WO2011127671A1 - Procédé pour l'extraction d'hydroxyde d'aluminium et d'alumine à partir de produit secondaire obtenu durant le raffinage de magnésium métallique avec de l'aluminium ou de l'alliage d'aluminium comme réducteur - Google Patents

Procédé pour l'extraction d'hydroxyde d'aluminium et d'alumine à partir de produit secondaire obtenu durant le raffinage de magnésium métallique avec de l'aluminium ou de l'alliage d'aluminium comme réducteur Download PDF

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WO2011127671A1
WO2011127671A1 PCT/CN2010/073122 CN2010073122W WO2011127671A1 WO 2011127671 A1 WO2011127671 A1 WO 2011127671A1 CN 2010073122 W CN2010073122 W CN 2010073122W WO 2011127671 A1 WO2011127671 A1 WO 2011127671A1
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aluminum
cao
solution
decomposition
naal
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PCT/CN2010/073122
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English (en)
Chinese (zh)
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冯乃祥
王耀武
胡文鑫
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东北大学
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Publication of WO2011127671A1 publication Critical patent/WO2011127671A1/fr

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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
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/04—Dry methods smelting of sulfides or formation of mattes by aluminium, other metals or silicon
    • 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
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
    • 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
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
    • C01F7/068—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process from carbonate-containing minerals, e.g. dawsonite
    • 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
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
    • C01F7/0693—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process from waste-like raw materials, e.g. fly ash or Bayer calcination dust
    • 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
    • C22B21/00—Obtaining aluminium
    • C22B21/0015—Obtaining aluminium by wet processes
    • C22B21/0023—Obtaining aluminium by wet processes from waste materials
    • 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
    • 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
    • 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
    • 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • C22B7/008—Wet processes by an alkaline or ammoniacal leaching
    • 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 invention relates to a method for extracting aluminum hydroxide and aluminum oxide, and more particularly to a method for extracting aluminum hydroxide and aluminum oxide from by-products of preparing magnesium metal from aluminum or an aluminum alloy as a reducing agent.
  • the reducing agent is ferrosilicon
  • the raw material is dolomite
  • the main chemical component of dolomite is CaC0 3 ⁇ MgC0 3 , which generates CaO ⁇ MgO after calcination at high temperature.
  • the ferrosilicon powder is compounded according to the chemical reaction equation (1), and then formed into a mass. Then, it is placed in a vacuum reduction furnace, and vacuum reduction is performed at a temperature of about 125 CTC to obtain magnesium metal.
  • the amount of reducing agent ferrosilicon is generally greater than about 10% of the theoretical compounding amount of the above chemical reaction equation.
  • the ratio of the reaction material to the product metal magnesium is 4.78:1, but the industrial actual material/magnesium is 6:1. That is to say, industrially, silicon-heated magnesium smelting produces about 5 tons of ash per ton of magnesium (the main component is 2CaO ⁇ Si0 2 ). This ash can in principle be used as a raw material for cement production in cement plants, but The added value is very low and the factory has abandoned it.
  • the by-product of the invention for vacuum-thermal reduction of magnesium metal by using aluminum or aluminum silicon alloy powder as a reducing agent is a bulk material mainly composed of a compound composed of CaO and A1 2 3 3 as a main component.
  • Alumina in by-products is a valuable metallurgical and chemical raw material. If the alumina in the slag is extracted and recycled, it can not only add a chemical product to the magnesium smelter, but also heat the aluminum. The production cost of producing magnesium metal by vacuum thermal reduction is greatly reduced. Summary of the invention
  • the present invention provides a method for extracting aluminum hydroxide and aluminum oxide from residual by-product slag after preparing magnesium metal by vacuum heat reduction method using aluminum or aluminum alloy as a reducing agent, which can heat aluminum
  • the by-product slag of magnesium smelting by vacuum thermal reduction is recovered and utilized, thereby greatly improving the economic efficiency of the magnesium plant.
  • the vacuum magnesium reduction method using aluminum or aluminum alloy as a reducing agent is carried out by the following steps:
  • Dolomite, magnesite ore, brucite and limestone are used as raw materials for calcination, in which dolomite is calcined.
  • the temperature is 1000 ⁇ 1200°C, and the CaO ⁇ MgO material is obtained after calcination; the calcination temperature of the magnesite ore is 800 ⁇ 1000°C, and the MgO-containing material is obtained after calcination; the calcining temperature of the brucite is 800 ⁇ 1000°C, After calcination, the MgO-containing material is obtained; the calcination temperature of the limestone is 1000-1200 ° C, and the CaO-containing material is obtained after calcination; two or more of the above four materials are mixed to prepare a MgO/CaO molar ratio of 1.5 ⁇ 18 raw materials.
  • the raw materials prepared above are ground to less than 100 mesh in a ball mill and uniformly mixed to obtain a powder to be reduced.
  • the reducing agent is aluminum powder or aluminum alloy powder with a particle size of less than 1 mm, and is made into a reaction material, and the reducing agent is added in an amount of 1.03 to 1.1 times the amount required for the reaction theory;
  • the aluminum alloy powder described is an aluminum silicon alloy powder or an aluminum magnesium alloy powder.
  • the reaction material is pressed into a dough or a block.
  • the lumps or block reaction materials are placed in a high-temperature vacuum reduction reactor with a magnesium crystallizer for vacuum reduction reaction.
  • the pressure in the reaction furnace is less than 30 Pa, and the reaction temperature is 900-1250 ° C.
  • the reaction produces gaseous magnesium metal.
  • the magnesium crystallizer is condensed and crystallized into metallic magnesium.
  • CaO + 3MgO + 2A1 3Mg + CaO ⁇ A1 2 0 3 ( 5 ) wherein the by-product slags are CaO ⁇ 2A1 2 0 3 , CaO ⁇ 6A1 2 0 3 , 12CaO ⁇ 7A1 2 0 3 and CaO ⁇ A1 2 0 One or a mixture of two or more of 3 .
  • the ratio of CaO and MgO in the batch should take into account the behavior of the component content of silicon in the reducing agent during the reduction process.
  • the method for extracting A1 2 0 3 and Al(OH) 3 by using the by-product of the metal thermal reduction reaction under the above vacuum condition is as follows: 1. First, the agglomerate The by-products are crushed and ground to below 100 mesh, and then the milled slag is placed in a Na 2 CO 3 solution or placed in a mixed solution of Na 2 CO 3 and NaOH at 50-300 ° C.
  • the slag A1 2 0 3 is leached, and the A1 2 0 3 in the leaching solution is present in the leaching solution in the form of NaAl(OH) 4 , and the CaO in the slag is precipitated in the form of CaCO 3 come out.
  • the decomposition is carried out by seed, it is necessary to add ⁇ 1( ⁇ ) 3 seed crystal to the solution containing NaAl(OH) 4 for seed seed decomposition, and to decompose NaAl(OH) 4 into Al(OH) 3 and Na(OH).
  • the ⁇ 1( ⁇ ) 3 formed after the decomposition of the seed in the solution is separated by filtration to obtain the product Al(OH) 3 , and a solution composed of Na(OH) and partially undecomposed NaAl(OH) 4 ; 3 Most of them are used as final products, and some are returned as seed crystals to the seed decomposition vessel to separate and decompose NaAl(OH) 4 .
  • the produced Al(OH) 3 can be calcined at a temperature of 800 ° C or higher to dehydrate Al(OH) 3 .
  • the NaAl(OH) 4 solution leached from the slag is decomposed by carbon to form ⁇ 1( ⁇ ) 3 , it is necessary to introduce C0 2 gas into the solution containing NaAl(OH) 4 in the carbon decomposition reaction vessel for carbon.
  • the decomposition is carried out to decompose NaAl(OH) 4 to form ⁇ 1( ⁇ ) 3 and Na 2 C0 3 products.
  • the CO 2 required for the carbon fraction process is derived from the CO 2 by -product formed by the dolomite or magnesite calcination process.
  • the Al(OH) 3 formed by the decomposition of carbon is separated from the Na 2 CO 3 solution formed by carbonation to form commercial aluminum hydroxide.
  • the produced Al(OH) 3 can be calcined at a temperature of 800 ° C or higher to dehydrate Al(OH) 3 to obtain an alumina product.
  • the desiliconization in the step 2 is a conventional alumina industrial desiliconization method.
  • the concentration of sodium carbonate is 80-150 g/L
  • the liquid-solid ratio of the Na 2 C0 3 solution to the slag is 50-1000 g/L, that is, leaching per liter of the leaching solution 50 ⁇ 1000g slag
  • the concentration of sodium carbonate in the mixed solution is 20-150 g/L
  • the concentration of sodium hydroxide is 80-300 g/L.
  • the liquid-solid ratio of the mixed solution to the slag is 50 to 1000 g/L.
  • the leaching time in the above method is 20 to 200 minutes.
  • the seed when the leached CaO-containing and A1 2 0 3 slag have a main chemical composition of CaO ⁇ 2A1 2 0 3 or CaO ⁇ 6A1 2 0 3 or a mixture of the two, the seed contains a small amount of NaAl after decomposition.
  • the (OH) 4 NaOH solution is subjected to carbonation treatment of a portion of the NaOH in the causticizing vessel, and then the Al(OH) 3 formed during the partial carbonation is filtered to become NaOH and Na 2 C0.
  • the mixed solution of 3 is returned to the leaching agent as a raw material in the wet mill.
  • the chemical composition of the material in the dissolution raw material is mainly CaO ⁇ A1 2 0 3 or 12CaO ⁇ 7A1 2 0 3 or a mixture of the two
  • the NaOH solution containing a small amount of Na after decomposition is subjected to carbonation treatment, followed by filtration.
  • ⁇ 1( ⁇ ) 3 formed after carbonation the NaOH in the solution completely changed to Na 2 C0 3 , and the Na 2 CO 3 solution was returned to the leaching agent as a raw material in the wet mill.
  • the main chemical component of the leached raw material is CaO ⁇ 2A1 2 0 3 or CaO ⁇ 6A1 2 0 3 or a mixture of the two
  • the Na 2 C0 3 in the mother liquor after carbon separation needs to be partially causticized, so that the Na 2 CO 3 portion of the mother liquor is converted into NaOH, the causticizing agent is calcium oxide, and the partially causticized carbon mother liquor contains NaOH.
  • the Na 2 C0 3 chemical component which is returned to the leaching agent as a raw material in the wet mill; when the main chemical component of the leached raw material is CaO ⁇ A1 2 0 3 or 12CaO ⁇ 7A1 2 0 3 or a mixture of the two
  • the Na 2 C0 3 contained in the mother liquor after the carbon separation is no longer subjected to causticization treatment, but is directly used to circulate the mother liquor into the wet mill as a raw material leaching agent.
  • the method of the invention can make full use of the obtained ash and prepare the aluminum hydroxide and the aluminum oxide by the decomposition method, thereby improving the economic benefit of preparing the metal magnesium, reducing the environmental pollution and reducing the magnesium metal. Preparation costs.
  • Fig. 1 is a flow chart showing the process for extracting aluminum hydroxide and aluminum oxide from by-products of preparing magnesium metal from aluminum or aluminum alloy as a reducing agent according to Example 1 of the present invention.
  • Example 2 is a schematic flow chart showing a process for extracting aluminum hydroxide and aluminum oxide from by-products of preparing magnesium metal from aluminum or aluminum alloy as a reducing agent according to Example 2 of the present invention.
  • Fig. 3 is a flow chart showing the process for extracting aluminum hydroxide and aluminum oxide from by-products of preparing magnesium metal from aluminum or aluminum alloy as a reducing agent according to Example 3 of the present invention.
  • Fig. 4 is a flow chart showing the process for extracting aluminum hydroxide and aluminum oxide from by-products of preparing magnesium metal from aluminum or aluminum alloy as a reducing agent according to Example 4 of the present invention.
  • the slag whose main component is CaO ⁇ 2A1 2 0 3 or CaO ⁇ 6A1 2 0 3 or a mixture of the two is ground and placed in a mixed solution composed of NaOH and Na 2 CO 3 , and the mixed solution may also be contained.
  • a small amount of NaAl(OH) 4 component then leaching the alumina in the ash to a NaAl(OH) 4 solution at a temperature of 50-300 ° C, and then filtering to dissolve the NaAl(OH) 4 solution and leaching generated during the slag separation CaC0 3, then (OH) 3 was added a seed crystal ⁇ 1 ( ⁇ ) NaAl 4 in the solution, so NaAl (OH) 4 solution was decomposed at a temperature 50-9CTC the precipitation of Al (OH) 3 Then, ⁇ 1( ⁇ ) 3 is filtered out and washed, and the obtained ⁇ 1( ⁇ ) 3 - part is used as a seed crystal to return the NaAl(OH) 4 solution for the seed decomposition process, and the other part is used as the industrial ⁇ 1 ( ⁇ ) 3 product. Or the obtained Al(OH) 3 is calcined at 800-1200 ° C to obtain an A1 2 0 3 product.
  • the mother liquor After seeding and filtering out the Al(OH) 3 formed by decomposition, the remaining liquid is the mother liquor.
  • the mother liquor mainly contains NaOH formed by the decomposition of Al(OH) 3 by the seed crystal and NaAl(OH) 4 which is not completely decomposed. .
  • the mother liquor is then transferred to a carbonation vessel, The C0 2 gas is introduced, and a part of the NaOH in the mother liquid is carbonated to Na 2 C0 3 , and then Al(OH) 3 formed in a part of the carbonation process is filtered out, and the filtrate contains NaOH and Na 2 C0 3 , and the filtrate is filtrated.
  • the leaching agent as the raw material is recycled. The process is shown in Figure 1.
  • the reduction material composed of MgO and CaO is prepared by preparing magnesium metal mainly from CaO ⁇ A1 2 0 3 or 12CaO ⁇ 7A1 2 0 3 , or by two Aluminum hydroxide and aluminum oxide are extracted from the slag composed of the mixture.
  • the slag whose main component is CaO ⁇ A1 2 3 3 or 12CaO ⁇ 7A1 2 0 3 or a mixture of the two is ground and placed in a solution whose main component is Na 2 CO 3 , and the solution may also contain a small amount of NaAl. (OH) 4 component, then leaching the alumina in the ash to a NaAl(OH) 4 solution at a temperature of 50-30 CTC, and then filtering to form a NaAl(OH) 4 solution and a leaching process.
  • OH OH
  • the mother liquor mainly contains NaOH formed by the decomposition of Al(OH) 3 by the seed crystal and NaAl(OH) 4 which is not completely decomposed. .
  • the mother liquor is transferred to a carbonation vessel, and C0 2 gas is introduced, and a part of the NaOH in the mother liquor is carbonated to Na 2 C0 3 , and then Al(OH) 3 formed in the partial carbonation process is filtered out, and the filtrate contains NaOH and Na 2 CO 3 , the filtrate was returned to the wet mill for recycling as a leaching agent for the raw material.
  • the process is shown in Figure 2.
  • the slag having a main chemical composition of CaO ⁇ 2A1 2 0 3 or CaO ⁇ 6A1 2 0 3 or a mixture of the two is ground and placed in a solution consisting of NaOH and Na 2 C0 3 , and the mixed solution may also be contained.
  • a small amount of NaAl(OH) 4 component, leaching the alumina in the ash to a NaAl(OH) 4 solution at a temperature of 50-300 ° C, and then filtering to make the NaAl(OH) 4 solution and the leaching process The CaC0 3 slag produced in the separation is separated, and then C0 2 is introduced into the NaAl(OH) 4 solution to decompose the NaAl(OH) 4 in the solution to form an Al(OH) 3 precipitate and Na 2 C0 3 , and then Filtration gives ⁇ 1( ⁇ ) 3 , and the obtained ⁇ 1( ⁇ ) 3 is calcined at 800-1200 °C to obtain industrial A1 2 0 3 , and the mother liquor filtered out of Al(OH) 3 is called carbon mother liquor, and the carbon mother liquor is mainly It is a composition of a permanent Na 2 C0 3 solution, and then a portion of Na 2 C0 3 in the mother liquor is reacted with CaO formed by calcination of limestone to
  • the reduction material composed of MgO and CaO is prepared by preparing magnesium metal mainly from CaO ⁇ A1 2 0 3 or 12CaO ⁇ 7A1 2 0 3 , or by two Aluminum hydroxide and aluminum oxide are extracted from the slag composed of the mixture.
  • the slag whose main component is CaO ⁇ ⁇ 1 2 0 3 or 12CaO ⁇ 7A1 2 0 3 or a mixture of the two is ground and placed in a solution whose main component is NaCO 3 , and the solution may also contain a small amount of NaAl (OH).
  • the alumina in the ash is leached to make a NaAl(OH) 4 solution, and then filtered to make the NaAl(OH) 4 solution and the leaching process to form solid Al (OH) 3 and NaC0 3 solution, and then filtered to obtain ⁇ 1 ( ⁇ ) 3 , the obtained ⁇ 1 ( ⁇ ) 3 is calcined at 800-1200 ° C to obtain industrial A1 2 0 3 , and the NaCO 3 solution is returned to the leaching of magnesium ash slag , forming a closed loop.
  • the process is shown in Figure 4.

Abstract

L'invention concerne un procédé d'extraction d'hydroxyde d'aluminium et d'alumine à partir du produit secondaire obtenu durant le raffinage de magnésium métallique avec de l'aluminium ou de l'alliage d'aluminium comme réducteur, qui comprend : la pulvérisation et le broyage au mouillé du matériau grumeleux, la soumission du matériau à l'extraction dans une liqueur alcaline, la filtration et la séparation du CaCO3 produit durant l'extraction pour obtenir une solution de NaAl(OH)4, la soumission ultérieure de la solution à la désiliconisation et la décomposition du germe ou la décomposition carbonisation pour décomposer NaAl(OH)4 dans la solution, la séparation de l'hydroxyde d'aluminium produit durant la décomposition à partir de la liqueur mère par filtration. Par ce procédé, en même temps que le raffinage du magnésium métallique, de l'hydroxyde d'aluminium et de l'alumine peuvent être préparés par utilisation complète du clinker obtenu par le procédé de décomposition, le bénéfice économique du raffinage du magnésium métallique est amélioré, la pollution environnementale est réduite et le coût de production du magnésium est réduit.
PCT/CN2010/073122 2010-04-12 2010-05-24 Procédé pour l'extraction d'hydroxyde d'aluminium et d'alumine à partir de produit secondaire obtenu durant le raffinage de magnésium métallique avec de l'aluminium ou de l'alliage d'aluminium comme réducteur WO2011127671A1 (fr)

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CN201010144062.1 2010-04-12
CN2010101440621A CN101845550B (zh) 2010-04-12 2010-04-12 从以铝或铝合金为还原剂制取金属镁的副产物中提取氢氧化铝和氧化铝的方法

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US10151017B2 (en) * 2016-04-24 2018-12-11 Yadian Xie Method for extracting ultra high purity alumina from wasterwater
CN115159552A (zh) * 2022-07-04 2022-10-11 重庆大学 一种从含铝资源中回收氧化铝的方法
CN115321589A (zh) * 2022-09-16 2022-11-11 东北大学 氟钛酸盐铝热还原制备钛或钛合金过程中副产物的综合利用方法

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CN110042240A (zh) * 2019-04-29 2019-07-23 安徽工业大学 一种真空铝热还原法同时制取金属锂和金属镁的工艺
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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1424256A (zh) * 2002-12-23 2003-06-18 广西壮族自治区河池地区矿业有限责任公司 含铁铝土矿生产氧化铝工艺
CN1562756A (zh) * 2004-03-19 2005-01-12 邝中 含铝酸钙的物料提取氧化铝工艺
CN101028935A (zh) * 2007-01-26 2007-09-05 长安大学 煤矸石中提取氢氧化铝或氧化铝及其废渣生产水泥的方法
CN101028936A (zh) * 2007-01-26 2007-09-05 长安大学 一种从高铝粉煤灰提取氧化铝及其废渣生产水泥的方法

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101264910B (zh) * 2008-04-25 2010-10-13 河南未来铝业（集团）有限公司 拜耳法生产氢氧化铝或氧化铝工艺中蒸发母液的加种子方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1424256A (zh) * 2002-12-23 2003-06-18 广西壮族自治区河池地区矿业有限责任公司 含铁铝土矿生产氧化铝工艺
CN1562756A (zh) * 2004-03-19 2005-01-12 邝中 含铝酸钙的物料提取氧化铝工艺
CN101028935A (zh) * 2007-01-26 2007-09-05 长安大学 煤矸石中提取氢氧化铝或氧化铝及其废渣生产水泥的方法
CN101028936A (zh) * 2007-01-26 2007-09-05 长安大学 一种从高铝粉煤灰提取氧化铝及其废渣生产水泥的方法

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
BI SHIWEN ET AL.: "Research on Extracting Alumina from Blast Furnace Calcium Aluminate slag", LIGHT METALS, 1992, pages 10 - 15, 26 *
HU WENXIN ET AL.: "Vacuum Thermal Reduction Kinetics of Calcined Dolomite with Al-Si-Fe Alloy", THE CHINESE JOURNAL OF PROCESS ENGINEERING, vol. 10, no. 1, February 2010 (2010-02-01), pages 127 - 132 *

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10151017B2 (en) * 2016-04-24 2018-12-11 Yadian Xie Method for extracting ultra high purity alumina from wasterwater
CN106185975A (zh) * 2016-07-22 2016-12-07 山东钢铁股份有限公司 一种利用高炉渣制备分子筛晶体的方法
CN115159552A (zh) * 2022-07-04 2022-10-11 重庆大学 一种从含铝资源中回收氧化铝的方法
CN115159552B (zh) * 2022-07-04 2024-01-26 重庆大学 一种从含铝资源中回收氧化铝的方法
CN115321589A (zh) * 2022-09-16 2022-11-11 东北大学 氟钛酸盐铝热还原制备钛或钛合金过程中副产物的综合利用方法
CN115321589B (zh) * 2022-09-16 2023-09-12 东北大学 氟钛酸盐铝热还原制备钛或钛合金过程中副产物的综合利用方法

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