PROCESS FOR PRODUCING METALLIC CHLORIDES

Abstract: Metallic chlorides are obtained from complex com­ pounds by reacting the latter, at a high temperature (1800°C-­ 2500°C) with gaseous chloride in a reaction zone, under reducing conditions, in the interior of a reactor packed with solid reducing material in lumps. The chlorides are obtained in the vapour phase and separated.

Description: PROCESS FOR PRODUCING METALLIC CHLORIDES This invention relates to a process for the production of metallic chlorides. More particularly, this invention relates to a process for the production of metallic chlorides from compounds of metals, which contain oxygen, also in the form of complex salts or oxides of various metals. Still more particularly, the present invention relates to a process for producing metallic chlorides starting from said compounds, when the latter are present in organic and/or inorganic inert materials at concentrations lower than iso%. Metals occur in nature in complex chemical and mineralogical forms because of the gradual exhaustion of the primary sources which were particularly pure and simple from a structural standpoint, such sources having hitherto been preferentially exploited both due to the high purity (as a matter of fact impurities are a depreciation factor for the ore) and because of the demand by the metallurgical factories due to the tecnological characteristics and the yields of the extraction processes available. At the same time, at present, the trend is towards recovering metals from the so-called secondary materials such as ore residues, metallurgic industry scraps, industrial scraps, industrial scraps of various origin; also in this case, materials are encountered in which more metals are present under various chemical forms, which can also be complexes, The problem, thus, is to find out metallurgical treatments which are capable of recovering metals from materials which contain same in a chemical form which is more or less complex and in association with other metals which are otherwise interesting and also to find processes for separating the several metals from each other by single-step operations and/or treatments which are efficient and are technologically reliable. In the light of these considerations, special attention deserve the chlorination runs, in which the metals which are contained in the materials to be treated are converted into chlorides, which, in their turn, are withdrawn from a reactor in the vapour state and thereaftercondensed, to be subjected to other subsequent physical processes to achieve their separation, such as fractional distillation and condensation, and chemical operations for extracting them, such as a shift of the metal one desires to extract in the chloride salt by means of another metal which has a greater affinity towards chlorine than the metal be extracted, or the electrolysis of the melted chloride. At present, the chlorination technology is used for primary pure raw materials (such as titanium from rutile), possibly coming from purification treatments, as is the case with alumina, but for complex materials this technology is not yet in use. The pyrometallurgical reactors in use at present never exceed temperatures of 9000C - 10000C so that the mechanism of cleaving the bonds between the several oxides and the subsequent chlorination reaction in a reducing environment of such oxides never attains kinetic characteristics of commercial interest and in some cases it proves even impossible to provide the industrial technological conditions which are required for carrying out the chlorination reaction. On the other hand it is not permissible to raise the temperature when working according to the known tecnology because of the chemical attack broughtabout by chlorine towards the refractory materials, which, due to the combined action of chlorine and heat collapse after a very short time. Quite surprisingly, is has been found that the difficulties or even impossibilities of the conventional art can easily be circumvented by carrying out the chlorination step at a temperature above 15000C, preferably 18000C -25000C and over, within a reaction zone provided with a packing of a solid reducing material. The process according to the present invention consists in reacting the metallic compounds, either alone or in admixture with inert organic and/or inorganic materials, with chlorine or substances which evolve chlorine under the reaction conditions, at a temperature above 15000C, preferably 18000C-25000C and over, in a reaction zone providing reducing conditions in the interior of a reactor packed with a solid reducing material in lump form, preferably a lumped solid reducing material which contains carbon, coke being preferred, whereby the chlorides of the metals which have been introduced are obtained in the vapour phase1 discharging the chlorinated metals through the reactor head, separating the chlorides of the several metals from each other by fractional condensation (at different temperatures) and/or with other conventionally known means. The heat which is necessary for carrying out the reaction is supplied by a burner, which is, preferably, of the arc-plasma type. The metallic compounds to be fed to the reaction zone be used according to the present invention, either alone or in admixture with inert materials, are,preferably, the alumino-silicates of the alkali metals and/or the alkaline earth metals and, among the latter and more particularly, the ores known under the names of leucite, alumite, the silicates of the metals of the Groups III and/or IV and/ or V of the Periodic System of the Elements and, preferably, the silicates of Zr, Ti, Mo, W, Pb, Zn, the aluminates; the titanates, the zirconates and such like. The reaction zone has preferably the formof a vat and the advantages which can be achieved with the process according to this invention are, in summation, the following 1) The reaction takes place at a high temperature, the reactor walls being shielded by the lumped solid reducing m; 2) The reaction takes place with a wide contact surface between the reactants as provided by the lumped solid reducing material packing; 3) The bed of solid reducing material can be brought to a temperature above the condensation temperature of the highest-boiling chloride, or, still better , above the condensation temperature of the mixture of chlorides in the vapour phase, whereby the chlorides can conveniently be discharged through the top of the reaction zone. The invention is better illustrated in detail hereinafter with reference to the accompanying drawing which must not be intended as a limitation of the invention, In the drawing, a reactor, 1, having the shape of a vat is packed with lumps of a solid reducing agent, preferably coke, which is renewed continuously by a cupola loader, 3, positioned at the reactor top. The coke column 2 has such a height as to prevent the chlorides in the gaseous phase from escaping through the reactor top instead of flowing through the pipe 12. Two level gauges, not shown, by interacting with the loading mechanisms (not shown), control the level of the coke column 2. Injections of nitrogen, moreover, prevent the chlorides coming from the vat from exiting the reducing material charge. The coke to be used is a conventional cupola metallurgical coke, preferably dried, to prevent water from interacting with the chlorides to produce oxidized compounds in the condensation stage. The lower section of the vat has pipes for introducing the charge and the chlorinating agent consisting of gaseous chlorine, the pipes being shown at 8 and 10. The charge 15 preheated with coke dust or another solid reducing agent and both the charge and the coke are peviously dried to prevent reactions of water and steam as outlined above and concurrently to prevent power consumption for drying in the reactor interior 1 and, finally, to provide a regular feed of the charge which should be fed at a grit size smaller than 5mm by pneumatic conveyors, the active fluid being the chlorinating agent itself. In addition, there is an arc-plasma burner 7 with its feeding pipings. In addition, the reactor bottom is provided with means for drawings the liquid phases, and such means are symbolically shown at 11. The reactor temperature is controlled and the heat which is required to provide the appropriate thermodynamic conditions is supplied by the plasma torch, to which the gas adapted to provide the reducing conditions is supplied, for example CO, which is necessary for the reactions and thus has the function of plasma gas. The material to be treated, which contains oxides or oxygen-containing compounds of any element, such as for example the oxides of alkaline earth metals and alkali me talus, of iron, titanium, tungsten, vanadium, cobalt, silicon, nickel, manganese, lead , zinc, molybdenum, ccpper, bismuth, aluminium, zirconium, rare earth, yttrium, cadmium, chromium, antimony, tin, other oxides of the metals of the Groups III, IV of the Periodic System, the oxides containing in the polymetallic nodules of marine origin, either alone or admixed or combined in salts or various compounds such as for example silicates, silicoaluminates, aluminates and such like, is blown into the reaction zone of the reactor 1, using chlorine itself as the driving fluid, and is rapidly heated in the reactor to react and form the gaseous chlorination products. It cannot be excluded that a liquid phase might be formed, which did not react and thus becomes a slag: these products are collected at the reactor bottom and are drawn through the spill holes indicated at 11. The reaction products, which are chlorides in the gaseous phase, rise to the oven top through the vat along the direction of the arrows and are withdrawn through the pipe 12. Coke provides a permeable layer through which the reacttion products can flow upwards whereas the slags and the liquid phases drop downwards, so that the coke bed has, in addition to those already mentioned in the foregoing, also the following functions,: a) to capture all the fine-grit material passing therethrough, and b) to provide a reducing environment for the chlorination reaction and, if so required, to act as a reducing agent as such, and to ensure that such functions are brought about all the vat height throughout. At any rate, with a view to saving metallurgical coke in lumps and avoid disturbing the coke bed itself with continuous addition of coke from the top, it is preferred to use a gaseous or a liquid hydrocarbon or solid coal so as to provide an agent which provides a reducing function Such reducing agents can be supplied by means of separate nozzles, or they can be fed together with the ore feed which contains the metallic compounds and thus also together with the chlorinating agent, the gaseous chlorine, or as a fraction of the plasma gas, or entirely as the plasma gas. Finally, it is also possible to feed CO with the charge and/or together with the plasma gas. At the exit from the vat, the gaseous chlorides, 12, flow into a hot cyclone, 6, to separate the coal .or other solid particles which have possibly been entrained, such solid phases, 9, being immediately recycled, whereafter the gaseous chlorides flow into a labyrinth condenser,4 consisting of a number of refractory-lined chambers having inlet ports staggered both in the vertical and the horizontal directions, each chamber having at its bottom a crucible of graphite of another refractory material having an appropriate magnetic susceptivity, which is optionally heated by an induction ring, each chamber being fitted with an inlet for a cold inert gas, such as nitrogen or cold recycle gas (temperature below 1000C). The function of the condenser 4 is to collect the liquid chlorides, but not the chlorides for which the possibility of formation of liquid phases is not predictable under normal conditions, such as for example the chlorides of zirconius,aluminium and nickel which, as is well known, vaporize without melting. Consequently, the temperature at the outlet 13 of the condenser 4 must be such as to prevent conditions favourable to the solidification of chlorides within such condenser: it is for this purpose that induction heaters have been provided in the chloride collecting crucibles of the several chambers so as to melt or vaporize possible incrustations. The chlorides which vaporize without melting, as mentioned above, or the vapours of those chlorides which have not yet been condensed, are solidified in the next condenser 5, which consists of a refractory-lined chamber having an inlet for a cold inert gas, two or more drums rotatable about an axis perpendicular to the direction of flow of the incoming gas/chloride stream and fitted with means for having water circulated internally thereof under pressure, doctor blades for scraping off the condensed chlorides from the drum surfaces, a conveying screw positioned at the bottom to withdraw the scales scraped off by the doctor blades and collected by the downward sloping chamber walls. The chlorides are discharged through 15. In the outlet 14 there could be left a few low-boiling chlorides, such as for example silicon tetrachloride, to be sent to a conventional cooling section or, directly in its gaseous phase, to the next metal recovery treatment. The gas which is left after the condensations, supplemented by other inert gas (nitrogen) can be recycled to the apparatus 4 and 5, or it can be sent to a combustion section for recovering heat. In order that the invention may be further illustrated in terms of its procedure, reference is invited to the following examples which should not be taken as limitations of the invention. EXAMPLE' 1 An iron-stripped leucite concentrate (theoretical formula K Al Si206) has been treated, with the following composition for the principal and interesting elements: SiO2: 55% - K20: 18% - Al203: 21% - Others: 9% This is a naturally occurring ore. For a ton of leucite, and limtedly to the reactor 1 shown in the accompanying drawing, that is vat-plasma system, the following consumption values for reducing agents, chlorine and electricity have been ascertained: Coke dust: 300kg; Metallurgical coke : 100 kg (size used 20 to 40 mm) Chlorine: 2000 kg - Electric power: 1300 kWh. For each ton (1000kg) of starting product(leucite concentrate) there have been obtained the following outputs: Aluminium chloride: 520 kg - Silicon chloride:1400kg Potassium chloride: 270 kg. The plasma gas had a temperature of 80000C so as to have the reactions taking place at 20000 C. The temperature at the vat top and at the outlet 12 was 15000C. E X A M P L E 2 Residual sludges of the ceramic industry, which had previously been dried, have been treated, which had the following composition with reference to the most interesting elements; Lead :20% - ZirconiumT%-Silicon 30%, the balance being oxygen and several other metals at a very low concentration (less than 0.1). From one ton of dried sludge there have been obtained the following products: Lead chloride: 250 kg - Silicon chloride: 1700 kg - Zirconium chloride: 170 kg. for which the relative consumptions were: Coke dust: 200 kg - Metallurgical coke: 70 kg (size 20 to 40 mm) Chlorine: 1600 kg - Electric power: 1100 kWh. The plasma gas has been fed at 80000C so as to have a processing temperature of 20000 C. The gases at the vat top outlet, 12, had a temperature of 15000C, In both Examples 1 and 2, CO was used as the plasma gas.

Claims: CLAIMS: 1. A process for the producticn of metallic chlorides from metal compounds which contain oxygen, also in the form of complex salts of oxides of various metals, characterized in that said compounds are reacted with clorine or substances which evolve chlorine under the reaction conditions in a reaction zone under reducing conditions, in the interior of a reactor packed with. lumped. solid reducing material at a temperature above 15000C, the as obtained chlorides of the metals being discharged in-the vapour phase through the reactor top and being separated from each other by fractional condensation. 2. Process according to claim 1, characterizedin that the lumped solid reducing material is a carbon-containing material. 3. Process according to claim 2, characterized in that the carbon-containing material is coke. 4. Process according to claim 1, characterized in that the temperature in the reaction zone lies in the range from 18000C to 2500 C. 5. Proceeds according to claim 1, wherein the heat necessary for carrying out the reaction is supplied by a burner. 6. Process according to claim 5, wherein the burner is an arcplasma burner. 7. Process according to claim 1, characterized in that the reducing conditions in the reaction zone are provided by coke. 8. Process according to claim 1, characterized in that the reducing conditions in the reaction zone are provided by a gaseous hydrocarbon. 9. Process according to claim 1, characterized in that the reducing conditions in the reaction zone are provided by a liquid hydrocarbon. 10. Process according to claim 1, characterized in that the reducing conditions in the reaction zone are provided by solid coal. 11. Process according to claim 1, characterized in that the reducing conditions in the reaction zone are provided by CO. 12. Process according to any of the preceding claims, characterized in that the material which provides the reducing conditions is fed into the reaction zone either separately or together with the metal compounds to be chlorinated. 13. Process according to any of the preceding dims, wherein the material which provides the reducing conditions is fed to the reaction zone as a portion of the plasma gas or entirely plasma gas. 14. Process according to claim 1, wherein the metal chlorides are condensed in a labyrinth condenser consisting of refractory-lined chambers having vertically staggered inlets and plates, each plate having a crucible on its bottom and an inlet for a cold gas. 15. Process according to claim 1, wherein the condensation of the chlorides takes place on two or more drums driven to rotation and having water circulating therein under pressure, the condensed chlorides being scraped off from the drum surfaces.

Inventors: D'ALTILIA, GIANLUIGI
Applicants: NUOVA SAMIM S.P.A.
Application year: 1983
Main classification: C22B1
IPC codes: C22B34, C01G1, C22B1, C22B9