Method to process nepheline ores to produce alumina and soda products
SUBSTANCE: method includes preparation of a nepheline-lime-soda charge, its sintering in a tubular rotary furnace by heat released when burning fossil coal. After sintering, leaching, desiliconisation and carbonisation of an aluminate solution is carried out to produce alumina and soda products. The fossil coal to burn is a brown coal, the solid residue of which contains calcium oxide CaO of at least 30 wt %, and silicon oxide SiO2 of not more than 40 wt %. Brown coal from the Kansko-Achinskiy field is burnt.
EFFECT: reduced consumption of lime in charge preparation and lower content of silicon oxide in an aluminate solution, using a less scarce fossil coal as fuel.
2 cl, 2 tbl, 1 ex
The invention relates to alumina industry, more specifically to the processing of alkaline aluminium-containing raw materials, mainly nepheline and evelinapetrova rocks, ores and concentrates sintering method.
There is a method of processing nepheline ores to obtain alumina and soda derivatives; including preparation of nepheline-lime-soda mixture, sintering in a tubular rotary kiln due to the heat released by the combustion of fuel, the subsequent leaching, obestsenivaya and carbonation aluminate solution with obtaining alumina and soda derivatives;. At the same time to charge set lime-silica ratio of CaO:SiO2= 2,00±0,05 and believe that this relationship will continue in the Speke .
The disadvantage of this method applied to the present time in the production of alumina by the method of sintering, associated with spending large amounts of limestone Pandwho is usually in charge of up to 50% of its weight , which reduces the productivity of the furnace sintering. It was originally set lime-silica ratio of CaO:SiO2called lime module charge Mand SHZat the entrance to the furnace and, consequently, lime module guardianship Mand NWat the exit from the oven.
The closest in technical essence and the achieved result is a method of processing Nefeli the new ores to obtain alumina and soda derivatives;, comprising preparing nepheline-lime-soda mixture, sintering in a tubular rotary kiln due to the heat generated by burning coal, the subsequent leaching, obestsenivaya and carbonation aluminate solution with obtaining alumina and soda derivatives; .
The disadvantage of this method is that the additive will bake the solid residue of combustion of coal reduces the amount of lime module in Speke Mandthat when the batch preparation necessitates additional, against the usual flow of limestone Pand dthat lime increases the modulus of the charge from the specified Mand SHZ=2,00±0,05 before the actual Mand chess Federation.
This reduction in size lime module in Speke due to the fact that in the solid residue burning coal of calcium oxide CaO is contained usually in 2-11 times less than the content of silicon oxide SiO2. While in the solid residue burning coal silicon oxide SiO2contains usually more than 50% (ibid), which increases costs when obestsenivaya obtained by leaching from SPECA aluminate solution, and also leads to increased losses of alumina.
All this, and use as fuel is relatively expensive coal results in high costs of this method.
The problem to which the invention is directed, is to reduce costs. Achieve the same technical result is to reduce the consumption of limestone in the preparation of the charge and the reduction of the content of silicon oxide SiO2in aluminate solution, and also to use as fuel more affordable, consequently, cheaper fossil coal.
This problem is solved and the technical result is achieved in that in the method of processing nepheline ores to obtain alumina and soda derivatives; including preparation of nepheline-lime-soda mixture, sintering in a tubular rotary kiln due to the heat released by the burning of fossil coal, subsequent leaching, obestsenivaya and carbonation aluminate solution with obtaining alumina and soda derivatives; according to the invention as fossil coal combustion using brown coal, the solid residue of combustion which contains calcium oxide CaO not less than 30 wt.%, and silicon oxide SiO2not more than 40 wt.%. When you use burning brown coal Kansk-Achinsk basin.
The difference between the claimed invention from the known  is that as fossil coal combustion using brown coal.
It is the use of combustion of brown coal, the solid residue of sgig the deposits which contain abnormally high, in comparison with the solid residue in the combustion of coal, the amount of calcium oxide and a lower amount of silicon oxide, ensures the achievement of the previously mentioned technical result: reduction of consumption of limestone in the preparation of the charge, reducing the content of silicon oxide aluminate solution and use as fuel cheaper fossil coal.
Below in table 1 are provided in accordance with the data source  the average chemical composition of the solid residue of combustion (for short: ash) brown coal Kansk-Achinsk basin and coal of a number of fields and swimming pools.
|The name of the field and the pool||The chemical composition of the ash on without sulfate mass %|
|The Kansk-Achinsk basin||33,5||12,3||11,1||36,1||of 5.4||0,9||0,7||-|
|Deposits of Central Asia||42,4||21,3||12,4||17,2||3,4||1,5||1,2||0,6|
|Dnieper basin||55,2||of 17.5||7,2||15,3||2,1||0,6||1,0||1,1|
|Field Behold the EPO-Eastern regions||48,9||22,8||12,1||9,9||2,6||1,4||1,5||0,8|
|The Eastern field||51,2||26,4||9,5||7,8||2,4||1,2||0,7||0,8|
|The Lviv-Volyn basin||44,1||22,6||20,5||7,5||1,7||2,1||0,6||0,9|
|Deposits of the Ural||52,4||23,7||13,3||5,6||1,8||1,4||0,7||1,1|
|Deposits of Kazakhstan||56,7||25,7||6,0||5,5||1,5||1,3||2,1||1,2|
|The Far field||56,1||25,2||7,1||of 5.4||1,6||2,5||1,4||0,7|
For example, nepheline ore Kiya-shaltyrskogo field is processed in furnaces sintering OJSC "RUSAL Achinsk" (same: AGK). These truncatewords ovens have an internal diameter of 5 m and a length of 185 meters On the section of the furnace where the combustion temperature reaches 1550-1650°C. as the main fuel you currently use coal from the Kuznetsk basin mark T.
In 2010, in accordance with technical requirements of the RUS-Engineering" LLC "Krasnoyarsk boiler factory produced the first heat calculation furnace sintering, working in the Kuznetsk coal basin, and then heat the calculation of the same sintering furnace, if it works on brown coal from the Kansk-Achinsk basin .
Based on these calculations, the conclusion about the possibility of maintaining the current thermal circuit in the furnace sintering OJSC "RUSAL Achinsk", if it works on the specified lignite fired.
The authors of the present invention is made more approximate calculations necessary to evaluate the impact of processing nepheline ore changes in the ash content of the coal when the translation work sintering furnace with coal for brown coal.
Initial data for the heat of combustion, the solid residue of combustion of coal , chemical composition of solid residues (angry) , the results of the calculations referred to 1000 kg combustion of brown coal, and other indicators are summarized in table 2.
|The lower heat of combustion, kJ/kg||25120||15660|
|Fuel consumption, kg||623,41||1000|
|The amount of ash, %||14,6||7,0|
|The amount of ash, kg||91,02||70,00|
|The content of CaO in the ash, %||7,3||36,1|
|The content of CaO in the ash, kg||6,64||25,27|
|The content in the ash SiO2, %||55,8||33,5|
|The content in the ash SiO2kg||50,79||23,45|
|The content in the ash K2O %||1,8||0,9|
|The content in the ash Na2O %||0,9||0,7|
|The content in the ash Fe2O3, %||6,8||11,1|
|The content in the ash Al2About3, %||24,9||12,3|
|The content in limestone CaO, %||54,0||54,0|
|The specific content in the mixture of limestone [2, 2.4]||0,418||-|
|The relative size of the SPECA from the mixture, % [2, table]||54,0||-|
|Performance furnace will bake [5, str], t/h||101-103||-|
|Hourly fuel consumption, t/h [4, p.71]||-||36,083|
|Molar ratio in the ashes|
In table 2, the data allow us to establish the following:
1. The combustion of one tonne of brown coal on the furnace ASC will provide a decrease in the charge of calcium oxide against the existing on 18,63 kg and, respectively, a decrease of limestone in the preparation of the charge 34.5 kg This allows you to increase the volume of the charge of new versus existing structure on the same 34,5 kg, the production of SPECA on 18,63 kg and alumina on 18,63 kg: 8,0 = 2,33 kg [5, p. 359].
Per hour sintering furnace burns brown coal 36,083 t (see table 2), which provides a reduction of limestone in the preparation of the charge on 1244,86 kg. This allows you to increase the amount of charge on the same 1244,86 kg, the production of SPECA on 672,23 kg and alumina on 83,07 kg
2. On AGK average productivity furnace will bake, running on coal, equal 102000 kg/h [5, str-138]. When operating such a furnace lignite fired her performance will bake to increase by 672,23:102000×100=0,66%.
3. The combustion of one tonne of brown coal on the furnace ASC will provide a reduction in the content of silicon oxide SiO2against the existing in Speke on 50,79 kg - 23,45 kg = 27,34 kg. Per hour of operation of the furnace will burn 36,083 tons of brown coal, the content of silicon oxide in Speke will decrease n the 27,34×36,083=986,51 kg
This reduction of silicon oxide in Speke reduce costs obestsenivaya obtained by leaching from SPECA aluminate solution and reduce the loss of alumina as when obestsenivaya solution, and during its decomposition by carbonization and decomposition. Simultaneously are shown in table 2 molar ratio in the solid combustion residues (ash) indicate that replacement furnaces sintering of coal for brown coal does not lead to significant negative consequences in the production of associated soda derivatives;.
Example. Nepheline ore processing for obtaining alumina and soda derivatives; produced by sintering furnaces OJSC "RUSAL Achinsk", which for a long period of time as the primary fuel used coal from the Kuznetsk basin. This is achieved in furnaces sintering temperature is recognized as optimal , and lime module SPECA Mand NWadopted unchanged. Thermal calculations , performed by well-known methods showed the possibility to save the current thermal circuit in furnaces sintering in the case of their work on brown coal from the Kansk-Achinsk basin.
Implementation of the proposed method on these furnaces sintering can be done after their reconstruction and consists, primarily, in the adjustment of the composition of the charge to reflect changes in the composition of the perches and will bake solid residues from the burning of fossil coal and structural and technological changes in the preparation of the coal for combustion and flow into the furnace sintering. If necessary can be modified in the existing process flow processes, including leaching, obestsenivaya and carbonation aluminate solution.
Implementation of the proposed method produced the following.
On the basis of existing in Speke lime-kremnievoi relationship CaO: SiO2i.e. lime module SPECA Mand NWthe amount and composition of the solid residue of combustion of brown coal, characterized by a content of calcium oxide CaO 36.1% and SiO233,6%, by well-known methods, for example , calculate the value of reduction of limestone in the preparation of the charge. According to the approximate calculation of the applicant per hour sintering furnace lignite coal consumption of limestone in the preparation of the charge can be reduced by 1244,86 kg, which can be considered as the increase of the charge of new versus existing, the composition also 1244,86 kg. This will increase the production of SPECA on 672,23 kg and alumina on 83,07 kg
Such relatively high, reducing the consumption of limestone virtually no effect on existing equipment, ensuring the preparation of nepheline-lime-soda mixture (crushing ore and limestone, separate grinding and dosing) and submission watered charge by filling in the low-temperature part of the furnace.
Significant, approximately ,6 times (25120 kJ/kg:15660 kJ/kg), the increase in coal combustion necessitates a substantial increase in the productivity of existing equipment, ensuring the reception of coal (bunker), grinding coal mill, coal injection air through the pulverized coal burners, as well as an increase in the geometry of the burners and their number.
Because the amount charged metal at the top (caudal) part of the preheated oven, the proposed method remains unchanged, so if the movement of the charge towards the gases resulting from the combustion of coal in the head part of the furnace processes occur without changes. While processed foods in the form of SPECA, formed due to the heat emitted during the combustion of brown coal, proceed in the refrigerator and the gaseous products of combustion of coal together with the process gases are directed into the gas purification system.
The cooled sintered crushed and sent for leaching. Resulting aluminate solution in accordance with the technological scheme of production is directed to obestsenivaya and carbonization and subsequent receipt of alumina and soda derivatives; types of soda and potash. As in Speke, and in the aluminate solution reduced the content of silicon oxide SiO2that simplified obestsenivaya and reduced it costs and losses at the time of receipt of alumina, and with whom coproductive.
When the reconstruction of the refinery furnaces sintering, it is advisable to solve a number of additional tasks that are not provided by the claimed invention, for example, to organize a closed scheme drying with direct fuel injection .
A more complete economic efficiency of the proposed method of processing nepheline ores of different composition, including evelinapetrova raw materials, applied specific sintering furnace can be determined during the development of the project with regard to all the processing undertaken by integrated processing of aluminium-containing raw materials and taking into account the prices of fossil fuels.
Sources of information
1. Liner A.I., Eremin NI, Liner Y.A., Pevzner I.Z. alumina Production. - M.: metallurgy, 1978. P.184-193.
2. Abramov VA, A.I. Alekseev, Badalian HA Complex processing evelinapetrova raw materials. - M.: metallurgy, 1990. P.36-46).
3. Recommendations for designing gears of thermal power stations: P 26-85. / VNIIG, L., 1986. P.74-76.
4. Justification the possibility of organizing a specified temperature in sintering furnaces OJSC "RUSAL Achinsk" using brown coal Kansk-Achinsk basin. Mikhailenko S.A., Masalsky G.B., Kapustin p. g and other OOO Krasnoyarsk boiler factory, 2010.
5. Complex processing of aluminium-containing alkaline materials. Arluk B. I., Liner Y.A pivnev A.I. - M.: metallurgy, 1994.
6. The technique of sintering of the charge alumina industry. Khodorov H., Shmargunenko NS - M: metallurgy, 1978.
7. The patent of Russian Federation №2259945, CL C01F 7/38, publ. 10.07.2005.
1. A method of processing nepheline ores to obtain alumina and soda derivatives; including preparation of nepheline-lime-soda mixture, sintering in a tubular rotary kiln due to the heat released by the burning of fossil coal, subsequent leaching, obestsenivaya and carbonation aluminate solution with the subsequent receipt of alumina and soda derivatives;, characterized in that as fossil coal combustion using brown coal, the solid residue which contains calcium oxide CaO not less than 30 wt.%, and silicon oxide SiO2- not more than 40 wt.%.
2. The method according to claim 1, characterized in that use lignite Kansk-Achinsk basin.
SUBSTANCE: method of sulphide stock containing noble metals comprises mixing stock with water solution of reagents and autoclave oxidising treatment by water solution of reagents on feeding oxygen and adding component with halogenide-ion to produce pulp. Then, pulp is divided into solution and solid residue. Note here that autoclave oxidising treatment is carried out by water solution containing component with halogenide-ion at 160-250°C and oxygen partial pressure of 0.5-5.0 MPa. Extraction of noble metals is carried out by leaching from solid residue by sulfite-sulfate solutions.
EFFECT: reduced number of processes, lower costs.
11 cl, 3 tbl, 1 ex
SUBSTANCE: proposed method consists in valuable metals are decomposed in salt melt containing 60-95 wt % of NaOH and 5-40 wt % of Na2SO4. Then, melt decomposition product is converted into solid phase by cooling to room temperature. After cooling, minced melt decomposition product is converted in water at temperature lower than 80°C to produce water suspension and water fraction is separated by filtration for components to be extracted therefrom.
EFFECT: higher efficiency of extraction.
22 cl, 1 dwg, 3 tbl
SUBSTANCE: manganese dioxide obtaining method involves dilution of manganese-containing raw material in nitric acid so that solution of manganese nitrates and nitrates of calcium, potassium, magnesium and sodium impurities contained in the ore is obtained. Then, thermal decomposition of nitrates in autoclave is performed. Thermal decomposition is performed at constant pressure drop in autoclave, starting from pressure of 0.6 MPa and reducing it to the end of the process to 0.15 MPa. At that, pulp is constantly mixed at thermal decomposition with the mixer rotating at speed of 1-15 rpm and with superimposition of vibration on it with frequency of 20-50 Hz. Method can be implemented at chemical plants provided with pressure autoclaves.
EFFECT: obtaining manganese dioxide of improved quality.
2 tbl, 2 ex
SUBSTANCE: invention relates to a method for treatment of low-grade oxidized zinc ores and concentrates with zinc, manganese, iron, lead, silver, calcium and silicon dioxide recovery. The method comprises crushing, fine crushing, lixiviating, settling-down of the above components from solutions, wherein the lixiviating shall be performed in stages: during the first and the second stage - lixiviation by sulphuric acid solution over the reducing substance, the oxidation-reduction potential φ (ORP): at the first stage φ=380-420 mV, at the second stage φ=420-460 mV. At the third stage lixiviation is performed by an ammonium carbonate solution with the composition (g/dm3): 60-110 NH3 general 30-65 C02 general while at the fourth stage it is performed by nitric acid NHO3. At the fifth stage sulphating roasting with H2SO4 term with further water leaching is performed, the sixth stage being lixiviation with ammonium fluoride aqueous solution of acid NH4HF2. The obtained soutions shall be puriied and used for zinc, manganese, iron, lead, silver, calcium, silicon dioxide and sodium sulfate, ammonium nitrate recovery. EFFECT: enhanced zinc recovery and rational utilization of the stock.
16 cl, 1 dwg, 3 ex
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
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
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
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
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++CO3 2-=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
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: process engineering.
SUBSTANCE: invention relates to method and device for adding powder to fluid metal. Method of mixing powder with fluid metal comprises adding powder to fluid metal in its mixing. Fused metal in source 14 under reduced pressure in crucible 12 wherein fused metal is displaced flows from source 14 upward via bypass tube 6. Powder is dispensed from container 1 and displaced by gas. Mix of powder and gas are added to fused metal in bypass tube 6 for mixing therein and feeding into crucible 12. Mixing device has source 14 to feed fused metal and powder container 1. Source 14 is communicated via bypass tube with container arranged above and kept at reduced pressure. Carrier gas feed control unit 4 communicated with mixing chamber 3 nearby outlet of powder container 1. Mixing chamber 3 is communicated with bypass tube 6 to feed powder into fused metal in bypass tube.
EFFECT: better mixing.
10 cl, 1 dwg, 1 ex
FIELD: metal industry.
SUBSTANCE: invention relates to a manufacturing process for a remelt block containing aluminum designed for making aluminum alloy for the aircraft industry in which scrap containing mainly aluminum alloys 2XXX or series 7XXX series used in the aircraft industry is supplied during a supply stage, the scrap is melted in a smelting furnace in order to obtain an initial molten metal bath during a smelting stage, the initial molten metal bath is subjected to purification by crystallization in order to obtain a solidified mass and a bath of residual liquid, and the solidified mass is recovered in order to obtain a remelt block during a recovery stage. All the metal is initially charged and then subjected to fractional crystallization; the crystallization speed given as the mass of formed crystals, expressed as a percentage of the weight initially charged, per hour of crystallization, being between about 3.8%/h and about 6.2%/h. Another subject of the invention is a manufacturing process for a semi-finished product and an alloy for the aircraft industry, typically an alloy of series 2XXX or series 7XXX is produced; this alloy is cast in the shape of a semi-finished product.
EFFECT: purification urify scrap of series 2XXX or series 7XXX alloys for iron and silicon, without eliminating additive elements such as zinc, copper and magnesium.
25 cl, 3 dwg, 1 ex, 2 tbl
SUBSTANCE: method involves melting of rejects in the furnace in inert atmosphere in presence of sodium tetraborate and boric anhydride at melting temperature or higher than melting temperature of aluminium; at that, at the beginning of the process the sodium borate is loaded to the furnace on the basis of 10-15% of the aluminium rejects mass expected to be loaded, boric acid the weight of which is calculated by the formula: m"нзвоз" = 0.0246 · mreject · X (1), where m"нзвоз" - weight of boric acid, which is loaded to the furnace, kg; mreject - weight of aluminium rejects loaded to the furnace, kg; X - content of aluminium oxide in aluminium reject, wt %; then, aluminium reject is loaded to the furnace on the basis that molten aluminium shall achieve the height of 800-1000 mm and exposed in the furnace during 45 minutes at temperature of 880-900°C. After exposure of molten aluminium in the furnace the temperature is decreased to 680-700°C and at this temperature the molten aluminium is drained to casting forms, first through the top taphole located at the height of 100 mm from the furnace melting pot bottom, then through lower taphole located on the level of the furnace melting pot bottom. Furnace has gas dead-end burners arranged in the chambers interconnected with the furnace melting pot by means of openings in the melting pot brickwork, and two tapholes.
EFFECT: invention allows obtaining high-quality aluminium from aluminium rejects, and reducing capital and operating costs.
4 cl, 1 dwg, 1 tbl
SUBSTANCE: procedure 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.
EFFECT: raised efficiency of extraction of aluminium and iron from ash-and-slag material, reduced expenditures for reagent treatment of material.
1 dwg, 2 tbl
FIELD: machine building.
SUBSTANCE: procedure consists in stages of supply of certain amount of composite material containing polymer and aluminium in first reactor, in heating composite material in non-oxidising medium at temperature sufficient for polymer volatilisation and production of hydrocarbon side product and aluminium in first reactor, in supply of aluminium free form one polymer into second reactor and in heating aluminium in non-oxidising medium at temperature sufficient for aluminium melting in second reactor. The installation consists of not less, than two reactors, one of which is equipped with an external heating element set around a cavity for mixing wherein there are arranged at least two screws each including a shaft and at least two internal heating elements positioned on it. The second reactor is equipped with a system of plasma heating located near a melting bath covered with material possessing fire-proof properties. The reactor has a case set around the cavity for mixing composite material, the plasma heating system arranged on the case and connected with the cavity, an inlet orifice for reception of certain amount of aluminium, free of polymer, an outlet orifice for discharge of melted aluminium communicated with the cavity, and heat insulating material applied in the said case at amount sufficient for maintenance of working temperature in the melting bath.
EFFECT: processing composite materials including paper-plastic, aluminium and materials consisting of thin-sheet plastic-aluminium used for manufacture of packages for food products and industrial products with facilitation of re-use.
61 cl, 7 dwg
SUBSTANCE: procedure consists in charging aluminium in stand into melt of salts of sodium and potassium chlorides, sodium fluoride, tetra-boric-acidic sodium, and boric acid anhydride at temperature 700-800°C and of composition, wt %: NaCl - 64, NF - 20, KCl - 11, Na2B4O7 - 3, B2O3 - 2. The furnace contains a crucible made as a shell out of refractory steel, a shell, a refractory lining of the crucible, burner devices, a cover of the furnace, tubes for refined melt process pouring and for pouring aluminium melt and salts during furnace repair or in case of emergency. A low end of the tube for refined aluminium melt process pouring is built-in into the crucible of the furnace at distance of 50-80 mm from the bottom of the furnace, while the level of melt of refined aluminium is at height of 860-900 mm from the bottom of the furnace.
EFFECT: raised efficiency of refinement of aluminium containing impurities as metal oxides or inter-metallic compounds and elimination of scull formation.
7 cl, 1 dwg, 1 tbl
SUBSTANCE: metal and slag are produced and carbon is extracted in one-furnace one-chamber reactor. Fume of Al2O and Al created at stages of slag and metal production are recovered in a reactor for fume recovery and processed with carbonic material producing a re-circulated material containing Al4C3. Re-circulated material is used for assistance in one or several stages of slag production.
EFFECT: raised efficiency of carbonic-thermal production of aluminium in one reactor, reduced exhausts into environment.
9 cl, 2 dwg
SUBSTANCE: according to the method there prepared is molten aluminium and heated above liquidus temperature. Molten metal is pored to the mould heated to the same temperature and filled with granules of water-soluble salts. At that, there used are salts which do not chemically interact with molten aluminium, with fusion temperature which is higher than heating temperature of molten metal and mould and with density which is higher than molten aluminium. After hardening the ingot is removed from the mould and placed in water.
EFFECT: enlarging the range of items made from foam aluminium, increasing quality of foam aluminium, reducing production cost of foam aluminium.
2 cl, 1 ex
SUBSTANCE: procedure for refining aluminium alloys consists in treating melt at temperature 750-760°C with briquette flux containing organic or non-organic binding, chlorides, fluorides and refractory fillers in form of dispersed particles of high melting aluminium and silicon oxides. When organic binding is used, flux has the following chemical composition, wt %: KCl 2.0-10.0; NaCl 2.0-10.0; organic binding 2.0-3.0; SiO2 or Al2O3·2SiO2 - the rest. 20-30 % water solution of salt constituent of flux is used as non-organic binding.
EFFECT: increased refining property and efficiency of process.
2 cl, 1 tbl, 7 ex
SUBSTANCE: facility consists of working chamber installed in case; also working chamber is formed with walls and bottom made out of refractory material and has inlet and outlet openings. The bottom of the working chamber is made step-like in the direction of the outlet opening. A vertical partition not reaching the bottom and a filter element are installed inside the working chamber; also the filter element is secured inside the working chamber between its walls and the vertical partition. A flap cover with heating elements and electro-mechanical drive is arranged in an upper part of the working chamber. The filter element is made as successively arranged porous filter partitions with dimension of pores at the first partition relative to the second one equal to 2/1-2/1.5. The filter partition installed at the inlet opening is arranged with a rise of 3-5 degrees in the direction of metal flow to the side of the outlet opening, while the filtering partition at the outlet opening is installed horizontally. Not less, than one opening is made in the cover; industrial drying fans are arranged over the opening, while the case is mounted on the bed with a tilt.
EFFECT: upgraded degree of metal purification, reduced labour cost for maintenance and expanded process functionality of facility.
SUBSTANCE: agglomerate contains pentaoxide of vanadium 0.2-2.0 %, oxide of calcium 0.1-1.2 %, dioxide of silicon 2.0-10.0 %, aluminium oxide 1.5-4.0 %, magnesium oxide 0.8-1.5 %, dioxide of titanium 0.2-2.0 % and iton oxides - the rest.
EFFECT: increased degree of transition of vanadium into slag.
2 tbl, 2 ex