Method for recovering metal chlorides from silicon or ferrosilicon alloys which have been reacted with chlorinating agents

Abstract: A method for recovering iron chloride, aluminium chloride and calcium chloride from silicon and ferrosilicon or from residues which contain silicon and/or ferrosilicon and metal chlorides and optionally copper and/or copper compounds. These materials are leached with CHl or CHl + FeCl₃/FeCl₂ solution, whereafter the solid silicon or ferrosilicon residue is removed from the leach solution together with any copper. Fe²⁺ in the leach solution is then oxidised to Fe³⁺ whereafter the leach solution is subjected to liquid-liquid extraction by means of an organic phase containing n-tributyl phosphate dissolved in a hydrocarbon solvent in order to extract FeCl₃ and at least a part of any CaCl₂ from the leach solution. FeCl₃ and any CaCl₂ are stripped from the organic phase by water and the remaining solution is concentrated by evaporation and adding HCl gas to the solution in order to selectively precipitate AlCl₃.6H₂O and AlCl₃.6H₂O is then recovered from the solution by filtration.

Description: The present invention relates to a method for recovering metal chlorides from silicon and ferrosilicon alloys which have been reacted with chlorinating agents. By the reaction of particulate ferrosilicon containing about 90-96% by weight of silicon with a leaching solution containing FeCl 3 /HCl, pure granular silicon is produced and metallic impurities in the raw materials, mainly Fe, Al and Ca are dissolved in the leach solution. This process for producing pure silicon is described in US patent No. 3,809,548. The leach solution from this process which contains a large amount of dissolved metal chlorides, particularly Fe, Al and Ca chloride, has up till now been disposed of. However, due to environmental reasons, it will no longer be acceptable to dispose of these kinds of metal chloride-containing leach liquors. The same kind of metal chloride containing-leach liquors can be produced from the residues from other processes. Thus, by the reaction of ground or lumpy silicon or ferrosilicon with chlorine gas or gaseous HCl in reactors for the production of chlorosilanes, preferably trichlorosilane or tetrachlorosilane, impurities contained in the silicon or the ferrosilicon raw material, mainly Fe, Al and Ca are accumulated mainly as chlorides in silicon-containing residues in the reactors. These residues, which mostly contain residual silicon or silicon alloys, together with the above mentioned metal chlorides and carbon, have so far also been disposed of. However, for environmental reasons, it will no longer be acceptable to dispose of these residues on normal disposal sites. These residues can, however, be leached by FeCl 3 /HCl solutions to produce a valuable silicon containing material and a leach solution containing metal chlorides. The silicon containing material can be used as a silicon source in different metallurgical processes. Finally, a metal chloride containing residue is produced by the reaction of silicon powder with alkylchloride, particularly methylchloride for producing alkylchlorosilanes. In this process copper or a copper compound is used as a catalyst. Also in this process, silicon based residues are produced which contain metal chlorides originating from impurities in the materials. The residue will, in addition, contain copper and copper compounds originating from the catalyst. It is known to recover copper values from this residue by subjecting the residue to a leaching process using mineral acids, particularly HCl, whereby copper and most of the metal chlorides are dissolved and where copper is recovered from the leach solution by, for example, cementation. The leach solution after copper has been removed does, however, contain a number of dissolved metal chlorides, such as Fe and Al. Moreover it is known from CA 102, 14,1985, 118116m, that iron values may be recovered from HCl containing waste liquids. The known process involves an oxidation step so to convert the iron content into iron-III-chloride, transferring the said iron chloride into an organic phase containing tributyl phosphate and stripping the iron chloride from the organic phase using water. It is an object of the present invention to provide a method for treating the above-mentioned metal chloride containing residues and leach solutions in order to recover iron chloride, aluminium chloride and at least a part of any calcium chloride present in the form of valuable products and to obtain a final solution having a very small volume compared to the starting solution. Accordingly, the present invention provides a method for recovering iron chloride, aluminium chloride and/or calcium chloride from materials in the form of silicon and ferrosilicon or from residues which contain silicon and/or ferrosilicon and metal chlorides and optionally copper and/or copper compounds, in which the materials are leached with HCl or HCl + FeCl 3 /FeCl 2 solutions, and thereafter the solid silicon or ferrosilicon residue is removed from the leach solution and any copper is removed from the leach solution, characterised by the steps of: oxidising Fe 2+ in the leach solution to Fe 3+ ; subjecting the leach solution to a liquid-liquid extraction by means of an organic phase containing n-tributyl phosphate dissolved in a hydrocarbon solvent, in order to extract FeCl 3 and at least a part of any CaCl 2 from the leach solution; stripping FeCl 3 and any CaCl 2 from the organic phase using water, concentrating the remaining solution by evaporation and adding HCl gas to the solution in order to precipitate AlCl 3 .6H 2 O selectively from the solution; and recovering AlCl 3 .6H 2 O from the solution by filtration. Preferably, the oxidation step is carried out by treatment with hydrochloric acid and chlorine gas. Preferably, the liquid-liquid extraction is conducted in a plurality of mixer-settler stages operating under counter-current flow conditions. By the present invention, the Fe and at least a part of the Ca are recovered in the form of a FeCl 3 -solution having a high Fe-concentration. The FeCl 3 solution obtained generally has a Fe 3+ concentration of above 100g/l. The FeCl 3 solution can be used for example in municipal sewage treatment plants as a flocculating agent. It has been found that better results can be obtained by using a FeCl 3 solution containing some CaCl 2 as a flocculating agent rather than by using a pure FeCl 3 solution. The AlCl 3 .6H 2 O is washed with water and preferably dissolved in water or in HCl in order to obtain AlCl 3 solutions which can be used for example in municipal sewage treatment plants as a flocculating agent. The residual solution after removal of Fe and Al has generally a total iron content of less than 5 g/l and an aluminium content of less than 5 g/l. The volume of this residual solution is very small compared to the volume of the starting solution, and may if it is further concentrated by evaporation have a volume which is less than 10% of the volume of the starting solution. This residual solution can in most instances be deposited after having been neutralised. The present invention may be carried into practice in various ways and some embodiments will now be described in the following examples. EXAMPLE 1 A leach solution from a process for leaching of metallurgical grade, 93.5% ferrosilicon with a HCl + FeCl 3 solution had the following composition: Fe 3+ : <1 g/l Fe 2+ : 85 g/l Al 3+ : 45 g/l Ca 2+ : 12 g/l HCl : 35 g/l Fe 2+ in this solution was oxidised to Fe 3+ by adding HCl and using chlorine gas. The oxidised solution had the following composition: Fe 3+ : 85 g/l Fe 2+ : <1 g/l Al 3+ : 45 g/l Ca 2+ : 12 g/l HCl : 60 g/l The oxidised solution was mixed with an organic phase comprising 40% n-tributyl phosphate (TBP) dissolved in an aromatic hydrocarbon solvent in order to extract Fe 3+ and a part of Ca 2+ from the leach solution. The extraction was carried out in four mixer-settler stages operated with counter-current flow. Fe 3+ extracted to the organic phase was thereafter stripped by contacting the organic phase with water in four mixer-settler stages with counter-current flow. An aqueous Fe 3+ solution was thus obtained, containing 110 g/l Fe 3+ and 10 g/l Ca 2+ . The Fe 3+ solution obtained can be used for example in municipal sewage treatment plants as a flocculating agent. The raffinate from the extraction step had the following composition: Fe 3+ : <2 g/l Fe 2+ : <1 g/l Al 3+ : 45 g/l Ca 2+ : 4 g/l HCl : 15 g/l This solution was subjected to evaporation and HCl gas was added in order to precipitate aluminium in the form of aluminium chloride hexahydrate which thereafter was filtered from the solution and washed with water. The aluminium chloride hexahydrate crystals had the following composition: Fe total : <0,01 grams pr. kg AlCl 3 .6H 2 O Al : 95 grams pr. kg AlCl 3 .6H 2 O The aluminium chloride hexahydrate crystals can be dissolved in water and used for example in municipal sewage treatment plants as a flocculating agent. The residual solution after precipitation of aluminium had the following composition: Fe total : <2 g/l Al 3+ : <2 g/l Ca 2+ : 4 g/l HCl : 390 g/l This residual solution can either be disposed of after recovering HCl or it can be further purified. EXAMPLE 2 Silicon-containing residue from a process where 96% silicon has been reacted with HCl gas at elevated temperature, was leached with a solution containing hydrochloric acid, aluminium chloride and FeCl 3 /FeCl 2 . The composition of the acid after leaching was as follows: Fe 3+ : <1 g/l Fe 2+ : 80 g/l Al 3+ : 45 g/l HCl : 15 g/l Hydrochloric acid and chlorine gas was added to the solution to oxidise ferrous chloride to ferric chloride. The oxidised solution had the following composition: Fe 3+ : 80 g/l Fe 2+ : <1 g/l Al 3+ : 45 g/l HCl : 60 g/l This solution was mixed with an organic phase comprising 40% n-tributylphosphate (TBP) in an aromatic hydrocarbon solvent in order to extract Fe 3+ from the solution. The extraction was carried out in four mixer-settler stages operated with counter-current flow. Fe 3+ extracted to the organic phase was thereafter stripped by contacting the organic phase with water. An aqueous Fe 3+ solution was thus obtained, containing 110 g/l Fe 3+ . The Fe 3+ solution obtained can be used for example in municipal sewage treatment plants as a flocculating agent. The raffinate from the extraction step had the following solution: Fe 3+ : <2 g/l Fe 2+ : <1 g/l Al 3+ : 45 g/l HCl : 15 g/l This solution was subjected to evaporation and HCl gas was added in order to precipitate aluminium in the form of aluminium chloride hexahydrate which thereafter was filtered from the solution and washed with water. The aluminium chloride hexahydrate crystals can be dissolved in water and used for example in municipal sewage treatment plants as a flocculating agent. The residual solution after precipitation of aluminium had the following composition: Fe total : <2 g/l Al 3+ : <2 g/l HCl : 380 g/l This residual solution can either be disposed of or can be further purified. EXAMPLE 3 Silicon-containing residue from a process where metallurgical grade silicon metal has been reacted with methylchloride in the presence of a copper catalyst was leached with a solution containing hydrochloric acid, aluminium chloride and FeCl 3 /FeCl 2 . The composition of the acid after leaching had the following composition: Fe 3+ : <1 g/l Fe 2+ : 65 g/l Cu 2+ and Cu + : 15 g/l Al 3+ : 45 g/l HCl : 15 g/l The copper in the solution was removed from the solution by cementation on iron. After adding iron to the solution the cemented copper and any residual elemental iron was filtered from the solution. The filtrate had the following composition: Fe 3+ : <1 g/l Fe 2+ : 80 g/l Cu 2+ and Cu + : <0.1 g/l Al 3+ : 45 g/l HCl : 15 g/l Hydrochloric acid and chlorine gas was added to the solution to oxidise ferrous chloride to ferric chloride. The oxidised solution had the following composition: Fe 3+ : 80 g/l Fe 2+ : <1 g/l Cu 2+ : <0.1 g/l Al 3+ : 45 g/l HCl : 60 g/l This solution was mixed with an organic phase comprising 40% n-tributyl phosphate (TBP) in an aromatic hydrocarbon solvent in order to extract Fe 3+ from the solution. The extraction was carried out in four mixer-settler stages operated with counter-current flow. Fe 3+ extracted to the organic phase was thereafter stripped by contacting the organic phase with water. An aqueous Fe 3+ solution was thus obtained containing 110 g/l Fe 3+ . The Fe 3+ solution obtained can be used for example in sewage treatment plants as a flocculating agent. The raffinate from the extraction step had the following composition: Fe 3+ : <2 g/l Fe 2+ : <1 g/l Cu 2+ : <0.1 g/l Al 3+ : 45 g/l HCl : 15 g/l The solution was then subjected to evaporation and HCl gas was added in order to precipitate aluminium in the form of aluminiumchloride hexahydrate which thereafter was filtered from the solution and washed with water. The aluminiumchloride hexahydrate crystals can be dissolved in water and used for example in municipal sewage treatment plants as a flocculating agent. The residual solution after precipitation of aluminium had the following composition: Fe total : <2 g/l Cu 2+ : <0.1 g/l Al 3+ : <2 g/l HCl : 380 g/l This residual solution can either be disposed of or can be further purified.

Claims: A method for recovering iron chloride, aluminium chloride and/or calcium chloride from materials in the form of silicon and ferrosilicon or from residues which contain silicon and/or ferrosilicon and metal chlorides and optionally copper and/or copper compounds, in which the materials are leached with HCl or HCl + FeCl 3 /FeCl 2 solutions, and thereafter the solid silicon or ferrosilicon residue is removed from the leach solution and any copper is removed from the leach solution, characterised by the steps of: oxidising Fe 2+ in the leach solution to Fe 3+ ; subjecting the leach solution to a liquid-liquid extraction by means of an organic phase containing n-tributyl phosphate dissolved in a hydrocarbon solvent, in order to extract FeCl 3 and at least a part of any CaCl 2 from the leach solution; stripping FeCl 3 and any CaCl 2 from the organic phase using water, concentrating the remaining solution by evaporation and adding HCl gas to the solution in order to precipitate AlCl 3 .6H 2 O selectively from the solution; and recovering AlCl 3 .6H 2 O from the solution by filtration. A method as claimed in Claim 1, characterised in that the oxidation step is carried out by treatment with hydrochloric acid and chlorine gas. A method as claimed in Claim 1 or Claim 2, characterised in that the liquid-liquid extraction is conducted in a plurality of mixer-settler stages operating under counter-current flow conditions. A method as claimed in any of Claims 1 to 3, characterised in that the Fe 3+ solution produced in the stripping step has a Fe 3+ content of at least 100 g/l. A method as claimed in any of Claims 1 to 4, characterised in that the AlCl 3 .6H 2 O produced is dissolved in water or an HCl-solution to produce an AlCl 3 -solution.

Inventors: ANDERSEN EINAR, CECCAROLI BRUNO, GUNDERSEN ROALD, ANDERSEN, EINAR, CECCAROLI, BRUNO, GUNDERSEN, ROALD
Applicants: ELKEM MATERIALS, ELKEM ASA
Application year: 1995
Main classification: C01B33
IPC codes: C01G49, C01B33, C01F7, C01B9, C01F11