WO2021140840A1 - 塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システム - Google Patents
塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システム Download PDFInfo
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- WO2021140840A1 WO2021140840A1 PCT/JP2020/046592 JP2020046592W WO2021140840A1 WO 2021140840 A1 WO2021140840 A1 WO 2021140840A1 JP 2020046592 W JP2020046592 W JP 2020046592W WO 2021140840 A1 WO2021140840 A1 WO 2021140840A1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/26—Magnesium halides
- C01F5/30—Chlorides
- C01F5/34—Dehydrating magnesium chloride containing water of crystallisation
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
- C25C3/04—Electrolytic production, recovery or refining of metals by electrolysis of melts of magnesium
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/26—Magnesium halides
- C01F5/30—Chlorides
- C01F5/32—Preparation of anhydrous magnesium chloride by chlorinating magnesium compounds
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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
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/20—Obtaining alkaline earth metals or magnesium
- C22B26/22—Obtaining magnesium
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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
- 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
- C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
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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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present disclosure relates to a magnesium chloride aqueous solution production system and a magnesium production system.
- This disclosure claims priority based on Japanese Patent Application No. 2020-001483 filed on January 08, 2020, the contents of which are incorporated herein by reference.
- a method called the Dow method is known as a method for recovering magnesium dissolved in seawater.
- alkali is first added to seawater to obtain magnesium hydroxide (Mg (OH) 2).
- hydrochloric acid is added to the obtained Mg (OH) 2 to obtain magnesium chloride (MgCl 2).
- MgCl 2 is subjected to melt salt electrolysis to obtain metallic magnesium (see, for example, Non-Patent Document 1).
- the magnesium chloride aqueous solution production system includes a crystallization part, a settling part connected to the crystallization part, a removing part connected to the settling part, and the removal.
- the crystallization section includes an acid-alkali generation section connected to the section and a reaction section connected to the sedimentation section, and the crystallization section is made by adding an aqueous sodium hydroxide solution to water to be treated using seawater as a raw material and magnesium hydroxide.
- the sedimentation portion stores the reaction slurry and precipitates the particles, and a recovery slurry containing the particles at a high concentration.
- a first connecting part that connects the main body part and the crystallization part that produces an aqueous solution and hydrochloric acid, and supplies the sodium hydroxide aqueous solution to the crystallization part, and the main body part and the reaction. It has a second connecting part that connects the parts and supplies the hydrochloric acid to the reaction part.
- FIG. 1 is a schematic view showing a magnesium chloride aqueous solution production system and a magnesium production system according to the first embodiment of the present disclosure.
- FIG. 2 is an explanatory diagram of a magnesium chloride aqueous solution production system and a magnesium production system according to the second embodiment of the present disclosure.
- FIG. 3 is an explanatory diagram of a magnesium chloride aqueous solution production system and a magnesium production system according to the third embodiment of the present disclosure.
- FIG. 1 is a schematic view showing a magnesium chloride aqueous solution production system 1 and a magnesium chloride production system 100 according to the first embodiment of the present disclosure.
- the magnesium chloride aqueous solution production system 1 includes a crystallization unit 10, a sedimentation unit 20, a removal unit 30, an acid-alkali generation unit 40, a reaction unit 50, and a pretreatment unit 60.
- the pretreatment section 60 is connected to the crystallization section 10 on the upstream side of the crystallization section 10.
- the water to be treated L1 supplied to the crystallization unit 10 is treated in advance and adjusted to a state suitable for the treatment after the crystallization unit 10.
- the pretreatment section 60 has a decarboxylation section 61 that removes at least a part of carbonic acid dissolved in the water to be treated L1.
- the water to be treated includes not only seawater but also concentrated seawater that is concentrated by removing water from the seawater.
- the concentrated seawater corresponds to, for example, a concentrated liquid produced by treating seawater with a reverse osmosis membrane and separating the water.
- the water to be treated includes a liquid obtained by decarboxylating seawater or concentrated seawater to reduce carbonation.
- the decarboxylation unit 61 can adopt a known configuration.
- the decarboxylation unit 61 includes a decarboxylation tower that removes carbon dioxide contained in the water to be treated L1 by adding hydrochloric acid (HCl aq.) To the water to be treated L1 and then aerating the water to be treated L1. be able to.
- HCl aq. hydrochloric acid
- the pipe P1 and the pipe P61 are connected to the decarboxylation unit 61.
- Water L1 to be treated is supplied to the decarboxylation section 61 via the pipe P1. Further, the water to be treated (water to be treated L61) decarboxylated by the decarboxylation section 61 is supplied to the crystallization section 10 via the pipe P61.
- the crystallization unit 10 is an apparatus for crystallizing Mg (OH) 2 by adding an aqueous sodium hydroxide solution (NaOH aq.) To water L61 to be treated.
- the water to be treated L61 is supplied to the crystallization section 10 via the pipe P61.
- the reaction slurry L2 in which the particles of Mg (OH) 2 are dispersed is generated.
- the settling portion 20 is connected to the crystallization portion 10 via the pipe P2.
- the reaction slurry L2 generated in the crystallization section 10 is supplied to the settling section 20 via the pipe P2.
- a settling tank that stores the reaction slurry L2 and setstles Mg (OH) 2 particles can be adopted.
- the sedimentation section 20 separates the reaction slurry L2 into a recovery slurry S containing Mg (OH) 2 particles at a high concentration and a separation liquid L3 containing Mg (OH) 2 particles at a low concentration. A large amount of calcium ions (Ca 2+ ) remain in the separation liquid L3.
- reaction section 50 is connected to the settling section 20 via the pipe P31.
- the recovered slurry S generated in the settling section 20 is supplied to the reaction section 50 via the pipe P31.
- the reaction unit 50 adds hydrochloric acid to the recovered slurry S to generate an aqueous magnesium chloride solution.
- the removing portion 30 is connected to the settling portion 20 via the pipe P32.
- the separation liquid L3 generated in the settling section 20 is supplied to the removing section 30 via the pipe P32.
- the removing unit 30 removes at least a part of the divalent cations contained in the separation liquid L3 to generate a reaction liquid L4 having a reduced divalent cation concentration.
- a typical example of the divalent cation removed from the separation liquid L3 is calcium ion.
- a known electrodialysis tank capable of selectively removing divalent cations can be adopted.
- the removing unit 30 may be a nanofiltration membrane that separates divalent cations.
- the removing unit 30 may be a reaction tank for adding sulfate ions to the separation liquid L3.
- the separated liquid L3 adding sulfuric acid ion, Ca 2+ and SO 4 2-and reacts, CaSO 4 is precipitated occur.
- the calcium ion concentration in the separation liquid L3 can be reduced.
- the acid-alkali generation unit 40 is connected to the removal unit 30 via the pipe P4.
- the reaction solution L4 generated in the removing unit 30 is supplied to the acid-alkali generating unit 40 via the pipe P4.
- the acid-alkali generation unit 40 has a main body unit 40A, a first connection unit 41, a second connection unit 42, and a third connection unit 43.
- the main body 40A produces an aqueous sodium hydroxide solution and hydrochloric acid from the reaction solution L4.
- a known bipolar film or an electrolyzer can be adopted for the main body 40A.
- hydrochloric acid and sodium hydroxide aqueous solution are produced based on the following reaction formula. NaCl + H 2 O ⁇ NaOH + 1 / 2H 2 + 1 / 2Cl 2 H 2 + Cl 2 ⁇ 2 HCl
- the first connection portion 41 includes a pipe P100, a storage tank 401, and a supply device 411.
- the pipe P100 connects the main body portion 40A and the crystallization portion 10.
- the storage tank 401 stores the sodium hydroxide aqueous solution produced in the main body 40A.
- the supply device 411 supplies the sodium hydroxide aqueous solution stored in the storage tank 401 to the crystallization unit 10.
- the second connection portion 42 has a pipe P40, a storage tank 402, a pipe P200, and a supply device 421.
- the pipe P40 connects the main body 40A and the storage tank 402.
- the storage tank 402 stores the hydrochloric acid produced in the main body 40A.
- the pipe P200 connects the storage tank 402 and the reaction unit 50.
- the supply device 421 supplies the hydrochloric acid stored in the storage tank 402 to the reaction unit 50 via the pipe P200.
- the third connection portion 43 includes a pipe P40, a storage tank 402, a pipe P300, and a supply device 431.
- the pipe P300 connects the storage tank 403 and the decarboxylation section 61.
- the supply device 431 supplies the hydrochloric acid stored in the storage tank 403 to the decarboxylation unit 61 via the pipe P300.
- the cost related to chemicals can be reduced as compared with the conventional method.
- the magnesium production system 100 includes a generation unit 80 and an electrolysis unit 90 in addition to the magnesium chloride aqueous solution production system 1 described above.
- the generation unit 80 is an apparatus for separating water from an aqueous magnesium chloride solution to obtain MgCl 2.
- the generation unit 80 can adopt a configuration in which the magnesium chloride aqueous solution is treated by heating, depressurizing, blowing air, or a combination thereof to evaporate the water content.
- the electrolysis unit 90 is an apparatus for obtaining metallic magnesium by electrolyzing MgCl 2 with a molten salt.
- a known molten salt electrolysis facility can be adopted.
- the magnesium chloride aqueous solution production system 1 as described above, the magnesium chloride aqueous solution can be produced after reducing the cost related to chemicals as compared with the conventional method.
- FIG. 2 is an explanatory diagram of a magnesium chloride aqueous solution production system and a magnesium production system according to the second embodiment of the present disclosure.
- the magnesium chloride aqueous solution production system and the magnesium production system of the present embodiment are partially common to the magnesium chloride aqueous solution production system and the magnesium production system of the first embodiment. Therefore, the components common to the first embodiment in the present embodiment are designated by the same reference numerals, and detailed description thereof will be omitted.
- the magnesium chloride aqueous solution production system 2 has a decarboxylation unit 61 and a separation unit 62 as a pretreatment unit 60.
- the separation section 62 is provided between the decarboxylation section 61 and the crystallization section 10.
- the separation unit 62 is connected to the decarboxylation unit 61 via the pipe P21. Further, the separation unit 62 is connected to the crystallization unit 10 via the pipe P22.
- the separation section 62 is a reverse osmosis membrane that separates pure water PW from the water to be treated L61 with reduced carbonation in the decarboxylation section 61.
- the separation unit 62 generates water to be treated (water to be treated L62) by separating pure water PW from the water to be treated L61. Therefore, in the magnesium chloride aqueous solution production system 2 having the separation unit 62, pure water PW can be produced together with the magnesium chloride aqueous solution.
- the water to be treated L62 is supplied to the crystallization section 10 via the pipe P62.
- the treatment on the downstream side of the crystallization section 10 is performed as described in the first embodiment.
- the mixing unit 70 refers to a location where the pipe P4 and the first supply pipe P63 are connected.
- the reaction solution L4 and the pure water PW are mixed, and the concentration of the reaction solution L4 decreases. As a result, the processing load on the acid-alkali generating unit 40 is reduced. Further, since pure water PW is used for diluting the reaction solution L4, scale components such as calcium sulfate and calcium hydroxide are less likely to precipitate in the acid-alkali generating section 40, and stable continuous operation is possible.
- the mixing section 70 is the connection point between the pipe P4 and the first supply pipe P63, but as the mixing section, a mixing tank for mixing the reaction solution L4 and the pure water PW is provided in the path of the pipe P4. It may be provided in.
- the magnesium chloride aqueous solution production system 2 having such a configuration, the magnesium chloride aqueous solution can be produced after reducing the cost related to chemicals as compared with the conventional method.
- FIG. 3 is an explanatory diagram of a magnesium chloride aqueous solution production system and a magnesium production system according to the third embodiment of the present disclosure.
- the same components as those in the first and second embodiments are designated by the same reference numerals, and detailed description thereof will be omitted.
- the magnesium chloride aqueous solution production system 3 has a decarboxylation unit 61 and a separation unit 62 as a pretreatment unit 60.
- the concentration of the separation liquid L3 is lower than that of the recovery slurry S , particles of Mg (OH) 2 may be dispersed in the liquid. Therefore, when the separation liquid L3 is treated in the removal unit 30 with the separation liquid L3, the particles of Mg (OH) 2 are clogged inside the removal unit 30, and there is a concern that the performance of the removal unit 30 may deteriorate.
- the water to be treated L62 does not have particles of Mg (OH) 2 dispersed in the liquid, so that the performance of the removal unit 30 described above can be suppressed from being deteriorated, and the length is long. It can be operated stably for a period of time.
- the magnesium production system 200 has a second supply pipe P81 that supplies water W1 separated from the magnesium chloride aqueous solution by the generation unit 80 to the mixing unit 70.
- the water W1 is, for example, water (pure water) evaporated from the magnesium chloride aqueous solution in the generation unit 80.
- the reaction solution L4 and the water W1 are mixed, and the concentration of the reaction solution L4 decreases. As a result, the processing load on the acid-alkali generating unit 40 is reduced. Further, by diluting the reaction solution L4, scale components such as calcium sulfate and calcium hydroxide are less likely to precipitate in the acid-alkali generating section 40, and stable continuous operation becomes possible.
- the magnesium chloride aqueous solution production system 3 having such a configuration, the magnesium chloride aqueous solution can be produced after reducing the cost related to chemicals as compared with the conventional method.
- the magnesium aqueous solution production system 200 having such a configuration, the magnesium aqueous solution can be produced after reducing the cost related to chemicals as compared with the conventional method.
- the decarboxylation section 62 is provided after the decarboxylation section 61, but the decarboxylation section 61 may be provided after the separation section 62.
- the separation unit 62 may be provided.
- preprocessing unit 60 can be omitted.
- the magnesium chloride aqueous solution production system includes a crystallization section 10, a settling section 20 connected to the crystallization section 10, a removing section 30 connected to the settling section 20, and a removing section.
- An acid-alkali generation unit 40 connected to 30 and a reaction unit 50 connected to a sedimentation unit 20 are provided, and the crystallization unit 10 adds an aqueous sodium hydroxide solution to water L1 to be treated using seawater as a raw material.
- Magnesium hydroxide is crystallized to generate a reaction slurry L2 in which magnesium hydroxide particles are dispersed, and the sedimentation section 20 stores the reaction slurry L2 to precipitate the particles, and the recovery slurry S containing the particles at a high concentration.
- the separation solution L3 containing particles at a low concentration, and the removal unit 30 removes divalent cations from the aqueous solution L1 to be treated or the separation solution L3 to generate a reaction solution L4, and the acid alkali generation unit 40 produces an aqueous sodium hydroxide solution and hydrochloric acid from the reaction solution L4, the reaction unit 50 adds hydrochloric acid to the recovered slurry S to generate an aqueous magnesium chloride solution, and the acid-alkali generation unit 40 produces the acid-alkali generation unit 40 from the reaction solution L4.
- a first connecting portion 41 that connects the main body 40A that produces an aqueous sodium hydroxide solution and hydrochloric acid, the main body 40A, and the crystallization section 10 to supply the aqueous sodium hydroxide solution to the crystallization section 10, and the main body.
- a production system for an aqueous magnesium chloride solution comprising a second connecting portion 42 that connects 40A and the reaction unit 50 and supplies hydrochloric acid to the reaction unit 50.
- hydrochloric acid and an aqueous sodium hydroxide solution can be generated in the acid-alkali generation unit 40 and supplied to the crystallization unit 10, the reaction unit 50 and the decarboxylation unit 61.
- the cost related to the chemical can be reduced as compared with the conventional method.
- the magnesium chloride aqueous solution production system has a pretreatment unit 60 for obtaining water to be treated L1 from seawater, and the pretreatment unit 60 is a separation unit for separating water from the water to be treated L1. It has 62.
- the reaction solution L4 and the pure water PW are mixed, and the concentration of the reaction solution L4 is lowered.
- the processing load on the acid-alkali generating unit 40 is reduced.
- pure water PW is used for diluting the reaction solution L4
- scale components such as calcium sulfate and calcium hydroxide are less likely to precipitate in the acid-alkali generating section 40, and stable continuous operation is possible.
- the magnesium chloride aqueous solution production system has a pretreatment section 60 connected to the crystallization section 10 on the upstream side of the crystallization section 10, and the pretreatment section 60 is water to be treated. It has a decarbonation section 61 that adds hydrochloric acid to L1 to remove at least a part of carbonic acid contained in the water to be treated L1, and the acid-alkali generation section 40 connects the main body section 40A and the decarbonation section 61 to decarbonate. It has a third connecting portion 43 that supplies hydrochloric acid to the carbonic acid portion 61.
- the production system of the magnesium chloride aqueous solution can be stably operated for a long period of time.
- magnesium production system described in each embodiment is grasped as follows, for example.
- the magnesium production system according to the fifth aspect is a production system for a magnesium chloride aqueous solution according to any one of the first to fourth aspects, and water is separated from the magnesium chloride aqueous solution to produce magnesium chloride. It has a generation unit 80 and an electrolytic unit 90 that obtains metallic magnesium by melt-salt electrolysis of magnesium chloride.
- the magnesium production system is provided in a path for supplying the reaction solution L4 from the removing unit 30 to the acid-alkali generating unit 40, and at least a part of the water W1 separated by the producing unit 80. It has a mixing unit 70 that mixes the reaction liquid L4 and the water W1 separated by the generation unit 80, and a second supply pipe P81 that supplies the water W1 separated by the generation unit 80 from the generation unit 80 to the mixing unit 70.
- the reaction solution L4 and the water W1 are mixed, and the concentration of the reaction solution L4 is lowered.
- the processing load on the acid-alkali generating unit 40 is reduced.
- scale components such as calcium sulfate and calcium hydroxide are less likely to precipitate in the acid-alkali generating section 40, and stable continuous operation becomes possible.
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Abstract
Description
本開示は、2020年01月08日に出願された日本国特願2020-001483号に基づき優先権を主張し、その内容をここに援用する。
以下、図1を参照しながら、本開示の第1実施形態に係る塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システムについて説明する。なお、以下の全ての図面においては、図面を見やすくするため、各構成要素の寸法や比率などは適宜異ならせてある。
塩化マグネシウム水溶液の製造システム1は、晶析部10と、沈降部20と、除去部30と、酸アルカリ生成部40と、反応部50と、前処理部60とを備える。
前処理部60は、晶析部10の上流側において晶析部10と接続されている。前処理部60では、晶析部10に供給される被処理水L1を予め処理し、晶析部10以降の処理に適した状態に調整する。本実施形態の塩化マグネシウム水溶液の製造システム1において、前処理部60は、被処理水L1に溶解する炭酸の少なくとも一部を除去する脱炭酸部61を有する。
晶析部10は、被処理水L61に水酸化ナトリウム水溶液(NaOH aq.)を加えてMg(OH)2を晶析させる装置である。被処理水L61は、配管P61を介して晶析部10に供給される。
沈降部20は、配管P2を介して晶析部10と接続されている。晶析部10で生じた反応スラリーL2は、配管P2を介して沈降部20に供給される。
反応部50は、配管P31を介して沈降部20と接続されている。沈降部20で生じた回収スラリーSは、配管P31を介して反応部50に供給される。
除去部30は、配管P32を介して沈降部20と接続されている。沈降部20で生じた分離液L3は、配管P32を介して除去部30に供給される。
酸アルカリ生成部40は、配管P4を介して除去部30と接続されている。除去部30で生じた反応液L4は、配管P4を介して酸アルカリ生成部40に供給される。
NaCl+H2O → HCl+NaOH
NaCl+H2O → NaOH+1/2H2+1/2Cl2
H2+Cl2 → 2HCl
上述したように、本実施形態の塩化マグネシウム水溶液の製造システム1では、酸アルカリ生成部40において塩酸と水酸化ナトリウム水溶液とを生成し、晶析部10、反応部50および脱炭酸部61に供給する。すなわち、塩化マグネシウム水溶液の製造システム1では、晶析部10で用いる水酸化ナトリウム水溶液と、反応部50および脱炭酸部61で用いる塩酸とを、塩化マグネシウム水溶液の製造システム1内で生成している。
マグネシウムの製造システム100は、上述の塩化マグネシウム水溶液の製造システム1に加え、生成部80と、電解部90とを有する。
生成部80は、塩化マグネシウム水溶液から水を分離しMgCl2を得る装置である。生成部80では、塩化マグネシウム水溶液を加熱、減圧、送風およびこれらの組み合わせにより処理し、水分を蒸発させる構成を採用することができる。
電解部90は、MgCl2を溶融塩電解し、金属マグネシウムを得る装置である。電解部90の構成としては、公知の溶融塩電解設備を採用することができる。
図2は、本開示の第2実施形態に係る塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システムの説明図である。本実施形態の塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システムは、第1実施形態の塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システムと一部共通している。したがって、本実施形態において第1実施形態と共通する構成要素については同じ符号を付し、詳細な説明は省略する。
塩化マグネシウム水溶液の製造システム2は、前処理部60として、脱炭酸部61と分離部62とを有する。
図3は、本開示の第3実施形態に係る塩化マグネシウム水溶液の製造システムおよびマグネシウムの製造システムの説明図である。本実施形態において第1,第2実施形態と共通する構成要素については同じ符号を付し、詳細な説明は省略する。
塩化マグネシウム水溶液の製造システム3は、前処理部60として、脱炭酸部61と分離部62とを有する。
マグネシウムの製造システム200は、生成部80で塩化マグネシウム水溶液から分離された水W1を混合部70へ供給する第2供給管P81を有する。水W1は、例えば生成部80において塩化マグネシウム水溶液から蒸発させた水(純水)である。
各実施形態に記載の塩化マグネシウム水溶液の製造システムは、例えば以下のように把握される。
Claims (6)
- 晶析部と、
前記晶析部と接続された沈降部と、
前記沈降部と接続された除去部と、
前記除去部と接続された酸アルカリ生成部と、
前記沈降部と接続された反応部と、を備え、
前記晶析部は、海水を原料とする被処理水に水酸化ナトリウム水溶液を加えて水酸化マグネシウムを晶析させ、前記水酸化マグネシウムの粒子が分散する反応スラリーを生成し、
前記沈降部は、前記反応スラリーを貯留して前記粒子を沈降させ、高濃度で前記粒子が含まれる回収スラリーと、低濃度で前記粒子が含まれる分離液とに分離し、
前記除去部は、前記被処理水または前記分離液から2価陽イオンを除去して反応液を生成し、
前記酸アルカリ生成部は、前記反応液から水酸化ナトリウム水溶液と、塩酸とを生成し、
前記反応部は、前記回収スラリーに塩酸を加え、塩化マグネシウム水溶液を生成し、
前記酸アルカリ生成部は、前記反応液から水酸化ナトリウム水溶液と、塩酸とを生成する本体部と、
前記本体部と前記晶析部とを接続し、前記晶析部に前記水酸化ナトリウム水溶液を供給する第1接続部と、
前記本体部と前記反応部とを接続し、前記反応部に前記塩酸を供給する第2接続部と、を有する塩化マグネシウム水溶液の製造システム。 - 前記晶析部の上流側において前記晶析部と接続された前処理部を有し、
前記前処理部は、前記被処理水から純水を分離する分離部を有する請求項1に記載の塩化マグネシウム水溶液の製造システム。 - 前記除去部から前記酸アルカリ生成部へ前記反応液を供給する経路内に設けられ、前記純水の少なくとも一部と前記反応液とを混合する混合部と、
前記純水を前記分離部から前記混合部へ供給する第1供給管を有する請求項2に記載の塩化マグネシウム水溶液の製造システム。 - 前記晶析部の上流側において前記晶析部と接続された前処理部を有し、
前記前処理部は、前記被処理水に塩酸を加え、前記被処理水に含まれる少なくとも一部の炭酸を除去する脱炭酸部を有し、
前記酸アルカリ生成部は、前記本体部と前記脱炭酸部とを接続し、前記脱炭酸部に前記塩酸を供給する第3接続部を有する請求項1から3のいずれか1項に記載の塩化マグネシウム水溶液の製造システム。 - 請求項1から4のいずれか1項に記載の塩化マグネシウム水溶液の製造システムと、
前記塩化マグネシウム水溶液から水を分離し塩化マグネシウムを生成する生成部と、
前記塩化マグネシウムを溶融塩電解し金属マグネシウムを得る電解部と、を有するマグネシウムの製造システム。 - 前記除去部から前記酸アルカリ生成部へ前記反応液を供給する経路内に設けられ、前記生成部で分離された水の少なくとも一部と前記反応液とを混合する混合部と、
前記生成部で分離された水を前記生成部から前記混合部へ供給する第2供給管を有する請求項5に記載のマグネシウムの製造システム。
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