Some Studies in the System AlCl3-FeCl3-KCl-NaCl-HCl-H2O at 25, 30 and 35°

Miles, G.L.

doi:10.1021/ja01199a042

Cited by 7 publications

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“…The temperature of the Al chloride liquor and the HCl content are the two most important parameters of the salting-out process, which affect both the precipitation of the main impurities (Fe, Ca, Na, and K) and the yield of the ACH crystals [32,33]. It was found that the temperature of the liquor does not significantly affect the ACH solubility.…”

Section: Ach Precipitationmentioning

confidence: 99%

Acid and Acid-Alkali Treatment Methods of Al-Chloride Solution Obtained by the Leaching of Coal Fly Ash to Produce Sandy Grade Alumina

Valeev

Shoppert

Михайлова

2020

Metals

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Sandy grade alumina is a valuable intermediate material that is mainly produced by the Bayer process and used for manufacturing primary metallic aluminum. Coal fly ash is generated in coal-fired power plants as a by-product of coal combustion that consists of submicron ash particles and is considered to be a potentially hazardous technogenic waste. The present paper demonstrates that the Al-chloride solution obtained by leaching coal fly ash can be further processed to obtain sandy grade alumina, which is essentially suitable for metallic aluminum production. The novel process developed in the present study involves the production of amorphous alumina via the calcination of aluminium chloride hexahydrate obtained by salting-out from acid Al-Cl liquor. Following this, alkaline treatment with further Al2O3 dissolution and recrystallization as Al(OH)3 particles is applied, and a final calcination step is employed to obtain sandy grade alumina with minimum impurities. The process does not require high-pressure equipment and reutilizes the alkaline liquor and gibbsite particles from the Bayer process, which allows the sandy grade alumina production costs to be to significantly reduced. The present article also discusses the main technological parameters of the acid treatment and the amounts of major impurities in the sandy grade alumina obtained by the different (acid and acid-alkali) methods.

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Section: Ach Precipitationmentioning

confidence: 99%

Acid and Acid-Alkali Treatment Methods of Al-Chloride Solution Obtained by the Leaching of Coal Fly Ash to Produce Sandy Grade Alumina

Valeev

Shoppert

Михайлова

2020

Metals

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“…Ref studied the phase equilibria of AlCl 3 –FeCl 2 –H 2 O under different temperature in neutral conditions for Al 3+ and Fe 2+ , a new chemical model was developed for the Al 3+ –Fe 2+ –Mg 2+ –Ca 2+ –K + –Cl – –H 2 O system, providing a new method for the efficient separation of aluminum chloride hexahydrate. To obtain alumina from the acid leaching system of calcined alum, ref studied the AlCl 3 –FeCl 3 –KCl–HCl–H 2 O system and the AlCl 3 –FeCl 3 –KCl–NaCl–HCl–H 2 O system at different temperatures for the removal of Ca 2+ , ref reported the phase equilibria of AlCl 3 –H 2 O and AlCl 3 –CaCl 2 –H 2 O at different temperatures and the thermodynamics for the separation of calcium and aluminum from calcium-rich fly ash leaching solution in combination with Pitzer theory. Refs , studied the phase equilibria of AlCl 3 –CaCl 2 –H 2 O at 298.15 and 308.15 K under neutral conditions; based on the solubility data, the phase diagram of the ternary system AlCl 3 –CaCl 2 –H 2 O was plotted.…”

Section: Introductionmentioning

confidence: 99%

Phase Diagram of AlCl₃–FeCl₃–H₂O(−HCl) Salt Water System at 298.15 K and Its Application in the Crystallization of AlCl₃·6H₂O

Cheng

Cao

et al. 2019

J. Chem. Eng. Data

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Aluminum–ferric separation has attracted significant interest in the field of hydrometallurgy. Using phase equilibria theory, fractional crystallization and separation of a mixed salt solution is a relatively effective method. The phase equilibria of the ternary system or tertiary system AlCl3–FeCl3–H2O(−HCl) at 298.15 K for different H+ concentrations were studied using the isothermal dissolution equilibrium method, and plotted the corresponding phase diagrams and density diagrams. The experimental results show that with increasing H+ concentration, the solubility of AlCl3 decreased from 31.20 to 0.13%, and the crystallization region of AlCl3·6H2O gradually increased. H+ concentration had little influence on FeCl3 solubility, and the solubility of FeCl3 was 47.52%. Through theoretical calculations, the desired amount of water to evaporate and crystal precipitation can be obtained through the calculation model for the system composed of different materials. The route is designed by the phase equilibrium and the phase diagram theory, and the separation of aluminum and ferric from aluminate acid leaching solution of coal gangue in literature. The direct yield of AlCl3·6H2O obtained by evaporation and crystallization was 77.15%, and the purity reached 99.81% after rinsing with concentrated hydrochloric acid.

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“…There are at least three possible solutions to this problem, which could be used singly or together. Examination of the original solubility work for this system suggests that it might be possible to separate NaCl from AICI3 by crystallizing NaCl using a 10-llM HCl (42).…”

Section: Aici3mentioning

confidence: 99%

Carbochlorination of metal oxides using a fused salt slurry reactor

Dobbins

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Physical properties 13 Chemical properties 15 Reaction Mechanism 16 Fused Salt Chlorination of Other Metals 17 Titaniferrous ores 18 Oxide chlorination study 18 SLURRY REACTION CHARACTERSTICS 20 Carbochlorination of a Pure Oxide 20 Mixed Oxides 26 EXPERIMENTAL EQUIPMENT AND PROCEDURES 29 Aluminum Chloride Purification 29 Fly Ash Solubility Experiments 31 Fused Salt Chlorination Experimental Design 33 Chlorination Equipment 34 ill Reactor 34 Metal chloride condensers 42 Noncondensable gas analysis 43 Chlorination Experimental Procedure 47 Analytical Procedures 50 Analysis of slurry samples 50 Chemical analysis 50 Particle size analysis 52 Reactant Characteristics 53 Alumina 53 Fly ash 55 Carbon sources 55 RESULTS AND DISCUSSION 58 Alumina Chlorination Screening Study 58 Experimental procedure 59 Alumina loading and melt composition effects 60 Carbon loading and chlorine flow rate effects 64 Temperature effects 65 Summary Temperature Dependence Reaction profiles Arrhenius analysis Mechanism versus temperature Chlorine side reactions Process considerations Chlorine sparger plugging Summary Mechanism Experiments 81 Coke impurities 81 Alumina-carbon prechlorination reaction 83 Carbon prechlorination 88 Summary 91 Carbon Loading and Surface Area Effects 91 Carbon particle reaction 97 Summary 101 Reaction Rate Versus Stirrer Speed 102 iv Proposed Reaction Mechanism 104 CO formation 108 Summary 109 Effect of NaCl-AlClg Melts on Fly Ash 109 Summary 114 Fused Salt Chlorination of Fly Ash 114 Major component chlorination 115 Minor component chlorination 122 Reactivity of mineral phases in fly ash 125 SEM micrographs 127 Comparison to gas-solid chlorination 132 FUSED SALT CHLORINATION PROCESS 135 Fused Salt-Gas-Solid Reaction Comparison 135

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Some Studies in the System AlCl₃-FeCl₃-KCl-NaCl-HCl-H₂O at 25, 30 and 35°

Cited by 7 publications

References 0 publications

Acid and Acid-Alkali Treatment Methods of Al-Chloride Solution Obtained by the Leaching of Coal Fly Ash to Produce Sandy Grade Alumina

Acid and Acid-Alkali Treatment Methods of Al-Chloride Solution Obtained by the Leaching of Coal Fly Ash to Produce Sandy Grade Alumina

Phase Diagram of AlCl₃–FeCl₃–H₂O(−HCl) Salt Water System at 298.15 K and Its Application in the Crystallization of AlCl₃·6H₂O

Carbochlorination of metal oxides using a fused salt slurry reactor

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Some Studies in the System AlCl3-FeCl3-KCl-NaCl-HCl-H2O at 25, 30 and 35°

Cited by 7 publications

References 0 publications

Acid and Acid-Alkali Treatment Methods of Al-Chloride Solution Obtained by the Leaching of Coal Fly Ash to Produce Sandy Grade Alumina

Acid and Acid-Alkali Treatment Methods of Al-Chloride Solution Obtained by the Leaching of Coal Fly Ash to Produce Sandy Grade Alumina

Phase Diagram of AlCl3–FeCl3–H2O(−HCl) Salt Water System at 298.15 K and Its Application in the Crystallization of AlCl3·6H2O

Carbochlorination of metal oxides using a fused salt slurry reactor

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Some Studies in the System AlCl₃-FeCl₃-KCl-NaCl-HCl-H₂O at 25, 30 and 35°

Phase Diagram of AlCl₃–FeCl₃–H₂O(−HCl) Salt Water System at 298.15 K and Its Application in the Crystallization of AlCl₃·6H₂O