Method of processing diamond-containing concentrates and chemically cleaning diamond surface
FIELD: mineral dressing.
SUBSTANCE: method comprises charging, chemically enriching concentrate, cleaning, and discharging desired product. Chemical enrichment is carried out by way of single or multiple processing in acid or in acids and then in alkali or alkali mixture, while heating material to 900-1000°C and holding it at this temperature in inert gas medium at stirring.
EFFECT: enhanced diamond cleaning efficiency.
6 cl, 1 tbl
The invention relates to the beneficiation of minerals and can be used on diamond enterprises.
As the closest analogue may be a method for recovery of diamonds from the diamond raw material for RF application for the invention №94027741 (published 27.06.1996), including loading, chemical enrichment of the concentrate by heating in alkali or their mixtures, cleaning product with water and acid, drying and unloading of the target product.
Known and used in practice ways of acid enrichment diamond concentrates using pure acids (hydrochloric, nitric, hydrofluoric, sulfuric, and others) and/or acid reaction mixtures (Aqua Regia, a mixture of chromic and others) do not provide complete dissolution and destruction of minerals and rocks kimberlite contained in concentrates. This applies above all to the most stable components (garnet, zircon, Distin, kyanite, chromite and other). These minerals are not destroyed and the enriched concentrates using alkaline melts at temperatures up to 500°C. destruction and dissolution is possible when the temperature of the alkaline melt 900°and requires a protective atmosphere to prevent oxidation and loss of mass of diamonds. Based on this known method of chemical enrichment of natural diamond conc the s dimensional grain size less than 0.5 mm at small (a few grams) the weight of the concentrate. However, its application to enrich samples of concentrates more mass (tens, hundreds of grams and the first kilos) and/or increased size (>0.5 mm) is greatly complicated by the formation of muddy sediments, further complicating the dissolution of particles of kimberlite and sustainable minerals due to filling with silt space between mineral grains and thereby obstructing access melt even in case of monolayer arrangement of grain concentrate.
However the bulk of sludge is formed during the destruction of minerals containing iron and calcium, which can be removed by pre-treatment in acids, in which there is a dissolution, but not education silts. The proposed method through the application of the principle of prior acid treatment in combination with the use of the principle of mixing of the concentrate and/or reaction medium (molten alkali), as well as operational and periodic change of the reaction medium allows you to remove from the reaction zone the sludge portion and to create a full and continuous contact of the melt with dissolved mineral grains throughout the volume of the concentrate.
This ultimately allowed to provide the technical result - the high efficiency of the proposed method by increasing the degree of cleaning of diamonds in comparison with the known method is mi.
For the implementation of the technical result in the method of processing diamondiferous ore concentrate, including loading, chemical enrichment concentrate, cleaning and unloading of the target product, it is new that the chemical enrichment concentrate initially lead by single or multiple processing in the acid or acid and then alkali or their mixtures by heating to a temperature of 880÷1000°and holding at this temperature in an inert gas under stirring.
Special cases of the method assume when heating the concentrate in alkali to the extract at a temperature of 450÷550°and in the process of aging at this temperature to perform single or multiple draining molten alkali with the replacement of the melt. In addition, the treatment in the acid or acids may be carried out if the temperature is 50÷150°and as acids to use salt and/or nitrogen, and/or hydrofluoric acid and/or sulfuric acid, or a mixture thereof.
General characteristics of the method includes it in automatic discrete mode with manual loading of concentrate in the cartridge, and the amount of concentrate that is loaded on one full cycle of chemical enrichment and clean the surface of the diamonds is 5±0,01 kg Method preduster the characteristic use of concentrates with different content of diamonds (diamond content of 50% and above). The final product is a graded diamond crystals with a size of more than +0.2 mm, the surface of which is cleaned from chemical compounds and preserves the integrity of the form of crystals. Technologically members of the proposed method processes the chemical enrichment of diamondiferous ore concentrate and purification of the target product (i.e., the surface of the diamond) consist of the following stages (phases):
- preparation of reagents;
- preparatory operations;
chemical decomposition of the mineral part of the diamondiferous concentrate;
- washing, drying, cooling, and packaging of the final product;
- neutralization of waste chemicals.
Characteristics of the raw materials, reagents and materials presented in the table. Below is an embodiment of the inventive method step by step description of the stages of enrichment and cleanup.
operation 1. Preparation of alkaline mixture. Prepare two portions 5±0.01 kg equimolar mixture of sodium hydroxide and potassium hydroxide (41,7% NaOH and 58.3% STAKE);
- step 2. Preparation of a solution of 15%hydrochloric acid. A solution of 15%hydrochloric acid is prepared by diluting concentrated 36%hydrochloric acid distilled water. The weight ratio of hydrochloric acid to water is 1:1,4;
- step 3. Prigot the effect of a 5%solution of sodium hydroxide. Dissolving 1 weight part of sodium hydroxide in 19 weight parts of water.
operation 1. Start installation of gaseous nitrogen. Nitrogen is obtained by the industrial installation. The oxygen content in the nitrogen control by using a detector;
- step 2. Installing the print cartridge with concentrate in the reactor. Sealed cartridge containing 5±0.01 kg of concentrate, is installed in the reactor and tightly close the lid of the reactor;
- step 3. Download the alkali in the melting apparatus. In each of the two melting apparatus loaded on a 5±0.01 kg alkaline mixture, and a hermetically sealed cover apparatus melting;
- step 4. The evaporation of water from the alkaline mixture. Evaporation of water is performed by heating the alkaline mixture in the melting apparatus at a temperature of 500±50°C for 2 hours with blowing nitrogen over the surface of the molten alkaline mixture at a rate of 10±0.1 l/h;
operation 5. Download liquid melts. In tanks for storage of liquid reagents upload a 15%hydrochloric acid, 36%hydrochloric acid, 56%nitric acid, distilled water, 5%solution of sodium hydroxide, ethyl alcohol. In the absorber exhaust the reaction gas load 5%solution of sodium hydroxide.
Chemical decomposition of mineral hour and diamondiferous concentrate:
operation 1. Chemical decomposition of the initial concentrate hydrochloric acid. The chemical decomposition of the carbonates with the removal of the hydrochloric acid solution of carbon dioxide, as well as translation in the solution of the oxides and hydroxides of the metals with the formation of their chlorides carried out by heating the source of concentrate in 5 l of 36%hydrochloric acid at temperatures of 20-80°C for 1.0 hour. The weight ratio of hydrochloric acid to the weight of the original concentrate 1:1 (weight ratio of hydrochloric acid to the weight of the mineral concentrate 2:1). At the end of the process hydrochloric acid solution is poured into the Converter. The waste (carbon dioxide) gas is neutralized in the absorber 5%solution of sodium hydroxide;
- step 2. Leaching the concentrate with distilled water. Removal from the reactor hydrochloric acid and insoluble impurities (with a particle size less than 0.2 mm) concentrate is washed three times with distilled water. Volume one portion of distilled water equal to 5±0,1 HP At the end of the wash portion of the wash water is drained into the catalytic Converter;
- step 3. Oxidative decomposition of concentrate nitric acid. Oxidative decomposition of sulphides of iron, manganese and zinc and translate them into a solution performed by heating the remaining concentrate 2.5 l 56%nitric acid at temperatures of 20-80°C for 1.0 hour. After the process is and the nitric acid solution is poured into the Converter. Exhaust oxides of nitrogen is neutralized in the absorber 5%solution of sodium hydroxide;
- step 4. Leaching the concentrate with distilled water. Removal from the reactor of the nitric acid and insoluble impurities (with a particle size less than 0.2 mm) concentrate is washed three times with distilled water. Volume one portion of distilled water equal to 5±0,01 L. At the end of the wash portion of the wash water is drained into the catalytic Converter;
operation 5. Alkaline concentrate smelting, past the acid treatment. Alkaline decomposition of the acid-insoluble silicates and difficultly soluble in acid sulfate barium remaining in the concentrate is carried out by heating it in 5±0.01 kg alkaline mixture at a temperature of 500±50°C for 1.0 hour. At the end of the process the alkaline mixture is poured into the Converter at a temperature of Plava 500±50°C;
operation 6. Final alkaline concentrate smelting. Alkaline decomposition of silicates (mainly garnet), does not decompose in alkaline medium at a temperature of 500±50°To conduct heat to 8.5±1.0 kg alkaline mixture at a temperature of 890±10°C for 1.0 hour in a stream of nitrogen and the excess pressure 0,02-0,03 MPa. At the end of the process the temperature of the melt is reduced to 500±50°With and merge into the catalytic Converter.
Washing, drying, cooling and upakovochnogo product:
operation 1. Rinsing with distilled water grained part of the final product. Leaching granular part of the final product from alkali and silts carried out once after cooling it to 50±10°With 5 liters of distilled water. At the end of the process wash water to drain into the neutralizer;
- step 2. Washing the surface of the granular crystals part of the final product hydrochloric acid. To clean the surface of the granular crystals part of the final product from the residual alkali and their oxides are heated in 5 l of 15%hydrochloric acid at temperatures of 20-80°C for 15 minutes. At the end of the process exhaust hydrochloric acid solution is poured into the Converter;
- step 3. Rinsing with distilled water grained part of the final product. Leaching granular part of the final product from the hydrochloric acid is carried out with distilled water portions 5 l until the pH of wash water 7±1.
- step 4. Washing the granular part of the final product with ethyl alcohol. Wash 5 litres of ethanol granular part of the final product from the remnants of water is performed once for 5 minutes. After washing the ethyl alcohol is discharged into the collection for recycling and regeneration in accordance with the established procedures;
operation 5. Drying of the final product. The final drying is the product is carried out at temperatures of 120-150° With a stream of nitrogen for 0.5 hours. After drying, the final product is cooled and remove the cartridge from the reactor for subsequent processes in the overall production chain.
Neutralization of exhaust agents:
operation 1. Neutralization of waste chemicals. Neutralization operating reagents spend 36%hydrochloric acid neutralizer while cooling and stirring neutralizing solution to the value of its pH 7±1.
- step 2. Filtering the neutralized solution. The neutralized solution is filtered, the liquid fraction is drained into the sewer, and solid phase stockpiling.
The implementation of the method in an industrial environment has confirmed its high efficiency in beneficiation of diamond-containing concentrates.
|№ p/p||Name of raw materials, reagents and materials||GOST, TU, rules or methods for preparation of the reagent or material||Indicators necessary for validation||Regulated indicators with tolerance|
|1.||The diamondiferous concentrate||The diamond content, %||99,99; 70 and 50|
|2.||Nitrogen gas||GOST 9293-74 high purity grade 1||The oxygen content, %, max||0,02|
|3.||Hydrochloric acid||GOST 3118-77 (1 MEAs) brand X4||Density, g/cm3not less than||1,18|
|4.||Nitric acid||THE 2612-046-0576-1643-95 grade analytical grade||Density, g/cm3not less than||1,35|
|5.||Sodium hydroxide||GOST 4328-77 grade analytical grade||The content of NaOH - 417±0,1%|
|Content CON - 58,3±0,1%|
|6.||Potassium hydroxide||GOST 24363-80 grade analytical grade|
|7.||Distilled water||GOST 6709-72||The electrical conductivity, s/Cm, no more than||1×10-4|
|8.||Ethyl alcohol||GOST 17299-78 technical grade||The quality of the alcohol test certificate on ethanol||-|
|9.||Water water||GOST 2874-82||Hardness total, mg-EQ/l, no more than||7,0|
|/td>||The content of iron ions, mg/l, max||0,3|
1. The method of processing diamondiferous ore concentrate, including loading, chemical enrichment of the concentrate by heating in alkali or their mixtures, cleaning product with water and acid, drying and unloading of the target product, wherein the enriched concentrate before heating in alkali or their mixtures perform single or multiple processing concentrate in acid or acids, and heating in alkali or their mixtures lead to a temperature 880-1000°aged at this temperature in an inert gas under stirring.
2. The method according to claim 1, characterized in that upon heating the concentrate in alkali conduct additional exposure at a temperature of 450-550°C.
3. The method according to claim 2, characterized in that the additional exposure perform single or multiple draining molten alkali with the replacement of the melt.
4. The method according to any one of claims 1 to 3, characterized in that the treatment in the acid or acids is carried out at a temperature of 50-150°C.
5. The method according to any one of claims 1 to 3, characterized in that the acid used salt and/or nitrogen, and/or hydrofluoric acid and/or sulfuric acid, or a mixture thereof.
6. The method according to claim 4, characterized in that the acid used to Solano and/or nitrogen, and/or hydrofluoric acid and/or sulfuric acid, or a mixture thereof.
FIELD: methods of determination of content of palladium and platinum in ores containing considerable amount of iron, copper, zinc and other metals.
SUBSTANCE: proposed method includes decomposition of ore by hydrofluoric and nitric acids followed by further decomposition by aqua regia, boiling-off to moist salts, dissolving of them in hydrochloric acid and extraction. Determination of content of palladium is carried out in organic phase thus obtained and that of platinum is carried out in hydrochloric acid phase. Extractants used for such determination are s-alkylisothiouronium halides and alcohols of C5-C8 fractions, as well as kerosene, benzene, toluene and xylols used as diluents. Used as s-alkylisothiouronium halides are chlorides, bromides and iodides from C7 to C14 and their fractions.
EFFECT: extended range of reagents and inert diluents.
2 cl, 2 ex
FIELD: non-ferrous metallurgy, processing of manganese-containing materials, namely hydraulic metallurgical processing of mixed manganese-containing materials or similar manganese ores for obtaining manganese concentrate possibly used in metallurgical, electrical engineering, chemical industry branches.
SUBSTANCE: method comprises steps of converting manganese and related impurities to solution by two-stage treatment of initial manganese containing material with mineral acid. At first stage hydrochloric or sulfuric acid is used for treatment. At second stage hydrochloric acid is used for treating insoluble residue at relation of acid concentration for first stage to its concentration for second stage 1 : (1.0 - 6.6) and simultaneously providing absorption of separated chlorine by alkali solution. After second treatment stage pH of pulp is reduced till 3.5 - 4.5 due to adding carbonate manganese ore. Manganese salt solution is separated from deposit of impurities by filtering. Manganese concentrate is extracted out of filtrate by mixing solution of its salt with solution after chlorine absorption for setting pH 9.5 - 10.5. Value pH is corrected, if necessary by means of milk of lime or sodium hydroxide solution containing excess of sodium chloride. Then concentrate is filtered, washed and dried. Produced manganese concentrate contains at least 60 % of manganese and phosphorus no more than 0.08%. Extraction degree of manganese to concentrate is no less than 92.8%. Invention provides possibility of producing for one technological cycle manganese concentrate including at least 60 % of manganese and no more than 3% of impurities from manganese-containing materials containing manganese less than 30 % and phosphorus 0.1 - 1.0.
EFFECT: enhanced efficiency of method.
4 cl, 2 tbl, 5 ex
FIELD: noble metal metallurgy, namely processes for producing refined silver.
SUBSTANCE: method comprises steps of dissolving metallic silver in nitric-acid electrolyte at presence of hydrogen peroxide; separating non-soluble remainder; extracting silver out of electrolyte; returning electrolyte for dissolving metallic silver. Metallic silver is dissolved at its flow rate 1.9 -2.0 kg per kg of nitric acid contained in electrolyte. Powdered silver produced from silver chloride by hydro-chemical reduction is used as metallic silver. Silver is extracted out of electrolyte at content of nitric acid in electrolyte in range 30 - 50 g/dm3 and at temperature of electrolyte no more than 35°C.
EFFECT: simplified technological system for producing refined silver.
2 tbl, 15 ex
FIELD: methods of treatment of circulating products containing palladium in form of metallic, oxide and metal-oxide forms.
SUBSTANCE: proposed method is used for production of stable isotopes in treatment of entrapping chambers of magnetic separators; metallurgy; processing ores and concentrates containing oxidized and native palladium and utilization of palladium-containing catalysts, as well as in analytical and preparative chemistry. Leaching is performed by solutions of nitric acid in presence of ammonium nitrate and weakly-basic anionite of epoxy-polyamine, type AH-31 at concentration of nitric acid in leaching solution from 120 to 190 g/l and ammonium nitrate from 160 to 240 g/l followed by separation of resin from pulp, washing of anionite with water from mother liquor and desorption of palladium from anionite. Proposed method increases degree of leaching palladium from sludge during one stage; method ensures obtaining pure solutions of palladium during its desorption from anionite reducing number of operations in treating the solutions for obtaining palladium or its compounds reducing the time required for conversion of palladium.
EFFECT: enhanced efficiency.
4 cl, 4 tbl, 4 ex
FIELD: hydrometallurgy; ore concentrates processing.
SUBSTANCE: the invention is pertaining to the field of hydrometallurgy, in particular, to processing of the loparite concentrate. The method includes a decomposing of the loparite concentrate at the temperatures of 103-105°C and the concentration of hydrofluoric acid of 38-42 mass % with production of the pulp containing fluorides of titanium, rare earth elements (REE), niobium, tantalum and sodium. The pulp is filtered at the temperature of 90-95°C with extraction into the fluorotitanium solution of fluorides of niobium and tantalum and no less than 58 % of sodium in terms ofNa2O and separation of the sediment containing fluorides of rare earth elements (REE) and a residual sodium. The produced solution is cooled down to 18-24°C with separation of the second sediment of sodium fluorotitanate. After that they extract niobium and a tantalum from the solution by octanol-1 extraction at a ratio of the organic and water phases as 1.1 : 1. The sediment of REE fluorides is washed from fluorotitanate by sodium water in a single phase at the temperature of 90-95°C and at the solid :liquid ratio = 1:2-2.5. The cleansing solution is separated and evaporated with extraction of the additional sediment of sodium fluorotitanate. After extraction of niobium and tantalum the fluorotitanium solution is evaporated and filtered with separation of the first sediment of sodium fluorotitanate from the concentrated solution of fluorotitanium acid, which is directed to extraction of titanium. The gained first, second and additional sediments of sodium fluorotitanate are combined and subjected to conversion with production of sodium fluorosilicate and the conversional fluorotitanium acid added to fluorotitanium solution before its evaporation. The technical result of the invention is a decrease in 2.0-2.5 times of the volume of the cleansing solutions at provision of a high degree of extraction of compounds of titanium and other target products. The produced sodium fluorotitanate contains the decreased amount of the impurity ingredients of calcium and strontium.
EFFECT: the invention ensures a decrease in two-two and a half times of the volume of the used cleansing solutions at provision of a high degree of extraction of compounds of titanium and other target products and a decreased amount of impurities of calcium and strontium in the sodium fluorotitanate.
7 cl, 1 dwg, 1 tbl, 3 ex
SUBSTANCE: method comprises leaching mineral raw in the water solution of acid with concentration from 1.8 g/l to 50 g/l by active oxygen in the presence of ions of trivalent ferrous and extracting metals from the leached products.
EFFECT: enhanced efficiency and reduced cost of treating.
13 cl, 3 ex
FIELD: inorganic compounds technologies.
SUBSTANCE: invention relates to technology of titanium-calcium mineral raw material, in particular to acid decomposition of sphene concentrate, and can be used to produce titanium dioxide and products based thereof. Prior to be treated with acid, concentrate is subjected to mechanical activation with energy supply intensity 10 kJ/s per 1 kg concentrate within 5 to 30 min. Mechanical activation in carbon dioxide medium is also possible at CO2 consumption 0.2-0,8 mole/mole CaO. For acid treatment of concentrate, 15-20% nitric acid is used at ambient temperature and atmospheric pressure, wherein additional titanium is transferred into solution. Resulting reaction mass is filtered to separate silica residue.
EFFECT: increased feasibility of process due to reduced acid treatment temperature and allowed atmospheric pressure.
2 cl, 5 ex
FIELD: metallurgy of non-ferrous and noble metals.
SUBSTANCE: proposed method includes leaching-out metals from oxidized ores or technogenious wastes and extraction of metals from solutions followed by additional strengthening of depleted solutions with the aid of leaching-out agent. Leaching-out of copper is performed at several stages with the aid of solutions at increasing oxidizing/reducing potential; leaching-out of gold is combined with last stage of extraction of copper. The high efficiency of leaching-out of copper at initial stages is reached in presence of ferric iron; leaching-out of gold and last stage of extraction of copper are performed in presence of active chlorine or oxichlorides; copper and gold are extracted from solution by carburizing and gold is extracted by sorption. Depleted solution is brought to pH=4-5 before additional strengthening with leaching-out agent and is treated with oxygen-containing gas, air for example.
EFFECT: enhanced efficiency.
6 cl, 1 ex
FIELD: chemical industry; production of strontium carbonate.
SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to production of strontium carbonate. The method provides for extraction and purification of strontium carbonate including isotope-enriched strontium carbonate produced by the electromagnetic separation method. The strontium concentrate is treated with an acid producing strontium-carrying sediment, transfer strontium into a solution with a separation and washing-down of the insoluble residue, produce crystals of strontium nitrate, purify the crystals from impurities by their washing-down with nitric acid. Then the crystals are dehydrated, dissolved and separated form impurities with the subsequent production of strontium carbonate. At that a solution produced after treatment of the strontium carbonate should be previously purified by settling and separation of the iron group impurities present in the form of hydroxides, and barium and lead - in the form of sulfates. The strontium-carrying sediment is settled in the form of the strontium carbonate due to addition in the solution of ammonium carbonate and ammonia with subsequent calcinations of the sediment at the temperature of 600-700°C. Strontium transfer in the solution by treatment of the calcined sediment of strontium carbonate with nitric acid at the ratio of (1:2) - (1:3). The dehydrated crystals of strontium nitrate are dissolved in water at the mass ratio of water to strontium nitrate equal to (1-2) :1 and the strontium carbonate is subjected to settling with the help of ammonium carbonate at pH equal to 9-10. The procedure of the preliminary separation of impurities in the form of hydroxides, sulfates and ammoniac complexes, calcinations of strontium-carrying with its subsequent dissolution and separation of impurities and a sedimentation of strontium with the help of ammonium carbonate at рН equal to 9-10 allows to extract 99.2 % of strontium-88 carbonate with a purification efficiency of 99.999 %. The technical result is production of pure strontium carbonate at minimum losses at phases of processing.
EFFECT: the invention ensures production of pure strontium carbonate at minimum losses at phases of processing.
3 cl, 5 ex
FIELD: precious metals technology.
SUBSTANCE: method comprises treatment of initial material with reagent solution under microwave irradiation to transfer precious metals into solution. Initial material is preliminarily subjected to mechanical activation during 5 to 120 min while maintaining ratio of mechanical power supplied to specific surface area of activated material within a range of 0.0133 to 25 W-kg·m2. Microwave treatment starts directly after mechanical activation using acid and/or oxidant to form slurry from activated material and reagent solution. Irradiation is carried out to boiling temperature. Acid and/or oxidant is selected from HCl and/or Cl2, HCl and/or H2O, HCl and/or Br2, HCl and/or NaClO3, HCl and/or HNO3, HF and HCl and/or NaClO3, mixtures of H2SO4 and HCl and/or H2O2, mixtures of HCl and HBr and/or H2O2, mixtures of HCl and HI and/or NaClO3 and J2, HCl and/or Cl2 and Br2.
EFFECT: increased degree of precious metal recovery.
3 cl, 13 ex
FIELD: non-ferrous metallurgy; elimination of waste in the course of processing tungsten-tin concentrates, production of calcium tungstate and tin compounds.
SUBSTANCE: proposed method includes reducing roasting of initial concentrate and hydrochloric acid leaching of cinder thus obtained. After hydrochloric leaching, tin hydroxide is settled from solution for obtaining tin dioxide. After acid leaching, solid residue is sintered with soda, sinter thus obtained is subjected to aqueous leaching and calcium tungstate is settled from solution. Solution obtained after settling of tin hydroxide is neutralized by lime milk driving off ammonia which is directed for settling of tin hydroxide; calcium chloride solution thus obtained is directed for settling of calcium tungstate from sodium tungstate solution. Proposed method makes it possible to close technological cycle of processing of blended tungsten-tin concentrates by water, ammonia and calcium chloride, thus reducing formation of wastes in production of tin and tungsten compounds.
EFFECT: reduced formation of wastes due to closed technological cycle.
1 dwg, 1 tbl, 1 ex
FIELD: chemical concentration of manganese ores; reduction of iron-manganese concretions.
SUBSTANCE: proposed method includes heating of ores together with reductant for reducing manganese dioxide (MnO2) to bivalent state (MnO). Subjected to reducing roasting are iron-manganese concretions of Baltic Sea containing no more than 26% of MnO2 with the use of organic agents as reductants contained in the amount of 14% at heating to temperature of 400°C and limited admission of air to roasting zone.
EFFECT: simplified procedure of reducing roasting.
1 dwg, 1 ex
FIELD: metallurgy of rare metals; methods of processing of titanium-silicon containing concentrates.
SUBSTANCE: the invention is pertaining to the field of metallurgy of rare metals, in particular, to the methods of processing of quartz- leucoxene concentrates of Yaregsky deposit containing high concentrations of the secondary rutile-quartz aggregate and may be used for production of artificial rutile - the raw for production of titanium by a chloric method and pigmental titanium dioxide. The method of the processing provides that the initial flotation quartz- leucoxene concentrate of 0.1 mm coarseness is treated with ammonium fluoride at its injection in a mass ratio to the concentrate of(0.6-1.25 : 1), and at the temperature of 195-205°C. Titanium and silicon compounds separation at the thermal treatment of the produced product is conducted at the temperature of 295-305°C with sublimation of ammonium silicofluoride and production in the bottom of the artificial rutile containing 90-95 % of titanium dioxide. Sublimates of ammonium silicofluoride are treated with handle an ammonia water gained at fluorination of the source concentrate with production of sediment of a silicon dioxide and the solution of ammonium fluoride after separation of silicon dioxide sediment is evaporated with production of ammonium fluoride, which is fed back for fluorination of a new batch of the initial concentrate. The technical result of the method is simplification of the process, reduction of power inputs and reduction of consumption of fluorine-containing reactant.
EFFECT: the invention ensures simplification of the process, reduction of power inputs and reduction of consumption of fluorine-containing reactant.
FIELD: metal recovery, in particular noble metals from technologically proof raw materials.
SUBSTANCE: method includes raw grinding to 0.2 mm; blending with batch containing halogen salts and/or oxygen-containing salts, and mixture opening: cake cooling, leaching with simultaneous reaction pulp agitation with hot water, and metal recovery from solution and insoluble residue. Opening is carried out in electrical furnace at 100-120oC preferably at redox potential of 1.8-2.6 V, by elevating of temperature up to 450-560oC at rate of 8-10oC/min and holding for 1-7 h at highest mixture redox potential. Opened and cooled cake is grinded and leached in opened agitator.
EFFECT: environmentally friendly method with increased yield; utilization of unconventional noble and non-iron metal sources.
1 cl, 2 tbl
FIELD: production of diamonds of jewelry property; high-quality cleaning of diamonds.
SUBSTANCE: proposed method includes stage-by-stage treatment of diamond by mixture of acids under action of microwave radiation; at first stage, use is made of nitric acid and hydrogen peroxide at volume ratio of components of 10:1, respectively; at second stage, volume ratio of mixture of concentrated nitric acid, hydrochloric acid and hydrofluoric acid is 6:2:1, respectively; diamond is treated at temperature not higher than 210°C, pressure of 35 atm as set by loading ratio of autoclave equal to 1:10 at power of oven of microwave radiation of 1200 W; duration of each phase does not exceed 40 min. Proposed method ensures perfect cleaning of diamonds from contamination of mineral and organic nature including bitumen compounds on surface and in cracks of diamond.
EFFECT: enhanced efficiency; reduction of time required for process.