Method of processing manganese ore

FIELD: chemistry.

SUBSTANCE: method involves grinding ore, mixing the ground ore with sodium bisulphate taken in stoichiometric amount required for binding manganese and impurities into sulphates. The mixture is calcined in three steps to obtain coal tar: at the first step at temperature 200-300°C for 1-2 hours, at the second step at temperature 400-500°C for 0.5-1.5 hours, at the third step at temperature 600-700°C for 2-4 hours. The coal tar is leached with water at temperature 40-80°C for 0.5-1 hour and weight ratio coal tar: water equal to 1:(3-4). After filtering the obtained pulp, sludge is separated and the filtrate is treated with sodium carbonate solution taken in stoichiometric amount required for binding and depositing manganese (II) and iron (II) compounds. After filtering the obtained suspension, the precipitate of manganese (II) and iron (II) carbonates is dried and washed to obtain a manganese concentrate. Calcination exhaust gases are absorbed with the filtrate from the manganese carbonate extraction step to obtain sodium bisulphate solution. Through evaporation of the obtained solution, crystallisation and drying, sodium bisulphate is obtained, which is taken for mixing with the ground ore to obtain the mixture.

EFFECT: simple process and zero-discharge scheme of the process of processing manganese ore.

2 cl, 1 dwg, 2 ex

 

The invention relates to chemical technology of manganese and can be used in beneficiation of manganese ores, in particular in the processing of oxide manganese ores.

A method of refining manganese raw materials, including leaching of raw materials working solution of sulfuric acid and ammonium sulfate with an estimated value of pH. In the resulting suspension is injected manganese iron as a reducing agent to achieve a pH of 1.8-2.0. The suspension is filtered with the release of insoluble precipitate and obtain a solution of divalent manganese; subsequent cleaning solution of manganese is carried out by deposition of iron and phosphorus ammonia at pH of the liquid phase of 4.5-5.0. The resulting suspension is filtered with the Department zelenotsvetnaja sludge. From purified ammonium sulfate solution get electrolytic manganese and circulating sulfuric acid containing ammonium sulfate [A.S. SU # 1518400, CL SW 47/0, publ. 30.10.1989, bull. No. 40].

The disadvantage of this method of processing manganese raw materials is the use of ferromanganese as a reductant and a significant amount of wastewater.

A method of refining the mn containing raw materials, providing its leaching with sulfuric acid in a concentration of 70-98% in the number of 77-95% of the stoichiometrically required for the binding of manganese sulfate in the presence of 20-40%of the CSOs solution of potassium bisulfite, used as a restorative solution. The resulting slurry is directed to the separation of phases. From the filtrate, containing manganese sulfate MnSO4, precipitated manganese carbonate by reacting with a solution of potassium carbonate. The suspension is filtered, the precipitate is washed, dried and calcined at a temperature of 650°C To produce manganese concentrate. The use of a solution of potassium bisulfite allows to reduce the consumption of sulphuric acid and to improve the quality of the finished product [Patent RU No. 2223340, CL SW 47/00, SW 3/08, publ. 10.02.2004].

The disadvantage of this method is the high corrosiveness of the reaction medium through the use of concentrated sulfuric acid, the use of expensive potassium bisulfite as a reductant, a significant quantity of liquid effluent directed to recycling.

The closest to the achieved result is a method for processing manganese ore, including the crushing ore, the receipt of the charge, the firing of the charge, the translation into a solution of manganese and related impurities, separating the sludge from the solution, precipitation of compounds of manganese, the allocation of manganese concentrate filtration and drying the precipitate, while the crushed ore is mixed carbonaceous material getting charges and are fired at 600-900°C and the ratio vosstanovit is: ore=1:(1-6). The obtained sintered process abgaznaya hydrochloric acid at 70-95°C, the ratio of T:W=1:(1,5-8,0) and at pH less than 1. Next, separate the sludge. Cleaning solution (filtrate) from the impurities is carried out by bringing the pH to 4.0 to 6.0 and the precipitate hydroxides. In the purified solution is injected oxidant (from the group of sodium hypochlorite, hydrogen peroxide, air, or a mixture thereof) at a ratio of oxidant: ore=1:(2,0-5,0). Allocation concentrate manganese is carried out at a temperature of 40-90°C and a pH of 7.6-14,0. The precipitate manganese concentrate consisting of manganese dioxide MnO2is separated from the mother liquor by filtration, the precipitate is washed with hot water and dried to obtain the target product [Patent RU No. 2175991, CL SW 47/00. C01G 45/02, publ. 20.11.2001].

The disadvantages of this method are the multistage process associated with holding, as recovery and oxidation of compounds of manganese, high corrosiveness of the reaction medium due to the use of hydrochloric acid, a significant amount of wastewater.

The objective of the invention is to simplify the process and development of a closed-circuit processing of manganese ores.

This goal is achieved in the proposed method of processing an oxide of manganese ore, including the crushing ore, the receipt of the charge, the firing of the charge, the translation into a solution of manganese and from the accompanying impurities, the separation of the sludge from the solution, precipitation of compounds of manganese, the allocation of manganese concentrate filtration and drying the precipitate, and the crushed ore is mixed with obtaining a mixture with sodium hydrosulphate, taken in an amount required for stoichiometric binding of manganese and impurities in sulfates. Then hold the firing of the charge in three stages with obtaining pitch: in the first stage, the mixture is subjected to heat treatment at a temperature of 200-300°C for 1-2 h, the second at a temperature of 400-500°C for 0.5-1.5 h, the third at a temperature of 600-700°C for 2-4 hours. Transfer into a solution of manganese and related impurities is carried out by leaching peck water at a temperature of 40-80°C for 0.5-1 h and the mass ratio peck: water=1:(3-4). The resulting slurry is filtered, separating the sludge from the leaching step. The filtrate is treated with sodium carbonate solution, taken in the quantity stoichiometrically required for the deposition of compounds of manganese (II) and iron (II). The resulting suspension is filtered, the precipitate of carbonate of manganese and iron washed with water and dried to obtain manganese concentrate. The filtrate, representing a solution of Na2SO4directed to the stage of absorption of the off-gases of the kiln charge. Upon absorption of flue gases containing sulfur dioxide, an aqueous solution of sulfate n the sodium form a solution of sodium hydrosulphate. The solution hydrosulfate evaporated, isolated crystals and after drying of the crystals obtained dry product is directed to mix with the crushed ore with getting charges. Sludge stage leaching consisting of aluminum hydroxide and silicon dioxide, is directed to the production of construction material.

The invention consists in the following: when firing the oxide of manganese ore in the presence of sodium hydrosulphate flow redox processes, including recovery of the oxidized forms of the compounds of manganese and trivalent iron in equations:

When firing the aluminum hydroxide turns into aluminum sulfate at the expense of course of the exchange reaction:

The exhaust gases of the firing process contain sulfur dioxide (SO3oxygen and water vapor. Thus, when roasting ore compounds of manganese and of iron, aluminum turn into water-soluble forms. When leaching received peck water sulfates of manganese (II) MnSO4and iron (II) FeSO4into solution. Aluminum sulfate Al2(SO4)3when leaching is subjected to hydrolysis with the formation of the precipitate of aluminum hydroxide and sodium hydrosulphate.

The reaction mass after leaching peck is a slurry, where the aluminum hydroxide and silicon dioxide precipitate. The slurry is filtered sludge Al(OH)3and SiO2separated and after washing is directed to the production of construction material. The filtrate containing the sulfates of manganese, iron (II), sodium, sodium hydrosulphate, shall be used for interaction with the sodium carbonate. When this water-soluble sulfates of manganese (II) and iron (II) are transformed into insoluble MnCO3and FeCOCwhich precipitates.

The precipitate of carbonate of manganese (II) and iron (II) is separated by filtration, washed, dried, obtaining the target product containing not less than 70% MPMs3. The filtrate, representing sulfate solution and sodium hydrosulphate, direct to the stage of absorption of the flue gas to absorb the sulfur dioxide and water vapor. When the absorption of sulfur dioxide forms sulfuric acid, which interacts with sodium sulfate to form sodium hydrosulphate:

The obtained absorption liquid, representing the solution of sodium hydrosulphate, evaporated, dried, and return to the step of mixing the crushed ore for batch preparation.

The process of firing W is hte ore and sodium hydrosulphate in three stages, namely, in the first stage at a temperature of 200-300°C for 1-2 h, the second at a temperature of 400-500°C for 0.5-1.5 h, the third at a temperature of 600-700°C for 2-4 hours, to ensure complete recovery of the oxidized forms of manganese with obtaining compounds of manganese (II) and iron (II), the high output of manganese ore. The temperature decrease, the decrease in the duration of stages of the firing process lead to lower output of manganese ore. Rising temperatures, increased duration of the stages of the firing process results in excessive energy and education class. The amount of sodium hydrosulphate, taken in an amount required for stoichiometric binding of manganese and iron impurities, aluminum sulfate, provides full transition of these components in water-soluble form and the effective and efficient use of the reagent. Consumption of hydrosulfate below stoichiometric norm leads to a decrease of the yield of the target product. Consumption of hydrosulfate above stoichiometric norm leads to excess reagent. The process of leaching when the mass ratio peck: water=1:(3-4)at a temperature of 40-80°C for 0.5-1 h to ensure complete transition in a solution of sulphate of manganese (II) and iron (II) and aluminium and high yield of the target product. Reducing water consumption is lower with the relationship 1:3 results in lower yield of the desired product due to the loss of manganese precipitate stage leaching from incomplete transition in solution MnSO 4. The increase of water flow leaching above the ratio of 1:4 results in dilute solutions and to increase in the future energy consumption for evaporation of a solution of sodium hydrosulphate. Lowering the temperature of the leaching below 40°C and the duration of the process is less than 0.5 h leads to loss of manganese and reduced yield of the target product. Lowering the temperature below 40°C also requires forced cooling of the reaction mass, as by leaching leads to heating of the reaction mass. Raising the temperature above 80°C is impractical because it does not increase product yield when the over-expenditure of energy for heating the reaction mass. The increase in the duration of the leaching process more than 1 h leads to performance degradation of the installation. Treatment of the filtrate with sodium carbonate solution, taken in the quantity stoichiometrically required for the deposition of compounds of manganese (II) and iron (II), to ensure complete precipitation of manganese and rational use of the reagent. Reducing consumption of sodium carbonate below the norm leads to loss of manganese, and rising consumption - waste of reagent.

Carrying out processing of manganese ores on the proposed method provides a simple process due to compatible with the assumptions of the burning process and the recovery of compounds of manganese, the lack of phase oxidation of compounds of manganese, closed circuit recycling through the process when you return and recycling of sodium hydrosulphate in the technological cycle. When using the invention can be obtained by technical result, which is expressed in the possibility of obtaining high-quality target product - carbonate of manganese and related products - aluminum hydroxide and silicon dioxide, sodium hydrosulphate. Manganese carbonate has a multifaceted application: used in metallurgy for the production of metallic manganese and ferro-manganese, dioxide and oxide of manganese.

Schematic diagram of processing of manganese ore shown in the drawing.

The implementation of the invention is illustrated by the following examples.

Example 1. 1000 g of crushed ore manganese oxide ore, containing in wt.%: 9,72 MP2About3, 27,53 Mno2, 10,46 Fe2O3, 7,33 Al2About3, 44,46 SiO2and 0.5 moisture, mixed with 2954 g of sodium hydrosulphate with getting 3954 g of the charge. The number of hydrosulfate taken in the stoichiometric ratio for binding of the compounds of manganese, iron, aluminium. The mixture is subjected to firing in three stages with obtaining pitch: in the first stage, the mixture is subjected to heat treatment at 250°C for 1.5 h, the second at the same time is the temperature value 450°C for 1 h, the third is at a temperature of 650°C for 3 hours. When roasting flow redox processes with the formation of sulfate manganese (II)sulfate iron (II)sulfate of aluminum and the release of sulfur dioxide (SO3oxygen and water vapor in the exhaust gases. As a result of firing the obtained 3301,1 g peck composition, wt.%: 20,1 MnSO4, 6,0 FeSO4, 7,45 Al2(SO4)3, 13,45 SiO2, 53,0 Na2SO4and isolated in the gas phase 355,3 g sulfur dioxide (SO3, 226,6 g of water, 71,0 g of oxygen. Next pitch is cooled and subjected to leaching for 1 h with water, taken in an amount 11884,0, the Mass ratio peck: water is 1:3,6. When leaching occurs heating of the reaction mass, the temperature rises to 60°C. the pH of the reaction mass 6.5, non-corrosive environment. Leachate get 15185,1 g of slurry containing 112,15 g of aluminum hydroxide and 446,6 g of silicon dioxide in the form of sediment. The slurry is filtered, separated 556,75 g of the washed sludge stage leaching, which after drying is directed to the production of construction material. 14628,35 g of the filtrate, containing in %: 4,54 MnSO4, 1,36 FeSO4, 3,54 NaHSO4, 9,85 Na2SO4handle with 3025,0 g of 20%sodium carbonate solution. When interacting with sodium carbonate, sulphate of manganese (II) and iron (II) form corresponding to rbonate and precipitate. Sodium carbonate (605,0 g) is taken in the quantity stoichiometrically required for the formation and deposition of carbonates of manganese and iron. The resulting suspension (17653,35 g) carbonates of manganese and iron are sent to the filtering. The precipitate is washed with water and dried, the result is 668,2 g of manganese concentrate, containing in wt.%: 75,65 MPMs3, 22,71 F3, 0,67 Na2SO4, 0,16 NaHSO4and 0.8 moisture. The filtrate number 16962,2 g containing 13,25% Na2SO4and 3.05% NaHSO4directed to the stage absorption stage exhaust gases of firing. When absorption is absorbed 355,3 g of sulfuric anhydride and 226,6 g of water and get 17544,1 g absorption solution containing 2954 g of sodium hydrosulphate. If necessary, the composition of the solution is adjusted by adding technical sulfuric acid. The solution hydrosulfate evaporated, isolated crystals are dried to obtain dry sodium hydrosulphate, which return a mixture of crushed ore with getting charges.

Example 2. 1000 g of crushed ore manganese oxide ore, containing in wt.%: 1,84 MP2About3, 28,03 MnO2, 9,52 Fe2O3, 11,92 Al2About3, 48,59 SiO2and 0.1 moisture, mixed with 2904 g of sodium hydrosulphate with getting 3904 g of the charge. The number of hydrosulfate taken in the stoichiometric ratio for binding of the compounds of manganese, iron, aluminium is Oia. The mixture is subjected to firing in three stages with obtaining pitch: in the first stage, the mixture is subjected to heat treatment at 250°C for 1 h, the second at a temperature of 450°C for 1 h, and the third is at a temperature of 650°C for 3.5 hours. When roasting flow redox processes with the formation of sulfate manganese (II)sulfate iron (II)sulfate of aluminum and the release of sulfur dioxide (SO3oxygen and water vapor from the exhaust gases. As a result of firing the obtained 3306,9 g peck composition, wt.%: 15,79 MnSO4, 5,48 FeSO4, 12,1 Al2(SO4)3, 14,69 SiO2, 51,95 Na2SO4and isolated in the gas phase 315,2 g sulfur dioxide (SO3, 218,9 g of water, 63,0 g of oxygen. Next pitch is cooled and subjected to leaching for 1 h with water, taken in an amount 10582,1, the Mass ratio peck: water is 1:3,2. When leaching is heated the reaction mass to a temperature of 63°C. the pH of the reaction mass is 6.7, Wednesday malokartinia. Leachate get 13889 g of slurry containing 182,38 g of aluminum hydroxide and 485,9 g of silicon dioxide in the form of sediment. The slurry is filtered, the separated sludge stage leaching, washed, dried and 668,3 g of dry sludge is directed to the production of construction material. 13220,7 g of the filtrate, containing in %: 3,95 MnSO4, 1,37 FeSO44, which 9.22 Na2SO4handle with 2464,0 g of 20%sodium carbonate solution. When interacting with sodium carbonate, sulphate of manganese (II) and iron (II) form the corresponding carbonate and precipitate. Sodium carbonate (492,8 g) is taken in the quantity stoichiometrically required for the formation and deposition of carbonates of manganese and iron. The resulting suspension (15684,7 g) carbonates of manganese and iron are sent to the filtering. The precipitate is washed with water and dried, the result is 543,7 g of manganese concentrate, containing in wt.%: 73,09 MPMs3, 25,41 F3, 0,69 Na2SO4, 0,31 NaHSO4and 0.5 moisture. The filtrate number 15119 g containing 12,41% Na2SO4and 5.56% NaHSO4directed to the stage absorption stage exhaust gases of firing. When absorption is absorbed 315,2 g of sulfuric anhydride and 218,9 g of water vapor and get 15653,1 g of a solution containing 2904 g of sodium hydrosulphate. The solution hydrosulfate evaporated, isolated crystals are dried to obtain sodium hydrosulphate, which return a mixture of crushed ore with getting charges. Washing solutions filtration of the slurry and the slurry of carbonate of manganese and iron are sent to the stage leaching peck.

1. The method of processing of manganese ores, including the crushing ore, the receipt of the charge, the firing of the charge, the translation in the solution of margins and related impurities, the separation of the sludge from the solution, precipitation of compounds of manganese, the allocation of manganese concentrate filtration and drying the precipitate, wherein the pre-mixing the crushed ore with sodium hydrosulphate, taken in an amount required for stoichiometric binding of manganese and impurities in sulfates, then hold firing the resulting mixture in three stages with obtaining pitch, and at the first stage, the mixture is subjected to heat treatment at a temperature of 200-300°C for 1-2 h, the second at a temperature of 400-500°C for 0.5-1.5 h, the third at a temperature of 600-700°C for 2-4 h while the translation of manganese and related impurities in the solution is performed by leaching peck water at a temperature of 40-80°C for 0.5-1 h and the mass ratio peck:water=1:(3-4), then the resulting slurry is filtered with the Department of sludge stage leaching, and the filtrate is treated with sodium carbonate solution, taken in the quantity stoichiometrically required for the binding and precipitation of compounds of manganese (II) and iron (II), the resulting suspension is filtered, the precipitate of carbonate of manganese (II) and iron (II) washed with water and dried to obtain the target product - manganese concentrate and filtrate, representing a solution of the sulphate and sodium hydrosulphate, direct to the stage of absorption of the off-gases of kiln containing ser the initial anhydride, obtaining solution of sodium hydrosulphate, after evaporation, crystallization and drying receive sodium hydrosulphate, which is directed to mix with the crushed ore with getting charges.

2. The method according to claim 1, characterized in that the slurry stage leaching consisting of aluminum hydroxide and silica, washed with water, dried and direct the production of construction material.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: method involves leaching alkali and alkali-earth metals with a solution of a chlorine-containing reagent and separating the insoluble residue containing manganese dioxide. The ore undergoes preliminary decarboxylation via thermal treatment at temperature 750-1000°C for 2-4 hours to obtain coal tar. The chlorine-containing reagent used when leaching the coal tar is 10-40% aqueous ammonium chloride solution, taken in weight ratio ore: ammonium chloride equal to 1:1-2. Leaching is carried out at temperature 20-100°C for 1-2 hours. After separating the insoluble residue, the filtrate is carbonised with exhaust gases from the ore decarboxylation step, followed by separation of the obtained calcium carbonate and return of the aqueous ammonium chloride solution to the coal tar leaching step.

EFFECT: obtaining quality end product - manganese dioxide concentrate and a by-product - calcium carbonate using a zero-discharge process scheme.

1 dwg, 1 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in separation of coal electrode and zinc cylinder, in flushing and dissolving in sulphuric acid. Also, flushing from ammonia chloride and zinc hydroxide is carried out with 0.2 M solution of sulphuric acid (H2SO4). Upon flushing residue of manganese oxide (IV) (MnO2), oxy-hydroxide of manganese (MnOOH) and coal mass (C) is crumbled in ball mills. Crumbled residue is dissolved in sulphuric solutions of concentration 0.05 mole/l containing 0.05-0.1 mole/l of oxalic acid at ratio of concentrations of ions of manganese and oxalic acid 1:5 at pH=1-2.2 and temperature of solution 80°C. Upon dissolving solution is filtered for removal of coal mass. Residues of zinc ions are removed from solution with isoamyl alcohol of 200 ml volume at presence of 2 M solution of ammonia thiocyanate and 0.5 M HCl, and there is performed neutralisation with 0.5 M solution of caustic soda (NaOH). Further, produced solution is evaporated at temperature 100°C to obtaining mass of crystalline compounds of composition sodium trioxalomanganate (IV) Na4[Mn(C2O42-)3] and salt of sodium oxalate (Na2C2O4). Produced mass is baked in atmosphere containing oxygen at temperature 400-500°C with production of MnO2 as a final product.

EFFECT: raised efficiency and ecological safety of procedure.

4 dwg, 3 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in sorption of cobalt on complex forming ionite from manganese containing solution and of desorption of cobalt from ionite. Desorption of cobalt is performed with solution with pH value=4.5÷5.5 containing ions of copper and(or) nickel possessing higher affinity to functional groups of ionite, than cobalt.

EFFECT: reduced amount of solution processing stages, reduced consumption of reagents and process equipment, increased efficiency and reduction of process cost.

1 dwg, 1 ex

FIELD: metallurgy.

SUBSTANCE: procedure for separation of scandium from manganese consists in contacting solution containing scandium and manganese with extractant in interval of pH 2.9-3.3 during 30 minutes. Contacting is carried out with extraction of manganese. As extractant there is used 0.25 M solution of N-(hydroxi-5-nonobensyl-β-hydroxi-ethyl-methyl-amine (NBEA-2) in thinner.

EFFECT: raised coefficient of metals separation.

5 ex

FIELD: metallurgy.

SUBSTANCE: invention refers to metallurgy, particularly to procedure for purification of manganese concentrates from phosphorus. The procedure consists in agglomeration of concentrate with sodium salts at 950-1000°C and weight ratio 1:0.4, and in successive water leaching with transfer of phosphorus into solution. Further concentrate is filtered and dried. Also leaching is carried out under effect of ultrasonic oscillations of 18·103-22·103 Hz per second frequency during 15-30 minutes. Finished concentrate is filtered and dried in ultrasonic fields of 18·103-22·103 Hz per second frequency.

EFFECT: upgraded quality of manganese concentrate by means of reducing concentration of phosphorus in it.

2 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: thermal reduction by heating charge containing reducer and manganese compound is performed at temperature 700-750°C in inert atmosphere. As manganese compound there is used manganese oxide (III) or manganese oxide (IV), or manganese chloride, while as reducer there is used hydride of lithium taken in excess at amount of 25-50 wt %. Also lithium chloride is additionally introduced into charge at ratio of lithium to lithium hydride taken in excess in moles equal to 2:1. Heated charge is conditioned during 30-90 min. Further manganese is extracted out of reaction mixture by means of cooling, flushing with water and filtering.

EFFECT: production of manganese in form of fine crystal powder and reduced expenditures.

7 cl, 4 ex

FIELD: process engineering.

SUBSTANCE: invention relates can be used in metallurgy, electronics and in production of pigments and welding electrodes. Wastes of production of ferrous alloys containing, mainly, manganese represent slimes of fume gases washing from furnaces producing ferromanganese and silicon manganese. Said wastes are directed for thermal sulphating 1 that comprises furnace processing of material fed from mixer wherein said wastes have been subjected to treatment by acid with flow rate approximating to stoichiometric. Teflon chutes are used inside the furnace to produce SO2. Then hydrometallurgical phase is performed consisting of vatting stage 2, primary 3 and secondary 4 washing stages and that of conditioning. Vatting is carried out at intensive mixing in reactor with coating that regulates acidity using anolyte of electolyser or synthetic anolyte. Primary washing stage 3 is carried out in the same reactor till pH increases to values approximating to neutral one by removing, mainly, iron and aluminium. Produced fine pulp is filtered in pressure filter, flushed by water, preferably, in the same pressure filter, to produce inert wastes. Fine pulp flushing water is added into the mixer or used again to concentrate manganese therein. At secondary flushing stage 4, zinc impurity is removed by settling ZnS. Solution obtained after conditioning 5, is directed to electrolysis 6 to produce electrolytic manganese.

EFFECT: possibility to recover wastes to produce 99,9%-pure manganese.

5 cl, 6 dwg

FIELD: metallurgy.

SUBSTANCE: method includes grinding of raw materials up to fineness less than 0.074 mm. After grinding it is implemented leaching during 20-40 minutes at temperature 40-50°C 0.5-1.0 "н." by solution of oxalic acid at relation of liquid to solid in pulp 3:1 with transferring of phosphorus into solution. After leaching it is implemented pulp filtration.

EFFECT: selective dissolution of phosphorus from raw materials.

2 tbl, 1 ex

FIELD: hydrometallurgy, chemical technology.

SUBSTANCE: invention relates to the leaching reaction of manganese from manganese-oxide ores. Solution used for leaching manganese-oxide ores contains the following components, wt.-%: sulfuric acid, 19.0-20.0; ethylene glycol, 30.0-80.0, and water, the balance. Using the proposed solution that is stable in strongly acid media and at high temperatures (200°C) provides enhancing the selective rate of dissolving manganese oxides from depleted manganese-oxide ores. Invention provides the complete dissolving manganese oxides based on surface reduction of manganese dioxide.

EFFECT: improved and valuable chemical properties of solution.

1 dwg, 2 ex

FIELD: processes for extracting matters with use of sorbents, possibly in non-ferrous and ferrous metallurgy, for cleaning industrial and domestic sewage.

SUBSTANCE: sorption is realized on anionite containing groups . Before sorption anionite is subjected to preliminary acidic, alkali or aqueous treatment. Sorption is realized for period less than 2 h, namely after preliminary acidic treatment of anionite at pH =4 - 5 or 7 - 8; after alkali treatment of anionite at pH 3 - 6 and after aqueous treatment at pH = 2.4 - 8.5.

EFFECT: determination of optimal conditions for rapid and effective extraction of manganese VII ions out of aqueous solution.

5 dwg, 4 ex

FIELD: chemistry.

SUBSTANCE: method involves leaching alkali and alkali-earth metals with a solution of a chlorine-containing reagent and separating the insoluble residue containing manganese dioxide. The ore undergoes preliminary decarboxylation via thermal treatment at temperature 750-1000°C for 2-4 hours to obtain coal tar. The chlorine-containing reagent used when leaching the coal tar is 10-40% aqueous ammonium chloride solution, taken in weight ratio ore: ammonium chloride equal to 1:1-2. Leaching is carried out at temperature 20-100°C for 1-2 hours. After separating the insoluble residue, the filtrate is carbonised with exhaust gases from the ore decarboxylation step, followed by separation of the obtained calcium carbonate and return of the aqueous ammonium chloride solution to the coal tar leaching step.

EFFECT: obtaining quality end product - manganese dioxide concentrate and a by-product - calcium carbonate using a zero-discharge process scheme.

1 dwg, 1 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: concentrate is subjected to two-stage oxidising roasting. Note here that, before first stage, said concentrate is mixed with sulfur-binding additive to perform first roasting stage at 550-650°C for 15-30 min. Prior to second roasting stage, molybdenum concentrate is added to calcine produced at first stage in amount of 10-30 wt % from concentrate used in first roasting step. Second roasting is performed at 600-670°C for 30-40 min with subsequent leaching of molybdenum and rhenium from calcine obtained in first step.

EFFECT: higher yield of molybdenum.

2 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: proposed method comprises irradiating ores by SHF-field and processing them by acid and/or oxidiser solution to transfer noble metals into solution. Prior to irradiation by SHF-field initial material is subjected to fractionation in upflow with variable hydrodynamic conditions at linear speed of said upflow of 10-50 m/h to produce concentrated fraction. Concentrated fraction is subjected to said irradiation. Note here that irradiation is executed in microwave range at load that allows heating the materials to 180-280°C. Then, noble metals are leashed into solution.

EFFECT: higher yield of noble metals.

1 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: method for industrial production of pure MgCO3 involves crushing olivine-containing rock and bringing the crushed rock into contact with water and CO2. At the first step, which is carried out under pressure, a dissolution reaction takes place according to the equation Mg2SiO4(s)+4H+=2Mg2++SiO2(aq)+2H2O. At the second step, deposition is carried out at higher pH. The following reactions take place: Mg2++HCO3-=MgCO3(s)+H+ and Mg2++CO32-=MgCO3(s). The presence of HCO3- and H+ ions is mainly a result of reaction of CO2 and water.

EFFECT: invention enables to produce pure magnesium carbonate from rock while binding free carbon dioxide gas.

19 cl, 4 dwg, 2 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in heat treatment of source concentrate with two-component salt mixture, one component of which corresponds to ammonia nitrate, in production of reaction mass and in transfer of gold and palladium into water solution. Also, per-sulphuric acid ammonia is the second component of salt mixture. Heat treatment is performed with salt mixture consisting of ammonia nitrate and per-sulphuric ammonia at ratio NH4NO3:(NH4)2S2O8 =1:1 taken at amount of 5-20% of concentrate weight. Reaction mass is heat treated at temperature 220-280°C during 0.5-1.5 hours. Gold and palladium are transferred into water solution by washing with water produced after heat treatment of reaction mass. The purpose of the invention is development of the procedure for extraction of gold and palladium from concentrates by oxygen-free process.

EFFECT: high degree of extraction of metals from concentrates.

2 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in raw stock fine crumbling, in autoclave oxidising leaching under pressure of oxygen, and in cake cyaniding with extraction of gold into cyanic solution. Also, autoclave oxidising leaching is performed at temperature 125-150°C. Upon leaching cake containing elementary sulphur is brought to pulp with water. Alcali agent is added into pulp and sulphur is autoclave oxidised at its dissolving and oxidation to a sulphate state. Cake is subjected to cyaniding after autoclave oxidation of sulphur.

EFFECT: increased extraction of gold into cyanic solution.

4 cl, 2 dwg

FIELD: mining.

SUBSTANCE: underground leaching method of mineral resources from raw material involves filling of cavities of underground openings in the form of chamber with raw material, and their sealing. Then, erection of pipelines and branch pipes for supply of leaching solution in raw material, air for oxidation of raw material minerals and supply of productive solution for processing is performed in openings. Prior to leaching the mine water is collected and leaching solution is prepared in the built chamber of capacity, which is mentioned below. Leaching is performed at increased temperatures and pressure which is maintained during the required period of time by shutting off gate valves of branch pipes which are used before opening for supply of leaching solution in raw material and supply of productive solution for processing.

EFFECT: lower costs for leaching of raw material owing to reducing capital investments, energy and material consumption.

1 dwg

FIELD: metallurgy.

SUBSTANCE: procedure for extraction of metals out of mineral raw materials consists in leaching crumbled source mineral material in not less, than two serially connected reactors and in mixing. Further, product of leaching is size-graded into sand and slime fractions. Sand fraction is leached in not less, than two serially connected reactors at mixing. Metals are extracted from phases of the slime fraction and product of leaching of the sand fraction.

EFFECT: raised degree of crumbled mineral raw material leaching, reduced power expenditures for processing, reduced volume of reactors, and increased efficiency of leaching.

10 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in leaching phospho-gypsum with solution of sulphuric acid and in dissolving rare earth metals into solution. Prior to leaching phospho-gypsum is washed from phosphorus with water. Phosphorus is washed out in a closed cycle with dissolving of phosphorus into solution and its successive utilisation; it is run through a layer of carbonate waste and is returned to a reverse cycle of phospho-gypsum washing with water depleted of phosphorus. Phospho-gypsum is leached with solution of sulphuric acid at its concentration from 3 to 250 g/l. Rare earth metals are extracted from leaching solution by their concentration on cation exchanger, by their removing from cation exchanger with production of a commodity regenerate and by their return into the reverse cycle of leaching water solution depleted of rare earth elements.

EFFECT: repeated utilisation of sulphuric acid solution at treatment of phospho-gypsum, obtaining maximum concentrated solution of rare earth metals cleared from impurities, reduced amount of phospho-gypsum wastes and their reclamation in building.

2 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in leaching with chloride solution at supply of chlorine, in purification of solution from copper and in production of copper sulphide cake, in extracting concentrate of precious metals and in electro-extraction of nickel from solution. Prior to leaching matte is separated to a sulphide and metallised fractions. The sulphide fraction is subjected to leaching with chloride solution with supply of chlorine. The metallised fraction produced at separation of matte is added into pulp produced at leaching thus performing purification of solution from copper and its withdrawal to copper sulphide cake. Upon purification of solution from copper solution is purified from iron, zinc and cobalt. Copper sulphide cake is roasted and produced cinder is leached. Solution is directed to electro-extraction of copper, while concentrate of precious metals and chamber product are extracted from residue by flotation.

EFFECT: reduced material and operational expenditures and losses of non-ferrous and precious metals.

2 cl, 12 ex, 2 dwg

FIELD: metallurgy.

SUBSTANCE: method includes graining of uranium ore, its sulphatisation by sulfur acid at presence of nitric acid. Additionally nitric acid is fed in amount required for oxidation of sulphides containing in uranium ore. Then received grains are subject to thermal treatment at temperature 200-300°C and leaching by water.

EFFECT: reduction of consumption of mineral acids for reprocessing of uranium ore and in increasing of uranium extraction.

5 ex

Up!