矿通过定量给料器和经计量后的浓硫酸按照一定比例加入到混料装置中，搅拌一定时间后，形成混合均匀的混合浆液，期间开启循环冷却水，控制混料装置内的温度在一定范围内。发明人发现，通过在混料装置中布置搅拌器，可实现浓硫酸与稀土精矿的快速强制混合，使稀土精矿与浓硫酸浸润充分，从而避免在后续酸解过程中出现结团现象，为酸解过程的传质创造了有利的条件，混料装置中的水冷夹套可通过循环水冷却混料装置，使得混料装置内部的温度保持在一定范围内。需要说明的是，上述稀土精矿并不受特别限制，例如可以为氟碳铈稀土矿，也可以为包头混合矿(氟碳铈稀土和独居石)；上述浓硫酸可通过计量泵送至混料装置中；混料装置内的搅拌器并不受特别限制，本领域技术人员可以根据实际需要进行选择，例如可以为双层搅拌桨，即分上下两层布置在搅拌轴上，可用于稀土精矿与浓硫酸的强烈混合。
根据本公开的一个实施例，在混料装置100中，稀土精矿入口101、浓硫酸入口102、和第一含氟气体出口104分别独立地位于搅拌器11上部，混合浆液出口103位于搅拌器11的下部。由此，有利于稀土精矿与浓硫酸反应的顺行，并提高整个工艺的效率。
根据本公开的再一个实施例，稀土精矿的粒径并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，稀土精矿的粒径可以为80-320目。发明人发现，若稀土精矿的粒径太大不利于稀土精矿与浓硫酸的反应，而粒径小虽然能够增加稀土精矿与浓硫酸的接触面积，但反应会过于激烈，使得反应不可控，由此不仅 造成磨矿能耗过高，而且还会降低稀土精矿的分解率。由此，采用本公开提出的稀土精矿的粒径可显著提高稀土精矿的分解率，同时节约能耗。
根据本公开的又一个实施例，稀土精矿与浓硫酸的混合质量比并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，稀土精矿与浓硫酸的混合质量比可以为1：(1.2-1.5)。发明人发现，稀土精矿与浓硫酸的混合质量比过低会造成稀土精矿与浓硫酸反应不充分，造成稀土精矿的分解率低，还会造成稀土精矿中的钍较难分解而富集在浸出渣中，形成放射性渣；而若稀土精矿与浓硫酸的混合质量比过高则会导致浓硫酸消耗过多，混料时间延长，且后续工序残酸高。由此，采用本公开提出的稀土精矿与浓硫酸的混合质量比可以进一步提高稀土精矿的分解速率，同时提高混料的速率，节约能耗。
根据本公开的又一个实施例，混合处理的条件并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，混合处理的温度可以不高于30摄氏度，时间可以为5-15min。发明人发现，混合处理的温度过高会使得稀土精矿与浓硫酸提前产生局部反应，混合效果差；混合时间过短达不到稀土精矿与浓硫酸充分接触的条件，影响传质效果。因此，混合处理温度过高、混合时间过长过短都会降低稀土精矿中稀土元素氧化物的分解率。
根据本公开的又一个实施例，浓硫酸的质量浓度并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，浓硫酸的质量浓度可以不低于93wt％。发明人发现，采用该质量浓度的浓硫酸可以显著提高稀土精矿的浸润效率，同时可提高混合浆液的品质，进而提高稀土元素氧化物的分解率。
根据本公开的实施例，酸解装置200具有混合浆液入口201、引发液入口202、熟料出口203和第二含氟气体出口204，混合浆液入口201与混合浆液出口103相连，并且酸解装置200内布置有搅拌桨21，酸解装置外壁上布置有加热装置22，且适于将混合浆液和引发液混合进行酸解处理，以便得到熟料和第二含氟气体。具体的，将上述混合浆液通过混料装置的混合浆液出口加入到酸解装置中，同时打开引发液进液阀门，稀释混合浆液中的浓硫酸放热，并通过辅助加热装置调节酸解装置内的温度，在酸解装置内完成酸解反应，形成散状熟料。发明人发现，在酸解装置内，可完成熟化和焙烧两大工序，显著缩短了稀土精矿酸解反应的时间，且在酸解过程中，内部物料的粘度变化大，由流体态逐渐变为半干状态，最终变为干性，得到熟料，酸解装置可有效应对上述物料特性的变化。酸解装置中的搅拌桨可加速酸解反应的进行，酸解装置外壁上的加热装置可提供酸解反应所需的合适温度，且因整个酸解过程中的温度低，可有效避免浓硫酸分解产生的含硫气体，从而使得产生的第二含氟气体的回收利用成为可能，同时可以有效避免钍进入渣中而造成放射性污 染和钍资源的浪费。需要说明的是，上述酸解装置并不受特别限制，本领域技术人员可以根据实际需要进行选择，例如可以为卧式反应器，搅拌桨可以为螺旋型并排相切排列的搅拌桨，加热装置的加热方式可以为电加热或者蒸汽加热。
根据本公开的一个实施例，在酸解装置200中，混合浆液入口201和第二含氟气体出口204分别独立地位于酸解装置200的上部，熟料出口203位于酸解装置200的下部。由此，有利于酸解装置内的酸解反应的顺行，并提高整个工艺的效率。
根据本公开的再一个实施例，酸解处理的条件并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，酸解处理的温度可以为150-300摄氏度，时间可以为1-4h。发明人发现，酸解处理的温度过高会使得浓硫酸分解产生含硫气体，同时也会造成后续熟料中的钍不易浸出进入溶液而留在浸出渣中形成放射性固废；而酸解温度太低和酸解时间过短时均会导致稀土元素氧化物分解率低；酸解时间过长不能进一步提高稀土精矿的分解率，反而增加了能耗，延长了整个工序时间。由此，采用本公开提出的酸解处理的温度和时间可以显著提高稀土精矿的分解率，提高钍的浸出率，同时节约能耗。
根据本公开的又一个实施例，引发液的具体类型并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，引发液可以为选自萃取工序产生的废酸或工业水中的一种。发明人发现，酸解反应需要达到一定温度才进行，利用引发液可使得浓硫酸稀释放热，提高混合浆液的温度，促进酸解反应的进行，这样可以将稀释热利用起来，减少了外部热源的供应。
该过程中，稀土精矿与浓硫酸混合后被加热到一定温度后，精矿中的REO、ThO 2等组分与硫酸反应生成可溶的硫酸盐。CaF 2、Fe 2O 3等也不同程度的反应为硫酸盐。硫酸稀土、硫酸钍、硫酸铁等可溶解于水溶液。氟以HF或SiF 4的形式进入焙烧尾气中，可在水蒸汽存在条件下与氨反应生成固体氟化氢铵(NH 4HF 2)，作为产品出售。同时该过程中(150-300摄氏度)，硫酸不会发生分解，且硫酸蒸发量很小。烟气中仅有HF、SiF 4以及少量的硫酸酸雾，这为以副产品的形式回收烟气中的氟创造了条件。
(1)氟碳铈稀土精矿酸解过程主要反应如下：
2REFCO 3+3H 2SO 4＝RE 2(SO 4) 3+2HF↑+2CO 2↑+2H 2O
ThO 2+2H 2SO 4＝Th(SO 4) 2+2H 2O
(2)独居石矿分解：
2REPO 4+3H 2SO 4＝RE 2(SO 4) 3+2H 3PO 4
Th 3(PO 4) 4+6H 2SO 4＝3Th(SO 4) 2+H 3PO 4
其他副反应
CaF 2+H 2SO 4＝CaSO 4+2HF↑
Fe 2O 3+3H 2SO 4＝Fe 2(SO 4) 3+3H 2O
SiO 2+4HF＝SiF 4↑+2H 2O
根据本公开的实施例，浸出装置300具有熟料入口301、水入口302和浸出浆液出口303，熟料入口301与熟料出口203相连，且适于将熟料和水混合后进行浸出处理，以便得到浸出浆液。具体的，酸解装置中的散状熟料经熟料出口通过定量螺旋机送入浸出装置，加入一定比例的水进行浸出反应，反应一段时间后，形成浸出浆液。发明人发现，因酸解过程中稀土精矿中的钍变为钍酸盐，钍酸盐在浸出的时候会进入浸出浆液中，如此，可实现钍资源的回收利用，避免钍的放射性危害。
根据本公开的一个实施例，浸出处理的条件并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，浸出处理的温度可以为常温，时间可以为0.5-1h。发明人发现，浸出温度为常温，无需加热即可将熟料中的硫酸盐溶解于水中，避免外部热源的浪费，同时适宜的浸出时间可保证硫酸盐溶解完全。
根据本公开的再一个实施例，水与熟料的质量比并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，水与熟料的质量比可以为(8-12)：1。发明人发现，水与熟料的质量比过低会造成硫酸盐过饱和而结晶析出，且水与熟料的质量比不宜过大，过大会造成系统物料流通量大，后续废液处理难度大。
根据本公开的实施例，固液分离装置400具有浸出浆液入口401、过滤液出口402和浸出渣出口403，浸出浆液入口401与浸出浆液出口303相连，浸出渣出口403与酸解装置200相连，且适于将浸出浆液进行固液分离处理，以便得到过滤液和浸出渣，并将浸出渣返回至酸解装置进行酸解处理。具体的，用泵将浸出装置所得的浸出浆液送至固液分离装置进行固液分离处理，获得过滤液和浸出渣，并将浸出渣定量分批次返回酸解装置中，而过滤液送入下一段萃取工序。由此，可显著提高稀土元素氧化物的分解率，同时提高钍的回收率。
根据本公开实施例的处理稀土精矿的系统通过在混料装置中布置搅拌器，可实现浓硫酸与稀土精矿的快速强制混合，使稀土精矿与浓硫酸浸润充分，从而避免在后续酸解过程中出现结团现象，为酸解过程的传质创造了有利的条件，并且混料装置外壁上的水冷夹套可通过循环水冷却混料装置，使得混料装置内部的温度保持在一定的范围内，如此，可有效避免高温下稀土矿的分解，从而可以实现钍资源的回收；同时，本申请中在酸解装置中即可实现熟化和焙烧两大工序，从而显著缩短了稀土精矿酸解反应的时间，且在酸解过程中，内部物料的粘度变化大，由流体态逐渐变为半干状态，最终变为干性，得到熟料，酸解装置可有效应对上述物料特性的变化。并且酸解装置中的搅拌桨可加速酸解反应的进行， 酸解装置外壁上的加热装置可提供酸解反应所需的合适温度，且因整个酸解过程中的温度低，可以进一步避免钍进入渣中而造成放射性污染和钍资源的浪费，并且可有效避免浓硫酸分解产生的含硫气体，从而使得产生的第二含氟气体的回收利用成为可能；酸解过程中稀土精矿中的钍变为钍酸盐，钍酸盐在浸出的时候会进入浸出浆液中，如此，可实现钍资源的回收利用，避免钍的放射性危害；浸出浆液经固液分离后所得的浸出渣可继续返回至酸解装置中进行酸解处理，可进一步提高钍的回收率和REO的分解率。由此，该系统原料适应性广、能耗低，且可实现连续化生产，同时可有效回收钍资源，并显著提高稀土精矿的分解率，REO分解率可达96％。
另外，根据本公开的实施例，参考图5，上述处理稀土精矿的系统进一步包括：球磨装置500和筛分装置600。
根据本公开的实施例，球磨装置500具有稀土精矿进口501和稀土精矿颗粒出口502，且适于在将稀土精矿与浓硫酸混合之前，预先对稀土精矿进行球磨处理，以便得到稀土精矿颗粒。由此，有利于提高稀土元素氧化物的分解率。
根据本公开的实施例，筛分装置600具有稀土精矿颗粒入口601、筛上料出口602和筛下料出口603，稀土精矿颗粒入口601与稀土精矿颗粒出口502相连，筛上料出口602与球磨装置500相连，筛下料出口603与稀土精矿入口101相连，且适于将上述得到的稀土精矿颗粒进行筛分处理，以便得到筛上料和筛下料，并将筛上料返回进行球磨处理，将筛下料与浓硫酸进行混合处理。发明人发现，通过将筛分之后粒径不合格的筛上料返回至球磨装置中进行球磨处理，可显著节约本工艺的原材料成本和时间成本，将经筛分之后得到的筛下料送至混料装置中与浓硫酸进行混合可进一步提高稀土元素氧化物的分解率。需要说明的是，筛分装置的筛下料出口可以通过计量装置与上述混料装置的稀土精矿入口相连。具体的，筛下料的粒径可以为80-320目。
根据本公开的实施例，参考图6，上述处理稀土精矿的系统进一步包括：尾气处理装置700。
根据本公开的实施例，尾气处理装置700具有含氟气体入口701、喷淋液入口702含氟浆液出口703，含氟气体入口701分别与第一含氟气体出口104和第二含氟气体出口204相连，且适于将第一含氟气体和第二含氟气体在喷淋液的作用下进行喷淋处理，以便得到含氟浆液。发明人发现，因混料装置和酸解装置都有温控装置，显著降低了第一含氟气体和第二含氟气体中的杂质含量，使得第一含氟气体和第二含氟气体中的粉尘含量少，因此，含氟气体在进行喷淋处理前可无需设置除尘装置而直接采用喷淋液喷淋处理，含氟气体和其中的粉尘会溶于喷淋液中，经过滤后，滤渣可返回至酸解装置循环使用，滤液可用于制备氟盐，有利于实现含氟气体的回收和利用，避免尾气污染环境的问题。
根据本公开的一个实施例，喷淋液的具体类型并不受特别限制，本领域的技术人员可以根据实际需要进行选择，根据本公开的一个具体实施例，喷淋液可以为选自水和碱液中的至少之一，其中，碱液可以为氨水。由此，有利于实现含氟气体的回收和利用，避免尾气污染环境的问题。
下面参考具体实施例，对本公开进行描述，需要说明的是，这些实施例仅仅是描述性的，而不以任何方式限制本公开。
实施例1
将氟碳铈稀土矿经球磨装置球磨，筛分装置筛分后，获得粒径为80-320目的氟碳铈稀土精矿颗粒；氟碳铈稀颗粒土精矿经计量后放入事先计量好盛有98wt％浓硫酸的混料装置中，浓硫酸与氟碳铈稀土精矿颗粒的质量比为1.4：1，开启混料装置的循环冷却水，控制混料装置内的温度小于30摄氏度，充分搅拌10min，形成拌酸均匀的混合浆液，同时产生第一含氟气体；再将混合浆液经混料装置的混合浆液出口排出，加入到酸解装置中，打开引发液(工业水)进液阀门，稀释混合浆液中的浓硫酸，放出热量，并通过酸解装置的辅助加热装置，调节酸解装置内的温度，在120摄氏度下搅拌30min，紧接着在250摄氏度下酸解1h，形成散状熟料，同时产生第二含氟气体；散状熟料经酸解装置的熟料出口定量送入浸出装置，在浸出装置中，水与熟料按照质量比8：1经计量后放入浸出槽，机械搅拌1h，形成浸出浆液，再将浸出浆液泵送至板框压滤机压滤，获得过滤液和浸出渣，浸出渣渣率为8wt％，分析浸出渣化学成分，将上浸出渣定量分批次返回酸解装置，而浸出液送入下一段萃取工序。
本实施例的稀土REO(稀土元素氧化物)分解率为95.18％，第一含氟气体和第二含氟气体经尾气吸收塔回收利用氟资源。
实施例2
将氟碳铈稀土矿经球磨装置球磨，筛分装置筛分后，获得粒径为80-320目的氟碳铈稀土精矿颗粒；氟碳铈稀土精矿颗粒经计量后放入事先计量好盛有98wt％浓硫酸的混料装置中，浓硫酸与氟碳铈稀土精矿颗粒的质量比为1.5：1，开启混料装置的循环冷却水，控制混料装置内的温度小于30摄氏度，充分搅拌8min，形成拌酸均匀的混合浆液，同时产生第一含氟气体；再将混合浆液经混料装置的混合浆液出口排出，加入到酸解装置中，打开引发液(废酸)进液阀门，稀释混合浆液中的浓硫酸，放出热量，并通过酸解装置的辅助加热装置，调节酸解装置内的温度，在130摄氏度下搅拌30min，紧接着在280摄氏度下酸解1h，形成散状熟料，同时产生第二含氟气体；散状熟料经酸解装置的熟料出口定量送入浸出装置，在浸出装置中，水与熟料按照质量比10：1经计量后放入浸出槽，机械搅拌0.5h， 形成浸出浆液，再将浸出浆液泵送至板框压滤机压滤，获得过滤液和浸出渣，浸出渣渣率为6.3wt％，分析浸出渣化学成分，将上浸出渣定量分批次返回酸解装置，而浸出液送入下一段萃取工序。
本实施例的稀土REO(稀土元素氧化物)分解率为96％，第一含氟气体和第二含氟气体经尾气吸收塔回收利用氟资源。
实施例3
将粒径为80-320目的含有氟碳铈稀土矿和独居石的混合矿经计量后放入事先计量好盛有98wt％浓硫酸的混料装置中，浓硫酸与混合矿的质量比为1.5：1，开启混料装置的循环冷却水，控制混料装置内的温度小于30摄氏度，充分搅拌10min，形成拌酸均匀的混合浆液，同时产生第一含氟气体；再将混合浆液经混料装置的混合浆液出口排出，加入到酸解装置中，打开引发液(含有工业水和废酸的混合液)进液阀门，稀释混合浆液中的浓硫酸，放出热量，并通过酸解装置的辅助加热装置，调节酸解装置内的温度，在85摄氏度下搅拌30min，紧接着在280摄氏度下酸解2h，形成散状熟料，同时产生第二含氟气体；散状熟料经酸解装置的熟料出口定量送入浸出装置，在浸出装置中，水与熟料按照质量比12：1经计量后放入浸出槽，机械搅拌1h，形成浸出浆液，再将浸出浆液泵送至板框压滤机压滤，获得过滤液和浸出渣，浸出渣渣率为6.8wt％，分析浸出渣化学成分，将上浸出渣定量分批次返回酸解装置，而浸出液送入下一段萃取工序。
本实施例的稀土REO(稀土元素氧化物)分解率为96％，第一含氟气体和第二含氟气体经尾气吸收塔回收利用氟资源。
实施例4
将粒径为80-320目的含有氟碳铈稀土矿和独居石的混合矿经计量后放入事先计量好盛有98wt％浓硫酸的混料装置中，浓硫酸与混合矿的质量比为1.4：1，开启混料装置的循环冷却水，控制混料装置内的温度小于30摄氏度，充分搅拌15min，形成拌酸均匀的混合浆液，同时产生第一含氟气体；再将混合浆液经混料装置的混合浆液出口排出，加入到酸解装置中，打开引发液(工业水)进液阀门，稀释混合浆液中的浓硫酸，放出热量，并通过酸解装置的辅助加热装置，调节酸解装置内的温度，在100摄氏度下搅拌30min，紧接着在280摄氏度下酸解2h，形成散状熟料，同时产生第二含氟气体；散状熟料经酸解装置的熟料出口定量送入浸出装置，在浸出装置中，水与熟料按照质量比10：1经计量后放入浸出槽，机械搅拌1h，形成浸出浆液，再将浸出浆液泵送至板框压滤机压滤，获得过滤液和浸出渣，浸出渣渣率为7.2wt％，分析浸出渣化学成分，将上浸出渣定量分批次返回酸解装置，而浸出液送入下一段萃取工序。
本实施例的稀土REO(稀土元素氧化物)分解率为96％，第一含氟气体和第二含氟气 体经尾气吸收塔回收利用氟资源。
以上详细描述了本公开的优选实施方式，但是，本公开并不限于上述实施方式中的具体细节，在本公开的技术构思范围内，可以对本公开的技术方案进行多种简单变型，这些简单变型均属于本公开的保护范围。
另外需要说明的是，在上述具体实施方式中所描述的各个具体技术特征，在不矛盾的情况下，可以通过任何合适的方式进行组合，为了避免不必要的重复，本公开对各种可能的组合方式不再另行说明。
此外，本公开的各种不同的实施方式之间也可以进行任意组合，只要其不违背本公开的思想，其同样应当视为本公开所公开的内容。
在本说明书的描述中，参考术语“一个实施例”、“一些实施例”、“示例”、“具体示例”、或“一些示例”等的描述意指结合该实施例或示例描述的具体特征、结构、材料或者特点包含于本公开的至少一个实施例或示例中。在本说明书中，对上述术语的示意性表述不必须针对的是相同的实施例或示例。而且，描述的具体特征、结构、材料或者特点可以在任一个或多个实施例或示例中以合适的方式结合。此外，在不相互矛盾的情况下，本领域的技术人员可以将本说明书中描述的不同实施例或示例以及不同实施例或示例的特征进行结合和组合。
尽管上面已经示出和描述了本公开的实施例，可以理解的是，上述实施例是示例性的，不能理解为对本公开的限制，本领域的普通技术人员在本公开的范围内可以对上述实施例进行变化、修改、替换和变型。

Claims (17)

  1. 一种处理稀土精矿的方法，其中，包括：
    (1)将稀土精矿与浓硫酸进行混合处理，以便得到混合浆液和第一含氟气体；
    (2)将所述混合浆液和引发液混合进行酸解处理，以便得到熟料和第二含氟气体；
    (3)将所述熟料和水混合后进行浸出处理，以便得到浸出浆液；
    (4)将所述浸出浆液进行固液分离处理，以便得到过滤液和浸出渣，并将所述浸出渣返回步骤(2)进行所述酸解处理。
  2. 根据权利要求1所述的方法，其中，在将所述稀土精矿与浓硫酸混合处理之前进一步包括：
    (5)将所述稀土精矿进行球磨处理，以便得到稀土精矿颗粒；
    (6)将所述稀土精矿颗粒进行筛分处理，以便得到筛上料和筛下料，并将所述筛上料返回进行所述球磨处理，将所述筛下料与所述浓硫酸进行混合处理。
  3. 根据权利要求1或2所述的方法，其中，进一步包括：
    (7)将所述第一含氟气体和所述第二含氟气体在喷淋液的作用下进行喷淋处理，以便得到含氟浆液。
  4. 根据权利要求1-3任一项所述的方法，其中，在步骤(1)中，所述稀土精矿的粒径为80-320目。
  5. 根据权利要求1-4任一项所述的方法，其中，在步骤(1)中，所述稀土精矿与所述浓硫酸的混合质量比为1：(1.2-1.5)。
  6. 根据权利要求1-5任一项所述的方法，其中，在步骤(1)中，所述混合处理的温度不高于30摄氏度，时间为5-15min。
  7. 根据权利要求1-6任一项所述的方法，其中，在步骤(1)中，所述浓硫酸的质量浓度不低于93wt％。
  8. 根据权利要求1-7任一项所述的方法，其中，在步骤(2)中，所述酸解处理的温度为150-300摄氏度，时间为1-4h。
  9. 根据权利要求1-8任一项所述的方法，其中，在步骤(2)中，所述引发液为选自工业水或后续工序中的过滤液中的至少之一。
  10. 根据权利要求1-9任一项所述的方法，其中，在步骤(3)中，所述浸出处理的时间为0.5-1h。
  11. 根据权利要求1-10任一项所述的方法，其中，在步骤(3)中，所述水与所述熟料的质量比为(8-12)：1。
  12. 根据权利要求1-11任一项所述的方法，其中，在步骤(7)中，所述喷淋液为选自水和碱液中的至少之一。
  13. 一种用于实施权利要求1-12任一项所述的处理稀土精矿的方法的系统，其中，包括：
    混料装置，所述混料装置具有稀土精矿入口、浓硫酸入口、混合浆液出口和第一含氟气体出口，并且所述混料装置内布置有搅拌器，所述混料装置外壁上布置有水冷夹套；
    酸解装置，所述酸解装置具有混合浆液入口、引发液入口、熟料出口和第二含氟气体出口，所述混合浆液入口与所述混合浆液出口相连，并且所述酸解装置内布置有搅拌桨，所述酸解装置外壁上布置有加热装置；
    浸出装置，所述浸出装置具有熟料入口、水入口和浸出浆液出口，所述熟料入口与所述熟料出口相连；
    固液分离装置，所述固液分离装置具有浸出浆液入口、过滤液出口和浸出渣出口，所述浸出浆液入口与所述浸出浆液出口相连，所述浸出渣出口与所述酸解装置相连。
  14. 根据权利要求13所述的系统，其中，进一步包括：
    球磨装置，所述球磨装置具有稀土精矿进口和稀土精矿颗粒出口；
    筛分装置，所述筛分装置具有稀土精矿颗粒入口、筛上料出口和筛下料出口，所述稀土精矿颗粒入口与所述稀土精矿颗粒出口相连，所述筛上料出口与所述球磨装置相连，所述筛下料出口与所述稀土精矿入口相连。
  15. 根据权利要求13或14所述的系统，其中，进一步包括：
    尾气处理装置，所述尾气处理装置具有含氟气体入口、喷淋液入口和含氟浆液出口，所述含氟气体入口分别与所述第一含氟气体出口和所述第二含氟气体出口相连。
  16. 根据权利要求13-15任一项所述的系统，其中，在所述混料装置中，所述稀土精矿入口、所述浓硫酸入口和所述第一含氟气体出口分别独立地位于所述搅拌器上部，所述混合浆液出口位于所述搅拌器的下部。
  17. 根据权利要求13-16任一项所述的系统，其中，在所述酸解装置中，所述混合浆液入口和所述第二含氟气体出口分别独立地位于所述酸解装置的上部，所述熟料出口位于所述酸解装置的下部。
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