Method for obtaining dephosphorised concentrate of oolitic iron ores
 Method of processing manganese-containing material / 2448175Method involves transfer of manganese and accompanying impurities into a solution through two-step treatment of the starting material with hydrochloric acid and absorption of chlorine with an alkaline solution. Further, impurities are separated to obtain a manganese salt solution which is then treated. The first step uses waste hydrochloric acid with concentration 1-10% with solid to liquid ratio equal to 1:(3-5). A manganese-containing residue is separated from the obtained pulp, where said residue is then treated at the second step with waste inhibited hydrochloric acid with concentration 20-24% and content of inhibitor of not less than 5 wt %, reaction with iron of which results in insoluble complex compounds, where said inhibitor is in form of quaternary ammonium salts, with molar ratio manganese:HCl=1.0:1.1. The insoluble residue of aluminosilicates is then separated and the manganese salt solution is then processed using existing methods. |
 Extraction of metals from sulphide minerals / 2448171Method has been elaborated for two-stage dilution of nickel in leaching acid. Suspension of mineral and acid is activated by oxidation. It is performed during T1 time by means of electrolysis or alternatively chemically, by adding for example of oxidating acid to mineral. After activation the suspension is exposed in oxygen-free conditions during T2 time. During T2 time much quicker dilution of sulphide begins; quick decomposition of sulphide gives the possibility to nickel to be diluted and thus leached from mineral. Diluted nickel is extracted from leaching acid for example by electrochemical extraction. |
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Method of processing chemical concentrate of natural uranium / 2447168 Method involves leaching the concentrate with aqueous nitric acid solution at high temperature to obtain a pulp consisting a solid and an aqueous phase. The aqueous phase is then separated by filtration from the solid phase in form of uranium nitrate solution. Uranium is then extracted from the nitrate solution using tributyl phosphate in a hydrocarbon solvent. The extract is washed and uranium is re-extracted. Leaching is carried out by adding nitric acid and water in an amount which enables to obtain a nitrate solution in the aqueous phase of the pulp, said nitrate solution containing dissolved silicon in concentration of 2.5-3.7 g/l. The solid phase, which consists of insoluble concentrate residues, is separated by filtration from the solution which contains dissolved silicon, uranium in concentration of 170-250 g/l and nitric acid in concentration of 80-120 g/l. Filtration is carried out not more than 24 hours after leaching, preferably not more than 5 hours after leaching. |
 Method of processing chemical concentrate of natural uranium / 2444576Method involves leaching in order to dissolve uranium when the concentrate reacts with nitric acid solution to obtain pulp from the concentrate. Uranium is then extracted from the pulp using tributyl phosphate in a hydrocarbon solvent. The extract is washed and uranium is re-extracted. Extraction is carried out from freshly prepared pulp which is obtained through direct-flow reaction at temperature 20-65°C of a stream of a suspension of the concentrate in water which is prepared beforehand and a stream of nitric acid solution with flow rate ratio which ensures nitric acid concentration in the pulp of 25-120 g/l. The period from the beginning of leaching to the beginning of extraction is not more than 10 minutes. |
 Method for obtaining cobalt and its compounds / 2444574Method for obtaining cobalt and its compounds involves conversion of cobalt from cobalt-bearing raw material to the solution; deposition of cobaltic hydroxide (III) using oxidiser and neutraliser, dilution of cobaltic hydroxide (III) with conversion of cobalt (III) to cobalt (II). Then, the obtained solution is cleaned from impurities and metallic cobalt or its compounds are obtained. Cobaltic hydroxide (III) is diluted with the participation of recovered reduced forms of iron and/or copper salts in the range of oxidation-reduction potential of 300-700 mV relative to silver-chloride comparison electrode and pH 1-3, thus adjusting the temperature of the process by means of evaporation cooling. Recovery of reduced forms of iron and/or copper is performed in a separate unit using the reducer. At insufficient amount of copper and iron in raw material supplied to the process there performed is cleaning of leaching solution from copper by cementation and recirculation of cleaning product to the recovery stage of reduced forms of iron and/or copper. |
 Manufacturing method of concentrate of precious metals from sulphide copper-nickel raw material / 2444573Method involves separation of Bessemer matte into metallised and sulphide fractions and oxidation leaching of metallised fraction with solution at the controlled chlorine supply. At that, ratio of sulphur and copper contained in metallised fraction is 0.3-0.7. Leaching is performed in the value range of oxidation-reduction potential of 430-470 mV, preferably 440-450 mV. Sludge of baths of electrolytic nickel refining of processing technology of sulphide Bessemer matte fraction is supplied together with metal faction of Bessemer matte for leaching. |
 Method for extracting rare metals from ash-slag masses of used underground gas generator / 2443788Intensified extraction of underground water is performed from used underground gas generator through the main water drain wells. Then, there created is cone of depression in the section of used underground gas generator for minimisation of underground water level and maintenance of maximum depression in the section of used underground gas generator. Treatment of ash-slag masses is performed using the solvent injected to the used underground gas generator, and leaching and collection of rare metal dissolved in the solvent extracted from underground gas generator is performed in surface chemical complex. |
 Procedure for extraction of aluminium and iron from ash-and-slag waste / 2436855Procedure for extraction of aluminium and iron from ash-and-slag waste consists in treatment with solution of sulphuric acid and in extraction of aluminium containing components into solution. Before extraction of aluminium containing components into solution waste is subjected to classification and multi-stage magnetic separation at periodic increase of field of magnetic induction for complete extraction of magnetic fraction containing iron. |
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Method of extracting lanthanides from apatite concentrate / 2430885 Apatite concentrate is decomposed with nitric acid to obtain nitrate-phosphate solution. Calcium nitrate and sodium fluosilicate are successively extracted from the solution. The solution is neutralised with ammonia to form a precipitate of phosphates of the main part of lanthanides and a mother solution with the residual part of lanthanides. The mother solution is treated by bringing it into contact with an amorphous titanium phosphate-based sorbent at pH of the solution equal to 1.4-1.7 with concentration of the residual part of lanthanides in the sorbent. The lanthanide-rich sorbent is separated, washed with water and treated with 0.5-3.0 M mineral acid with desorption of lanthanides. The amorphous sorbent used is one of the sorbents with the following composition: TiOHPO4·nH2O, (Ti1-xZrx)OHPO4·nH2O, TiONH4PO4·nH2O, (Ti1-xZrx)ONH4PO4·nH2O, where n≥1, x=0.05-0.5. |
 Heap leaching method of antimony ores / 2429304Method involves ore pre-benefication with X-ray radiometric separation and further heap leaching of antimony from ore. At that, leaching is performed with solution containing sulphuric acid and sodium chloride in presence of manganese compounds of oxidation degree of not less than 3 or with solution containing chlorhydric acid, active chlorine and sodium chloride, or with solution containing sulphuric acid and sodium chloride in presence of chlorinated lime. Productive antimonous chloride solution obtained after leaching is supplied for removal of antimony with cementation, hydrolysis or electric deposition. After removal of antimony the solutions are regenerated with release of manganese compounds and returned for leaching. |
 Procedure for purification of iron containing material from arsenic and phosphorus / 2413012Procedure consists in crumbling material and in its leaching. Also, material crumbling and leaching is performed in concentrated solution of sodium chloride when compounds of arsenic and phosphorus are dissolved to suspension. Produced suspension is subjected to gravitation separation to a solid phase of concentrated iron containing material and to suspension of dispersed impurities. The separated solid phase of iron containing material is further subjected to washing with acid concentrated solution of sodium chloride. |
 Procedure for refinement of iron ore from arsenic and phosphorus / 2412259Procedure consists in crumbling ore, in its mixing with carbon reducer and in mixture sintering. Also, before sintering ore is additionally mixed with carbonate slime; mixture is sintered in oxygen containing medium. Upon sintering arsenic and phosphorus are leached with solution of sodium hydroxide and simultaneously are subjected to wet magnetic concentration. |
 Method of oxidation of sulphide minerals / 2385954Method of sulphide minerals oxidation includes feeding of pulp with sulphide minerals and oxidising agent into reactor with following its blending and outlet of oxidised composition from reactor. During blending of pulp and oxidising agent in internal chamber of reactor in turbulent conditions it is implemented mechanical activation of surface of solid phase of pulp and disperse of oxidising agent. Outlet of oxidised compositions from internal chamber into external chamber of reactor is implemented under action of pressure created by inlet flow of pulp through openings overlapped in top part of internal chamber by regulator of pulp outlet. Additionally liquid phase of pulp is continuously circulates from external chamber into internal chamber of reactor. Oxidation rate of sulphide minerals is regulated by means of changing of oxidising agent concentration in pulp ensured b changing of its amount form 3000 up to 15000 mg·l/h at activation of pulp in reactor. |
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Method of silicon- calcium-containg concentrate purification from admixtures / 2365648 Invention relates to method of purifying natural and technological silicon- calcium-containing concentrate from admixtures of sulfur, phosphorus and carbon and can be applied in production of materials used in coating of welding electrodes. Method includes crashing of concentrate into fractions not more than 100 mcm. Milled concentrate is distributed in layer not more than 1mm on working surface, which has coefficient of light flow reflection not less than 0.6. Then concentrate is processed by influencing on it by movable laser ray with density of irradiation power 102-106 wt/cm2 at rate of laser ray axis movement 0.3-2.0 cm/s relative to processed concentrate, admixtures being removed as gaseous products from zone, located at distance 2-4 mm from laser ray axis. |
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Method of reproprocessing of the sulfide products / 2272081 The invention is pertaining to reprocessing of sulfide ores and concentrates. The sulfide products are treated in an alkaline melt. In the capacity of the melt they use a mixture prepared at least out of two alkalis from NaOH sodium hydroxide and KOH potassium hydroxide in the mass ratio of NaOH : KOH - from 0.65 up to 0,75. The invention allows to reduce the operational temperature of the alkaline smelt process. |
 Method of producing pellets from recovered iron and method of producing cast iron / 2447164Moulded powdered pellets containing iron oxide and carbon are heated and recovered in rotary-hearth kiln. Note here that pellets are produced using stock wherein mean diameter of iron oxide particles makes 50 mcm or smaller. Note here that carbon oxide-to-carbon dioxide ratio in recovery zone is kept varying from 0.3 to 1. Recovery is conducted at 1400°C or lower to produce recovered iron-containing pellets with iron schooping of 50-85% and fractions of residual carbon of 2% or less. |
 Installation for direct melting / 2431682Installation consists of fixed reservoir for direct melting containing chimney and side wall, of unit for supply of solid source material including metal containing source material and carbon containing material from place of location of source of solid source materials at distance from reservoir, of unit of supply of oxygen containing gas from place of location of source of oxygen containing gas at distance from reservoir. The installation also has a unit for withdrawal of exhaust gas designed for facilitation of flow of exhaust gas from the reservoir. The unit for withdrawal of exhaust gas has two pipelines of exhaust gas of matching diameter. The pipelines pass outside from the reservoir. |
 Installation for direct melting / 2431681Installation consists of fixed reservoir for direct melting with unit for supply of solid particles for introduction of hot metal containing source material and carbon containing material. Also, the unit supplying solid material has multitude of tuyeres for blow-in of solid particles passing downwards and inside through windows in a side wall of the reservoir. Tuyeres for blow-in of solid particles have multitude of tuyeres for blow-in of metal containing material into the reservoir and multitude of tuyeres for blow-in carbon containing material into the reservoir. Also, multitude of tuyeres for blow-in of metal containing material into the reservoir are arranged in pairs along perimetre of the side wall of the reservoir for direct melting, while separate tuyeres for blow-in of solid carbon containing material are positioned between neighbour pairs of the tuyeres for blow-in of metal containing material. |
 Installation for direct melting / 2431680Installation consists of fixed reservoir containing chimney and side wall with lower cylinder section, upper cylinder section of less diametre, than lower section and transitive section connecting upper and lower sections. The reservoir also has the unit for supply of solid materials for delivery of solid source material including metal containing source material and carbon containing material into the reservoir and the unit of oxygen containing gas supply from a source of oxygen containing gas located beyond boundaries of the reservoir to the reservoir. The unit for supply of oxygen containing gas has the unit of blow-in of gas equipped with multitude of tuyeres for oxygen containing gas blow-in to the reservoir passing downwards through orifices in the transitive section of the side wall of the reservoir and the gas supply unit passing from the source of gas located beyond the boundaries of the reservoir for supply of oxygen containing gas to the unit of gas blow-in. |
 Installation for direct melting / 2431679Installation consists of fixed reservoir for direct melting with liquid bath, of unit for supply of solid particles including metal containing source material and carbon containing material from place of location of source of solid source materials positioned at distance from reservoir. The installation also contains the unit for supply of oxygen containing gas from the place of location of the oxygen containing gas source at a distance from the reservoir. Also, the unit for supply of oxygen containing gas includes a unit for gas blow-in consisting of multitude of pipes for introduction of oxygen containing gas passing through orifices in the reservoir, and a unit of gas delivery channels passing from the place of gas source location at a distance from the reservoir. The unit of gas delivery channels is designed for delivery of oxygen containing gas to the unit of gas blow-in. The unit of gas delivery channels has one main of gas delivery positioned above lower half of the reservoir connected with pipes for gas blow-in. |
 Installation for direct melting / 2431678Installation consists of stationary tank for direct melting with liquid bath, of unit for supply of solid substances containing multitude of tuyeres for introduction of solid substances, of unit supplying oxygen containing gas with multitude of tuyeres for gas injection and of gas supplying main passing around total periphery of tank and positioned at distance from this tank, of spent gas withdrawal unit, of metal pouring unit and of unit for discharge of slag. The installation also consists of multitude of access zones for a bridge crane. These zones are arranged further from centre of the tank relative to the gas supply main to facilitate removal of tuyeres for introduction of solid particles from orifices in a side wall of the tank for direct melting and facilitate arrangement of replaceable tuyeres in these orifices. The installation also consists of multitude of access zones for a bridge crane. These zones are arranged closer to centre of the tank relative to the gas supply main to facilitate removal of tuyeres for gas injection from orifices in a side wall of the tank and facilitate arrangement of replaceable tuyeres in these orifices. |
FIELD: metallurgy.
SUBSTANCE: invention refers to preparation of iron-ore raw material for metallurgical treatment by cleaning the latter from harmful impurities deteriorating the quality of obtained metals and alloys. Method for obtaining dephosphorised concentrate of oolitic iron ores involves high temperature treatment, cooling and leaching of concentrate with mineral acid. High temperature treatment of iron-bearing material is performed in the range of 1350-1450°C in reducing medium with participation of clinker minerals till molten metal and sinters are formed. They are cooled to magnetising roasting temperature of 750-860°C, crushed and separated with magnetic separation into clinker and concentrate. Then, concentrate is cooled to 50-90°C and supplied at that temperature for leaching with mineral acid for dilution of phosphorus.
EFFECT: improved process efficiency.
5 cl, 2 tbl, 1 ex
The invention relates to the field of preparation of iron ore for metallurgical treatment by cleaning the last from harmful impurities that degrade the quality of the metals and their alloys.
In modern conditions the reduction of available quality raw iron ore base for ferrous metallurgy is becoming increasingly important issue involved in technological turnover of billions of reserves and resources oolitic iron ores. The Genesis of most of these ores, for example, as Lisakovsk brown iron ores in Kazakhstan, Bakchar iron ore in Russia and the other, leads to a high content in the oolites of phosphorus to 0.9% and more. Existing standards for pyrometallurgical section upper limit redistribution of phosphorus in iron ore concentrate value of 0.30%.
Exceeding this standard has a harmful effect on the quality of the metallurgical process and its result, for example, worsening removal of slag from the melt surface and increasing the brittleness of the resulting metal.
The problem obesfosforivanie concentrate oolitic iron ores can significantly expand the resource capabilities of ferrous metallurgy.
There are several approaches to solving this problem, based on physical, chemical and combined methods of exposure to particles of ore m the material oolitic structure. Tested mechanical action (grinding and magnetic separation), high-temperature exposure (burning and duplex melting), hydrometallurgy (leaching). Each of the tested methods of removal of phosphorus in iron ore and metal has its own disadvantage.
Mechanically impossible to remove phosphorus to content less than 0.30%, because the phosphorus is part of not only iron-bearing minerals, but also in the composition of the cement mass.
Duplex melting metallurgical charge removes phosphorus from the metal to the required limits, but makes such a metal noncompetitive on its cost because of the dual power.
Leaching of phosphorus mineral acids requires a large consumption of agent (for example, in the case of sulfuric acid per 1 kg leachable phosphorus spent 30 kg acid), complex apparatus registration process, high environmental cost.
Closest to the proposed method are combined physico-chemical methods obesfosforivanie iron ore, including the operation of roasting and leaching. In these methods, the firing prior to leaching, makes phosphorus more available for chemical agent due to recrystallization of iron minerals in L-Fe2O3and concentration of phosphorus between grains GE is the atita. This technique is a combination of high temperature exposure with hydrometallurgy - increases the efficiency of the leaching of phosphorus from iron ore concentrate mineral acids.
The Australian Institute of mining and metallurgy, conducting experiments on obesfosforivanie iron ore Hamersley ridge (Avstral. IMM, 5/97, s-202) spent roasting of the concentrate at a temperature of 500-600°C for 1-1 .5 hours, applying for leaching sulfuric acid in an amount of not less 110-150% of the stoichiometric with respect to phosphorus, at a temperature of 60-80°C, T:W=1:3-1:5, and the leaching time is 2-3 hours. The disadvantage of this known technical solution is high residual phosphorus content in the concentrate to about 40% of the original.
Joint stock company of closed type "Mekhanobr engineering" suggested method of purification of iron ore concentrate from the impurities of phosphorus (RF patent No. 2184158), including roasting, cooling, leaching with a mineral acid under given parameters of leaching, separation of the liquid phase from the solid, and iron ore concentrate is subjected to oxidizing roasting at a temperature of 800-1000° C exposure is not more than one hour. The leaching is carried out with sulfuric or nitric acid at a ratio of T:W=1:(1-2) and a temperature of 20-50°C, ending the process when it reaches a horse is Noah acidity of the solution 6-10 g/L. The main disadvantage of this technical solution is the relatively high consumption of thermal resources and a significant consumption of acid.
The last known technical solution adopted for the prototype.
The task is to increase the efficiency of obtaining objectstring concentrate oolitic iron ores due to conditions selection modes, high-temperature and leaching.
The technical problem is solved as follows. To achieve the technical result of the proposed high-temperature processing of ore carried out in the temperature range of 1350-1450°C in a reducing environment with the participation of clinker minerals to the melt formation and class. The spectrum of iron and clay minerals, cooled to a certain temperature level, crushed and divided into clinker and iron ore concentrate.
The concentrate is heated to a certain temperature level, is treated with mineral acid effective to dissolve the phosphorus concentration rate of 20 kg acid per 1 ton of concentrate. The solution after leaching, phosphorus is used to produce phosphate fertilizers.
The positive effect of changes to the prototype method due to the fact that the heat process resource consumed simultaneously to obtain two products - clinker and zhelezorudnog the concentrate, while the phosphorus in the melt SPECA, partially departs in clinker role of slag and phosphorus remaining in the concentrate becomes more available for leaching. In addition, the heat resource of high-temperature processing of the raw materials used for optimal regimes of magnetic separation concentrate and leaching process.
Due to the waste part of the phosphorus in the "clinker slag and its greater availability in concentrate leaching reduced specific consumption of acid on obespechenie. The solution of environmental problems neutralization of waste leaching through the utilization of phosphate productive solution in phosphate fertilizer production significantly reduces the cost of concentrate.
Getting partially objectstring concentrate oolitic iron ore offered by the patent RF №2402499, while the spectrum is cooled to the temperature range of magnetizing roasting 750-860°C, crushed and through magnetic separation, grinding is divided into clinker and concentrate. The concentrate is cooled to a temperature range of 50-90°C and fed to the processing of mineral acid is sulfuric H2SO4nitrogen HNO3or HCl salt.
When the content in the concentrate of calcium compounds, mainly calcite, caso3in fewer than 1% of the use is as sulfuric acid, when the content of calcite about 1% nitric acid and when the content of calcite over 1% - hydrochloric acid. All acids used diluted: 51% H2SO4; 43% HNO3and 36% HCl. Based on the need to ensure efficiency and completeness of the completion of the leaching process, the following modes of process asbestosfree concentrate various acids:
- 51% H2SO4with respect to T:W=1:1 and a temperature of 50-60°C for 60 minutes;
- 43% HNO3with respect to T:W=1:1 and a temperature of 60-70°C for 45 minutes;
- 36% HCl with respect to T:W=1:1 and a temperature of 70-90°C for 30 minutes.
Experimental verification of the proposed method in laboratory and pilot-scale conditions on the Bakchar and lysakowski ores showed the possibility of obtaining concentrates with iron content of 53-60% and phosphorus 0.12 to 0.29 per cent.
An example implementation of the invention
Positive results solve phosphorus removal prior to refining to achieve the maximum cost reduction of metallurgists is achieved at the Lisakovsk Mining and processing plant (Kazakhstan) in the period 2000-2009, by implementing technologies, including heat treatment of the gravitational-magnetic concentrate with subsequent leaching it into sulfuric acid, are presented in table 1.
| Table 1 | |||
| The chemical composition of the concentrate Lisakovsk oolitic ores | |||
| Product | Mass fraction, % | ||
| Fe | P | SiO2 | Al2O3 |
| Source | 49,0 | 0,79 | 10,7 | 4,5 |
| End | 60,0 | 0,19 | 7,8 | the 4.7 |
Close to the prototype of the technological scheme of asbestosfree concentrate Lisakovsk oolitic ores with the rise in energy prices in 2009 became unprofitable. However, the achieved results of the combined physico-chemical effects on oolitic iron ore removal from concentrate more than 80% of phosphorus and an increase in iron content in the concentrate to 60% - stimulated further improvement of the method for its application to Bakchar phosphorous iron ore oolitic structure. And, first of all, it was required to reduce specific heat consumption in operation high temperature is osdate for iron ore.
In 2008 he was offered the technology co-firing, fusion and sintering at a temperature of 1350-1450°C iron and clinker minerals, allowing to obtain partially obestsvechenny concentrate oolitic iron ore (RF patent No. 2402499). The present invention improves the quality of the separated concentrate by conducting the separation in the temperature range magnatunebrowser firing 750-860°C by increasing the iron content and increases its output.
Bakchar iron ore contains phosphorus in an amount to 0.46(1,1)% P(P2O5). When sintering the redistribution of iron obtained from this ore will contain 0,9-1,2% P, while odnoslotovyj Converter process is feasible when the phosphorus content is not more than 0.3% P. a restriction on the content of phosphorus for ores/concentrates, suitable for direct open-hearth redistribution is less than 0.15% P. the quality Requirements of iron ore concentrates, pelletized for undomanager redistribution on electrostatically installations, provide the maximum phosphorus content in the pellets and briquettes - a 0.02% P.
Thus, the evidence necessary to further reduce the phosphorus content in the separated concentrate Bakchar iron ore is not in doubt. Guaranteed hydrometallurgy 80%removal of phosphorus from the end of the waste makes possible its use in pyrometallurgy, giving more than 90% of the volume produced in Russia metal.
A wide range of content of calcium minerals in Bakchar iron ore - 0,43÷2,34% involves the use of various acids in the leaching of various types of ores.
Taking into account the proposed typing and chemical composition of the Bakchar iron ore (Belous NH Dressability, agglomeration and technical-economic indicators of pretreatment of Bakchar iron ore. - Novosibirsk : IGD so an SSSR, 1963) proposed the appropriate use of acids for leaching of phosphorus in the extraction of various types of ore and mixed ore (see table 2).
| Table 2 | ||||||
| The applicability of the acid to the leaching of phosphorus from natural types Bakchar iron ore | ||||||
| Natural ore | I | II | III | IV | V | VI | A mixture of I-VI |
| The phosphorus content, % | 0,14 | 0,34 | 0,54 | 0,57 | 0,54 | 0,4 | 0,46 |
| The content of calcium mineral, % | 0,58 | 2,34 | 0,71 | 0,40 | 0,40 | 0,43 | 0,41 |
| Mineral acid | HNO3 | HCl | HNO3 | H2SO4 | H2SO4 | H2SO4 | H2SO4 |
| Note: | Type I - siderite ore with glauconite; | |||||
| Type II - sand ore with sideritis cement; | ||||||
| Type III - chamosite-hydrogeology ore with sideritis cement; | ||||||
| Type IV - hydrogeology ore; | ||||||
| V - type hydrogeology ore with chamosite; | ||||||
| VI - type hydrogeology ore with quartz. | ||||||
When organizing an open excavation mining sm is si types Bakchar iron ore, similarly, the career development plan Lisakovsk field, it is appropriate as well as in Lisakovsk Mining, the use of sulfuric acid. If the selective testing of each ore type with separate storage possible choices as a leaching agent nitric or hydrochloric acids.
In addition, the choice of acid may affect the economic feasibility of expanding the range of phosphate fertilizers produced by recycling Vasilchenko product.
For example, in addition to the simple superphosphate and precipitate can be obtained in the case of the use of nitric acid azotosoderjashchig superphosphate (14% digestible P2O51,5-2% N) and ammonium dihydrogen phosphate (47-51% digestible P2O5, 10-10,5% N).
In General, the proposed technical solution to the problem of increasing the efficiency of obtaining objectstring concentrate oolitic iron ores are provided:
- saving heat source when the joint firing, melting and sintering of iron and clay minerals;
- increase the yield and quality of magnetic iron ore concentrate through a separation in the temperature range of magnetizing roasting and waste part of the phosphorus in the "clinker slag";
- creation of optimal temperature regimes through the use of thermal inertia ohlazhdaem the concentrate;
- selection on the basis of experimental data of the concentration of the acid, the ratio of T:W time and leaching;
- use Vasilchenko phosphorus fertilizer.
An example of the implementation of the proposed technical solutions, containing all the characteristics specified in the claims, on the basis of Tomsk iron ore, cement and energy raw materials is as follows. High-temperature processing of Bakchar oolitic iron ore in the blend "Kamensky limestone - Bakchar iron ore - overnight coal is carried out in the kiln. When the weight ratio of the main ingredients of the mixture 4:3:1 and the corresponding content of the clinker minerals CaO, SiO2, Al2O3, Fe2O3(% weight.): 52; 6; 0,73; 0,5 - for limestone, 0,6; 22; 4; 44 - ore; 10; 50; 25; 9 - for coal, 1 ton of Portland cement clinker will be 0.6 t Bakchar iron ore concentrate (67% Fe).
The procedure of roasting is a thermal cycle of heating and cooling the mixture in the temperature range 50°C→1450°C→750°C, when activated physicochemical changes in the mix of ingredients. This Radiostantsiya processes are controlled by thermodynamics and kinetics of recovery of iron oxides in the systems Fe-C-O and Fe-H-O.
The recovery environment is provided with the solid carbon in the ash of brown coal; carbon monoxide Gazah combustion; the hydrogen produced by the decomposition of water vapor and methane in the zone of the ignition furnace. The most efficient recovery of ore (up to Fe3O4and Fe) is in the range 650-960°C, when flow solid-phase reaction CaO+SiO2, CaO+Al2O3, CaO+Fe2O3. At a temperature of 1000-1200°C interaction calcium and iron oxides with the formation of silicates, aluminates, and ferrites of calcium in the hot zone of the kiln at a temperature of 1350-1450°C is partially melt the mixture and sintering clinker iron ore cakes. In the cooling zone the temperature class is reduced to a temperature of magnetizing roasting 750-860°C and finally for 3-6 hours initial charge is converted into a spectrum containing clinker minerals alit 3CaO*SiO2, bleaches 2CaO*SiO2, tricalcium aluminate CaO*Al2O3, keturahnalley almaterra CaO*Al2O3*Fe2O3and magnetic oxide of iron, Fe3O4and reduced iron Fe. In the process of recrystallization of iron minerals significant portion of the phosphorus migrates in the composition of the clinker minerals "clinker slag", and the melting of minerals escapes with the exhaust gases. Further changes are crushed, pulverized to a fineness 0,0074 mm and rasmol separated by magnetic separators, for example, type EVM, AWS or PolygraphInter MAGN is coherent cage A.S. No. 774529, clinker and iron ore concentrate. Then the magnetic fraction is cooled to temperatures of 50-90°C and comes in contact vats, which are fed by a mineral acid. The dissolution occurs and the transition in a solution of mineral components of the phosphorus remaining in the iron ore concentrate. After that, the solid fraction is separated from the liquid fraction: obestsvechenny concentrate is fed to a two-stage leaching carried out in spiral classifiers, and a solution of phosphorus is used for the manufacture of phosphate fertilizers (sour plum neutralized first with ground limestone, and then lime milk).
On the core material obtained in the years 2006-2008 by conducting exploration on the Eastern and Western parts of the Bakchar manifestations of oolitic iron ores, in laboratory experiments the effective conditions of the process obesfosforivanie for various natural types of ore. The criteria of efficiency and completeness of the completion of the leaching process correspond to the following modes of obesfosforivanie roasting-magnetic concentrate:
for hidrogeylogos ore, hidrogeylogos ore with chamosite, hydrolytically ore with quartz and mixtures of ores obesfosforivanie is 51% H2SO4with respect to T:W=1:1 and a temperature of 50-60°C for 60 minutes;
for siderite ore with CH is Aconitum and chamosite-hidrogeylogos ore with sideritis cement objectstorage is 43% HNO 3with respect to T:W=1:1 and a temperature of 60-70°C for 45 minutes;
for sand ore with sideritis cement objectstorage is 36% HCl with respect to T:W=1:1 and a temperature of 70-90°C for 30 minutes.
Samples objectstring to the level of 0.12 to 0.29% R concentrate Bakchar oolitic iron ores contain iron in the range of 53-60% Fe (up to a maximum of 67% Fe).
In General, the proposed technical solution to the problem of increasing the efficiency of obtaining objectstring concentrate oolitic iron ores are provided:
- saving heat source when the joint firing, melting and sintering of iron and clay minerals;
- increase yield and quality of the magnetic iron concentrate by conducting the separation in the temperature range of magnetizing roasting and waste part of the phosphorus in the "clinker slag";
- creation of optimal temperature regimes through the use of thermal inertia of the cooled concentrate;
- selection on the basis of experimental data of the concentration of the acid, the ratio of T:W time and leaching;
- use Vasilchenko phosphorus fertilizer.
1. The method of obtaining objectstring concentrate oolitic iron ores, including high temperature processing, cooling, leaching the concentrate with a mineral acid, characterized t is m, that high-temperature processing of iron-containing material is carried out in the range of 1350-1450°C in a reducing environment with the participation of clinker minerals prior to the formation of melt and cakes, which are cooled to a temperature of magnetizing roasting 750-860°C, crushed and divided magnetic separation on clinker and concentrate, which is cooled to a temperature of 50-90°C and served at this temperature on the leaching of mineral acid for dissolution of phosphorus.
2. The method according to claim 1, characterized in that depending on the environment type oolitic iron ore iron ore concentrate is leached with sulfuric acid concentration of 51%, a nitric acid concentration of 43% or hydrochloric acid concentration of 36%.
3. The method according to any one of claims 1 and 2, characterized in that the leaching is carried out with sulfuric acid at a ratio of T:W=1:1 and a temperature of 50-60°C.
4. The method according to any one of claims 1 and 2, characterized in that the leaching is carried out with nitric acid at a ratio of T:W=1:1 and a temperature of 60-70°C.
5. The method according to any one of claims 1 and 2, characterized in that the leaching is carried out with hydrochloric acid at a ratio of T:W=1:1 and a temperature of 70-90°C.