• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
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  • 优先权
    • 专利摘要:
    In the process for the preparation of pure aluminum oxide by the steps of hydrochloric acid decomposition of mechanically or thermally activated clay or alumina containing minerals, separating the insoluble residue, removing the iron from the solution, crystallizing the aluminum chloride in the iron-free solution, thermally decomposing the crystallizate to aluminum oxide and recovering the hydrochloric acid from the decomposition gases, the improvement comprising effecting the process by the steps of mechanically pretreating the clay, drying the pretreated clay, thermally or mechanically activating the clay, subjecting the activated clay to circulating leaching, separating the leached material into an SiO2 containing residue and an AlCl3 solution, extracting the AlCl3 solution to an evaporating crystallization and thermally decomposing the crystals to produce alpha -Al2O3. All of the stages are interrelated one to the other for maximum recovery of byproducts, heat, acid and the like. The alpha -Al2O3 is directly produced in a form of high purity suitable for most applications.
    公开号:SU969670A1
    申请号:SU797770527
    申请日:1979-04-04
    公开日:1982-10-30
    发明作者:Зигфрид Цигенбальг；Герхард Хааке；Рудольф Зиберт；Герхард Фишер
    申请人:Мансфельдский Комбинат Им.Вильгельма Пика (Инопредприятие)；
    IPC主号:
    专利说明:

    3rdyb704
    em (energy expenditure, difficult work of several absorption
    equipment, and high costs. arrangements in countercurrent.
    Izvesten (patent of the German Empire. A method of production 414128) is known, in which clay clay is evaporated (German patent of a part of hydrochloric acid {solution from the above empire 562498), consisting of extracting iron from a evaporated solar chloride suspension from aluminum, and Some of the gleigh leaching solutions are used for absorption compared with its thermal decomposition of but dilute hydrochloric acid gases, by distillation with chlorides. For the off-gases and water vapor, the distillation process itself requires a stream of, for example, thermal hydrogen chloride — high concentration of decomposition in a rotary kiln, which must be additionally obtained. However, it is prepared in such a way that it costs 20% more expensive. hydrochloric acid solution, pritsess; due to the high costs of the apparatus, which helps wash the suspension jsRU and energy,
    crystals for the purpose of separation of chlorides. One of the decisive disadvantages of limestone and aluminum, in the washing process, is the additional solution of a significant amount of alkali metal chlorides, alkaline chlorides, because with a decreasing magnesium concentrate, as for sublimation by hydrochloric acid, it increases It is necessary to establish a certain level of aluminum chloride. In addition, the ratio of iron oxide, alumina to the end of the process as calcium hydroxide is used as a washing solution and alkali metal chlorides of magnesium solution.
    Only hydrochloric acid, free from the same-after removal of iron, the final prosthesis, the preparation of which additionally jsuct is freed from the remaining in it the irocess. Moreover, with the presence of salts by washing with water, non-ferric ferric ions with ferrous chloride, i.e., solid solutions are formed before aluminum introduction, solid solutions should be removed, and chlorides should not be removed by iron washing. In order to do the washing. This limits the maintenance of JJ additives within acceptable limits, keeping the iron in solution from leaching — this method can be processed, and the intended use of only clay with a low content of ferrous washing acids for higher amounts.
    clay production is severely limited. To obtain aluminum chloride, which is known to be a choke, which afterwards is intended to produce the alumina of this method (patentmini for the production of aluminum, from the German Empire 438745), methods are enriched (layered descriptions of hydrobolic acid using solution retentions and non-accepted applications 15 not only for washing the chloride suspension (92 064, 15 92 070), in which crystalline aluminum, but also for leaching the new tallization of aluminum chloride, portions of clay are carried out, it enrichment pactBOpatakim way that this product has been pesol hydrochloric acid leaching of the clay and its thermal decomposition d t imeprovod not separately but together in ob is sufficient to obtain alyurazom oxide, that the solution in one operation pos mini purity. This is achieved by being held in contact with the absorption of the multistage process by fractional gases containing hydrochloric acid crystallization. As a result, that, and with aluminous raw materials. As a result of incomplete crystallization in the first stage, those of this injected hydrochloric acid dissipate sufficiently pure crystallisate. directly to leaching. The residual solution, the enriched impurity solution, retains its ability to cc, after the separation from it of the crystal absorption of additional hydrochloric acid, suspended. Thus, n clay is obtained from tl., A more concentrated solution is loaded into the second stage, and pre-crystallization. The crystalline precursor preparation, which is formed during this process, is returned to the first stage of the hydrochloric acid bath. The process and the residual solution remain, however, the method also does not resolve the sample-stage crystallization.
    权利要求:
    Claims (17)
    [1]
    The impurity lemma is characterized by high- This process of fractional cryotallium costs for equipment, since non-cost can be done only with significant impurities, enters the third costly equipment.  Crygallipation equipment, necessary to return the crystals after separation of the solid and liquid phases and transferring to the pulp in the previous stages, consists of a large number of crystallizers of centrifuges, heat exchangers, dissolution tanks, pumps, etc.  depending on the required number of stages.  A known method (laid out description of the invention to non-accepted application 15 92 070), in which the amount of final solution ejected can be kept within acceptable limits only when the initial solution is slightly soiled, t.  e.  when reworked comparatively; pure clay and aluminous materials.  Impurities such as, for example, titanium salts, in the presence of calcium ions, are very difficult to give off by precipitating with sulfuric acid.  A known method is to isolate ferric chloride (1U) from aluminum chloride and aqueous solutions containing ferric chloride (111), which selectively acts as a water-insoluble organic resin reagan to remove iron (laid out description of the application to the unaccepted application 1592 065).  The removal of iron is a necessary prerequisite for obtaining alumina, which is suitable as a starting material for the electrolysis of aluminum.  This method makes it possible to obtain aluminum chloride almost completely purified from jellies or other impurities such as sodium magnesium or calcium, it does not affect, although the removal of these impurities is extremely suitable for producing alumina that meets all quality requirements. .  Known method H. O-PoppKeiott, l) -li. 5avjyer Hiarochtoric Acid Leacbittgr of Catoiined Kaotiv to Probe T lmrla. T S-PaperseEeciiovl Paper NO DC-LB, which consists in the extraction of alumina ISH1 by leaching the compacted draft clay with hydrochloric acid, p. The following stages: separation of the solid and liquid phases, removal of iron, crystallization and thermal decomposition, the production of a sufficiently pure crystalline aluminum chloride hexahydrate is carried out by crystallizing the coarse-grained material using a foam layer and rinsing it with concentrated hydrochloric acid on a centrifuge.  Crystallization of aluminum chloride chloride is complicated by the presence of a narrow metastable region and a high nucleation rate.  In addition, the final speed of the crystals in a solution of high solution E и and a small difference in density between the crystal and the solution is very small.  During crystallization in the fluidized bed, this leads to a small flow rate of the supersaturated solution in the fluidized bed of crystals, to obtain small quantities of crystals per 1 m of supersaturated solution, as well as to a specific crystallization productivity.  In addition, regeneration with concentrated hydrochloric acid from the contaminated wash solution is necessary.  Due to the low solubility of the impurities, a significant amount of hydrochloric acid is required.  Known method (F. A-Peier -DW. JoVinSOM, R. ) i) producing alumina by leaching rough clay with hydrochloric acid (research report No. 6133 by Bureau oi Mines).  However, the method describes only the sequence of individual stages of the process (Tessa, not enough attention to create closed cycles with minimal waste; the method is characterized by insufficient consideration of the potential for leakage of contaminants and utilization of the by-products obtained.  Environmental requirements are also not satisfactorily fulfilled.  The chemical composition and physical properties of alumina are also not given, so the question of the suitability of alumina and for the production of aluminum remains open.  The purpose of the invention is to create a technologically and technically advantageous method for producing pure aluminum oxide from clays and alumina materials by leaching with hydrochloric acid: one that can be technologically simple and economically profitable to be implemented in industrial conditions; the creation of a method for the integrated use of readily available types of raw materials in closed cycles with the production of small amounts of by-products.  products, with an optimal combination of process stages agreed upon among themselves and the corresponding requirement of environmental protection; the creation of a method for the possible complete isolation of impurities, which makes it possible to obtain alumina.  796 cooTDeTcfByromyro for the purity of the requirements of the aluminum industry, the compliance of the physical parameters of alumina with the requirements of pred. should be applied to it when used in the aluminum industry.  The method is carried out as follows.  Chernov clay with moisture, from which it comes out of the mine, stumbles into the equipment to give it a suitable form according to the pressing or cutting technology, followed by drying at 130-25, resulting in a molded product with a grain size of mm or in a grinding mill "" Purified with drying, to produce matritsa with a particle size of 0-1 mm.  The residual moisture after the substance is not more than 3%.  After that, mechanical or thermal activation is performed to correct the acid-insoluble kaolinite into a soluble metakaol. Thermal activation of clay or clay minerals is carried out in one stage or in several stages at 6OO-8OO C. oxidation of organic matter and iron, so that additional oxidation of the solution; leaching is not required.  By appropriate choice of the mode of thermal activation, it is possible to reduce the content of iron (K) in solution in the solution below the 1Omg / l.  The mechanically or thermally activated material is fed to the hydrochloric leaching, where complete dissolution of the leached part of the clay is achieved with a slight transfer of the impurities into the solution.  The leaching with hydrochloric acid is carried out depending on the grain size of the loaded clay as a percolation leaching (circulation leaching; extraction) of coarse-grained clay i from 2 to 20 mm, or as a suspension leaching for fine-grained clay from 0 to 2 mm.  The parameters and results of percolation leaching are as follows: The grain size of the clay, mm 2-20 Hydrochloric acid concentration,% 15-25 Stoichiometric amount of hydrochloric acid introduced (in relation to aluminum oxide),% 80-120 0 Leach temperature, C105-110 Duration of leaching, h6-12 Removal of alumina 80-90 Solubility.  iron,% 50-60 For suspension leaching, dannt 1c is similar except for the duration of leaching, which is reduced to 30-120 minutes (depending on the grain size).  The subsequent separation of the solid and liquid phases after leaching can be carried out in thickeners, rotating cell filters and other passing devices, with the use of flocculants; Polyacrylamide-based oiSecne products have a significant increase in sedimentation and. Filtration Properties When stoichiometric or substoichiometric amounts of acid are used (in relation to the clay being charged), vital titanium is precipitated by hydrolysis. and is absorbed by the leaching cake.  This allows the titanium titanium solution to be almost completely removed, eliminating the possibility of precipitation. Calysh sulfate during crystallization. Titanium content. it decreases to values below 5 mg / l.   High-silicon cake, subjected to a multi-stage washing process, in its hydraulic properties, high.  Its intrinsic strength and low apparent density, and also due to its high content of amorphous silicic acid, is a valuable starting or additive material for the building and glass industries.  In addition, there are possibilities for its use as a filler in many other areas. .  .   The solution obtained after leaching has the following state: AC-fL O, g / l 90-100 1h e / zr, g / L carried free, g / l 5-5O Nclg, g / l.  Oh, 1. -0.3, g / l Ti O, mg / l mg / l 30-60 SiO, mg / l 50-100 De-ironing of aluminum chloride solution - with the above content of iron (III) chlorine, free salt KHCJiOTbi and about 190 -280 g / l of chloride is carried out by liquid-liquid extraction.  The organic extraction, practically water-insoluble solution based on higher paraffin hydrocarbon, at boiling (145-200 C) contains 5-15% secondary aliphatic amine with 6-12 carbon atoms, and in order to prevent the formation of the third phase add higher aliphatic alcohol with 6- 12 carbon atoms in a concentration of 2040 weight.  %  After separation of the phases, the iron in the organic phase is reextracted in the second stage of extraction using water or diluted hydrochloric acid with a content of 10 -4 O g / l free acid.  The resulting organic phase, free of iron, can again be used for the first stage extracts.  The ratio of the volume of organic and aqueous phases should be from 1: 1 to 1 during extraction. : 5, and when reextraction from 3: 1 to 7: 1.  The optimum temperature for exchange processes is 25-4 ° C.  The content of chepase in the extracted solution during the calcination process can be reduced to a quantity below 10 mg / l with complete oxidation of the organic components.  Instead of an extractant based on secondary aliphatic amines, a solution of tributyl phosphate can also be used, the ratio of which to the aqueous phase is 1: 2.  Iron extraction is adjusted at a phase ratio of 4: 1 to 6: 1.  The solution of ferric chloride obtained during the extraction process by the method of decomposition of eroi by spraying can be processed into high-quality ferric oxide with simultaneous extraction of hydrochloric acid.  Other beneficial components, such as gallium, are obtained from iron-rich reextracts by additional liquid-liquid extraction based on higher, water-insoluble aliphatic alcohols mixed with gasoline or kerosene,. long chain aliphatic amines or m-tributyl phosphate.  Extracted solution of aluminum chloride, containing v 20 wt.  % aluminum chloride is evaporated in one stage or in several stages to a concentration of v-30 wt.  %  This l 30% solution of aluminum chloride is fed to the crystallization.  With the given physicochemical properties of the solution and the crystals, the method of crystallization with the circulation of the suspension is used, since by circulating supropensive, a large amount of crystals is introduced into the boiling zone, which ensures its effective. effective reduction of supersaturation.  This method of crystallisation allows the crystallizate to be scattered, with a small residual moisture content.  By washing with a freshly prepared solution in a centrifuge, the content of impurities can be reduced in potassium to (5%, in calcium to 31 {5%, in titanium to 41CF%, in vanadium to 2-l (J% and in silica).  In the case of an average grain size of crystallized at least 0.25 mm and a residual moisture content of 1-7%, only 1-7% of the stock solution should be withdrawn in relation to the volume of fresh solution introduced.  From this mother liquor, crude alumina is obtained by thermal decomposition, which is subsequently processed for the necessary purposes.  The resulting crystallisate containing 52-54% aluminum chloride, is fed to a two-stage thermal decomposition.  In the low-temperature stage, at 150-200s, partial decomposition is carried out using hot exhaust gases from the high-temperature stage of the process.  The composition of the intermediate products is selected so that the gases from the high-temperature stage of the decomposition process contain at least 3% by volume of hydrogen chloride.  This contributes to the fact that at 12OO-13OO with almost no introduction of gaseous hydrogen chloride or other chlorinating agents, almost complete chlorinating sublimation of impurities, in particular alkali and earth-alkali metals, occurs.  The amount of C1-glnokozem meets the requirements of melt electrolysis.  The waste gases formed during the thermal decomposition of aluminum chloride are fed to the adiabatic or isothermal absorption of hydrogen chloride in order to extract 15-25% hydrochloric acid for leaching.  The application of the principle of the fluidized bed during thermal activation in the proposed method provides good conditions for heat transfer and at the same time high performance per unit volume and time.  In addition, the principle of the fluidized bed makes it possible to achieve very constant temperatures, which prevents the calcinate from overheating and the associated decrease in the solubility of the contained alumina; allows the use of both circulating and slurry leaching methods, which allows the processing of raw clays with a different granulometric composition.  Leaching of clay in a lumpy form according to the method of circulation leaching compared with the method of suspension leaching has the technological advantage that after the leaching process does not require separation of the solution from the cake in special devices, the solution can be discharged from the self-filter system with a low content of solid.  The crystallisate obtained according to the proposed method after centrifugation contains very little residual moisture, t.  e.  the mother liquor is enriched with impurities, so that the required purity of the crystallisate is achieved by washing the evaporated stock solution in a centrifuge.  Thermal decomposition results in volatilization of 85-95% sodium and potassium from their initial content.  This also eats two thirds of the initial amount of calcium, and thus the calcium is separated from the alumina produced.  This repeated purification of alumina is a prerequisite for the simple crystallization of aluminum chloride hexahydrate and leads to a significant reduction in equipment and energy costs.  To remove the distilled chlorides from the process, an electrostatic precipitator is used, in which impurities are collected in the form of dust, which is processed separately due to its high content of alumina.   for example, to obtain aluminum sulfate.  The method is characterized by a continuous sequence of individual stages, which are optimally matched to each other in terms of equipment and energy consumption, is harvested by obtaining pure alumina, satisfying the requirements of many aluminum industry, recycling the resulting by-products and, therefore, is a method that has a positive effect on the environment.  Example.  Rough clay from a mine with a moisture content of 2O-24% is subjected to preliminary mechanical processing using semi-wet technology (1), which consists in coarse crushing of the ore mass in knife roller crushers, in the subsequent fine grinding and homogenization in wet-runners with a separator and casting the desired shape on a device for wiping clays or on a press.  0 After drying (2) with on /. Clay of the following composition, weight,  %: 30.6-34.0 45.1-46.4 2.40-2.65 2.05-2.20 0.018-0.024 0.05-0.15 Losses during 12.2-13.6 calcinations Then the material enters the thermal activation (3) at 600-80 ° C.  | One ton of ка-calcined clay obtained in this stage with a grain size of 0-2 O (preferably O-10 mm), after sifting off the fine fraction to 2 mm, is subjected to a circulation leach according to the circulation principle (5), and 1 t of this clay has the following composition, kg: Ae2. 0z380.0, 8, 8. O0.6 CaO2.7. 16.4 (50.6 6:10 a549.0 8O-9O% alumina containing in clay is easily leachable.  The clay is placed in the reaction vessel of the percolation leaching apparatus, adding 3342 L of 20% hydrochloric acid in the amount of 9O% stoichiometric demand (as for alumina), leached for 8 hours at the boiling point 1O5-HO C.  As a result, 2896 liters of crude aluminum solution are obtained, containing, kg: 820 50.3 28.6 and wash water.  Contains aluminum chloride, which are sent for the regeneration of hydrochloric acid (7).  In this stage, 1254 kg of cake are obtained with the following composition, kg: 5 FeaOj8.7 6i O, 549, OH O627.0, 5 Extraction of iron (jj) from the solution is carried out using an aliphatic amine secondary in an organic solution with respect to the organic phase to the aqueous phase 1: 2 of the following composition, ec.  %: Secondary gh alchfatiiyskikh aminov1O aliphatic higher alcohol30 Paraffin hydrocarbon6O.  The aqueous solution after extraction is practically free of iron and its composition remains unchanged.  The extraction of the organic phase from the organic phase is carried out in a volume of 361 l from the stages of a crystallization pack with a 5: 1 ratio of the organic phase and the aqueous phase, with an aqueous reextract of 48 g / l gel; The purified aluminum chloride solution in vacuum evaporators (12) is evaporated to saturation.  2175 l of a saturated solution of aluminum chloride and 734 l of a weakly acid condensate of steam are obtained.  One stripped off solution of the following composition, wt.  %: A SEG29.00 MaSvr, 2O KSe-L, 5O SASEO. 0.2 5, 012 SiOi, 0.003 TiCCi0.003. .  enters crystallization (12).  In this stage, 1470 kg of crystallisate, 1234 l of condensate of evaporation, practically free lOT HCP, and 163 l of ejected mother liquor are obtained.  After washing in a centrifuge with an evaporated solution of aluminum, crista lysate contains, by weight.  %: O, 025 0.0014 0, OOOZ 0.0003 0, OOO4 Crystallized undergoes a two-stage thermal decomposition (13) at the simultaneous chlorinating sublimation of the mixtures in order to obtain 270 kg of alumina containing,%: era3O, O2 5iOa0.01 , 06 kgO0.07 CaO0.03. 0,003 VaP50,008 Angle o (. tist (p | 1th otkosE is.  With solorzhlini at, -glololomp more than 8O%, a bumper surface l / 2O m / g is obtained, an apparent density of 7 0.55 g / cm.  The alumina obtained by the proposed method, in its quality satisfies the T1x boiling, presented by the aluminum industry.  From the gases from the decomposition process in the acid recovery unit (7), the hydrochloric acid is again extracted by leaching from the adiabatic absorption of hydrogen chloride.  Also, leaching solutions are used in leaching in two stages (5.9) and part of the weakly acidic condensates of evaporation from the evaporation process (12) of the extracted solution of aluminum chloride before crystallization.  The total alumina extraction method is 71%.  Claim 1.  The method of obtaining pure alumina by hydroacid leaching of mechanically and thermally activated clay or alumina minerals with separation of insoluble cake, removal of iron from the solution by crystallization of aluminum chloride, thermal decomposition of crystallized alumina, regeneration of hydrochloric acid from gases from the decomposition process, distinguished by the fact that , raw materials in several successive stages are subjected to preliminary mechanical processing, as well as mechanical or thermal activation, so about contained therein alk mini oxide is transferred to the acid-form; mechanically or thermally activated material, depending on the grain size, is subjected to either percolation leaching according to the circulation principle in case of a predominance of a fraction greater than 2 mm gph, maximum grain size of 5-10 mm, or suspension leaching in the case of a predominance of a fraction less than 2 mm in size using 20- 25% hydrochloric acid solution, and the stoichiometric amount of hydrochloric acid in relation to the content of alumina in the clay is 80-12 O% and works at the boiling point of 105 d And the pulp obtainable thereby, is supplied to the separation of solid and liquid phases, such as, e.g., at 1X azhdenie and / or filtration, the filtrate goes to op zhidkostnozhidkostnuyu extraction ganic ex counterparties, e.g., based on secondary.    aliphatic amines or neutral ether phosphoric acid. obtained by extraction solution having an aluminum chloride content of 20 wt.  %  and iron 2O mg / l is evaporated in one or several steps to a concentration of 30% by weight.  %, and the extracted and one stripped off solution is subjected to single-stage or multi-stage crystallization at 65-110 ° C and pressure 0.1-1.0 atm; the crystallization is carried out in such a way as to obtain high-purity crystals with an optimal composition and physical properties that meet the requirements imposed on the quality of the alumina obtained; the resulting crystallisate is then subjected to a two-stage thermal decomposition process, consisting of a partial decomposition stage at 150-DEPC and a complete decomposition stage at 1200-1350 ° C, and the resulting off-gases containing hydrogen chloride are absorbed to obtain hydrochloric acid, in circulation during leaching. .
    [2]
    2. A method according to claim 1, characterized in that the pre-mechanical treatment and thermal activation of the wire is performed so as to obtain a material with a grain size from 2 to 10 mm, suitable for percolation leaching, and oxide solubility aluminum in hydrochloric acid is higher than 8O%.
    [3]
    3. A method according to claim 1, characterized in that as a result of the essence combined with grinding, as well as as a result of subsequent thermal activation, a material with a size of 0.5 mm, suitable for suspension leaching, and solubility is obtained 80% aluminum oxide in hydrochloric acid ..
    [4]
    4. A method according to claim 1, wherein the method is that by mechanically activated material with a grain size of 0.5 mm, suitable for slurry leaching, and with Solubility of alumina in hydrochloric acid is higher than 80%.
    [5]
    5. The method according to claim 1, wherein the thermal activation is carried out predominantly in the temperature range from 700 to 80 ° C according to the principle of the fluidized bed, with observance of a sufficient temperature constant, i.e. The optimum temperature is not lowered and does not increase; a long enough treatment ensures oxidative destruction of organic impurities.
    [6]
    6. Method according to paragraphs. 1-5, characterized in that the leaching, depending on the grain size, is carried out either in a fixed bed with the circulation of the solvent, or in suspension.
    [7]
    7. Method according to paragraphs. 1-6, characterized in that, in order to fully hydrolyze the primary dissolved titanium, the leaching uses a predominantly stoichiometric amount of hydrochloric acid in relation to the initial amount of alumina 100%.
    [8]
    8. Method according to paragraphs. 1-7, differing from the fact that as compared to the pure initial suspension, as a result of using flocculants based on polyacrylamides, in the range of 10-100 g / m, the deposition rate doubles and the filter capacity rises by 2% 100%.
    [9]
    9. Method according to paragraphs. 1-8, Tl and Chaus, so that the silica cake obtained after leaching is used, for example, in the construction industry as a supplement for the production of lightweight concrete or is processed appropriately for other purposes, such as glass or fillers.
    [10]
    10. Method according to paragraphs. 1-9, characterized in that a solution containing 5-15% by weight of a secondary aliphatic amine, 20 -40% by weight is used as an extractant. % aliphatic alcohol, and the balance of aliphatic hydrocarbons, preferably paraffinic hydrocarbons, in the range of boiling temperatures of 145-200 ° C, the ratio of which to the aqueous phase containing 190-280 g / l of chloride is from 1: 1 to 1: 5, extraction It is carried out at a temperature of 254 ° C, and when iron is reextricted, the ratio of the organic phase to the aqueous phase is from 3: 1 to 7: 1, and the aqueous phase of reextraction contains 1 O-4O g / l of hydrochloric acid, preferably 20 g / l.
    [11]
    11. Method according to paragraphs. 1-9, characterized in that the extractant used is a solution of tributylfsfat with respect to the aqueous phase from 1: 2 to 1: 3 and that the iron is extracted from its solution at a ratio of the organic phase to the aqueous phase from 4: li to 6: 1, and an aqueous solution of reextraction.
    179C9G
    contains lO-IO g / l of hydrochloric acid, preferably 20 g / l.
    [12]
    12. Method according to paragraphs. 1-11, characterized in that the aqueous solution from the stripping process is processed to produce gallium radiation, high-purity iron oxide is obtained by thermal decomposition, and gases from decomposition containing hydrogen chloride are directed to the regeneration of hydrochloric acid.
    [13]
    13. Method according to paragraphs. 1-12, characterized in that the crystallization is carried out with a forced circulation of the suspension of crystals, the purity of the crystallized product is obtained by washing with an initial solution with a low content of impurities, and by centrifuging, crystallized with a low residual moisture is obtained.
    [14]
    14. Method according to paragraphs. 1-13, that is, a-2ccc, and so that the clarified mother liquor in a volume of 1-7% is removed to remove impurities from the mold
    (in relation to the amount of the freshly prepared solution introduced) and lererabaty-2 $ it is cast onto rough alumina.
    7018
    [15]
    15. Method according to paragraphs. 1-1.4, about tl and hrrrrrrrrrrr. With the fact that the intermediate product from the stapia of the partial decomposition with a gentle temporarum traces such a composition that allows the reaction gases to get at least as high as the thermal decomposition stage. . hydrogen chloride in order to maximize the distillation of the original impurities.
    [16]
    16. Method according to paragraphs. 1-15, characterized in that the exhaust gas from the low-temperature decomposition stage is subjected to fine purification and the main amount of volatilized impurities is removed with the resulting dust.
    [17]
    17. Method according to paragraphs. 1-16, characterized in that the waste gases containing chloride of matter are preferably converted by adiabatic adsorption to 15-TH 30% recycle hydrochloric acid.
    Recognized as an invention according to the results of the examination carried out by the Office for the Invention of the German Democratic Republic
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    同族专利:
    公开号 | 公开日
    HU184690B|1984-09-28|
    DD147185A3|1981-03-25|
    US4224287A|1980-09-23|
    DE2906646C2|1987-06-19|
    DE2906646A1|1979-10-31|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DD78204962A|DD147185A3|1978-04-24|1978-04-24|METHOD FOR PRODUCING PURE ALUMINUM OXIDE|
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