METHOD FOR PRODUCING A REDUCING AGENT FOR THE PRODUCING OF TECHNICAL SILICON

Description

[0001] The invention relates to the field of metallurgy, in particular, to techniques for producing reducing agents for manufacturing superpurity industrial silicon.

[0002] A method of silicon manufacturing is known that includes dosing, mixing, loading, and melting a fusion mixture comprising quartzite and charcoal, in an electric furnace (Ragulina R. I., Yemlin B. N. Elektrotermiya Kremniya i Silumina (Electrothermy of Silicon and Silumin). Moscow: Metallurgiya, 1972, p. 240). However, this manufacturing method involves the consumption of charcoal, an extremely scarce and expensive raw material. Furthermore, this method entails exceptionally high losses of a reducing agent due to the very low strength of charcoal, which heavily crushes and grinds when introduced into the fusion mixture, and especially when the fusion mixture is reloaded.

[0003] A method of silicon manufacturing is known that includes dosing, mixing, loading, and melting a fusion mixture comprising quartzite and Columbian coals with very low iron and ash content, in an electric furnace (http: / / www.up-pro.ru / library / production_management / systems / kremnij-kruchkov.html). The drawback of this method is the high cost of Columbian coals due to transportation expenses.

[0004] A method of producing a briquetted mix for silicon manufacturing is known (patent RU 2528666, C01B33 / 025, Publ. 05.27.2014), which includes mixing a silica-containing raw material and a carbonaceous material of plant origin (sawdust, wood waste, etc.) and briquetting them to produce briquettes, which are subjected to thermal pyrolysis in the absence of oxygen until the pyrolysis gas is completely released. The drawbacks of this method are low strength, low bound carbon content, and high cost of briquette production.

[0005] A method of producing carbonizate (Rexyl) (patent KZ 23615, C10B57 / 00, C10B55 / 00, Publ. 12.15.2010) from non-caking bituminous coals is known, in which the coals are subjected to high temperature heat treatment in an inert atmosphere in the absence of air. The drawback of this method is the need to select raw materials for carbonizate production, more specifically, low-ash bituminous coals with a low content of detrimental impurities that all end up in the carbonizate after the heat treatment.

[0006] A method of producing a fusion mixture for melting pure silicon is known (patent RU 2424341, C22C33 / 04, C01B33 / 025, Publ. 07.20.2011), wherein amorphous silicon dioxide is mixed with a carbon-containing reducing agent in the form of carbon black at a ratio of 1:1.5 and silica gel, followed by the fabrication of pellets or briquettes of various shapes that are dried and calcined at 900-1,200°C. The drawbacks of this method of fusion mixture production include the high cost of carbon black and an increased yield of volatile silicon monoxide SiO.

[0007] A method of briquetting semi-coke, primarily lignite, is known (patent RU 2376342, C10L5 / 12, Publ. 12.20.2009), comprising the following stages of preparing starting components: crushing semi-coke down to 0-7 mm, mixing semi-coke with hydrated lime with a water-to-lime ratio of 3:1 or 5:1, compressing, impregnating the briquettes with liquid glass, and drying.

[0008] The drawback of this method is a high ash and undesirable impurity content, in particular, iron content, which limits the application of the briquetted reducing agents in manufacturing premium grades of industrial silicon.

[0009] A method is known that includes heat treatment of a coal bed in a vertical shaft unit with firing at the side opposite the air supply. A coal fraction of 20-70 mm is used as a raw material, and air is supplied through the coal bed at a specific flow rate of 70-99.5 m 3< / (m 2< ·h) depending on the coal grade. The method provides a solid product with higher strength, lower ash, as well as larger mean piece size, with a simultaneous increase in product yield (patent RU 2275407, C10B49 / 02, C10B53 / 00, Publ. 04.27.2006).

[0010] The drawback of the known technical solution is the presence of a mineral part in large pieces of the heat treated coal, contaminating the final product and limiting its application in silicon manufacturing.

[0011] A method of producing semi-coke is known, which includes the stages of heating, drying, and carbonizing solid carbon-containing feedstock with air blasting supplemented with a flammable gas having the temperature of exit from the unit and at a concentration not exceeding the lower flammability limit of the gas. The amount of supplemented gas is preferably 8-10% of the volume of the produced flammable gas. The carbonization temperature is 920-950°C. The technical result is improved semi-coke quality due to a reduced yield of volatiles in the product, increased semi-coke yield by about 5-6%, and shortened treatment duration (patent RU 2169166, C10B49 / 04, Publ. 06.20.2001).

[0012] The drawback of the analog is the presence of iron compounds in the mineral part, which deteriorates the quality of the produced industrial silicon.

[0013] The closest method in terms of technical essence is a method of processing coal crushed down to 10 mm, which is implemented by simultaneous thermal oxidative coal treatment at a temperature of 700-950°C due to partial coal oxidation with air and separation of the mineral part of the coal that is heavier than the coal. The blasting air for bed fluidization is supplied at a rate of 2,500-4,200 m 3< / (m 2< ·h). Fine carbon, vapor gases from coal thermal decomposition, and coke gasification products partially burn in the fluidized bed, maintaining its working temperature. The heavier rock particles settle down in the lower part of the fluidized bed and are removed from the unit via a sifting grate. The combustion products are fed to the waste-heat boiler to generate thermal energy. The invention provides high-energy, low-ash, heat treated solid fuel from high-ash coals without preliminary upgrading of starting coal (patent RU2401295, C10B49 / 10, Publ. 10.10.2010).

[0014] The drawback of the prototype is the insufficient coal separation from rock particles and high iron content, which limits the application of the briquetted reducing agents in manufacturing premium grades of industrial silicon.

[0015] RU 2364737 C1 discloses a method of ecologically clean complex use of solid fuels (mainly low-grade high-reactive coals) integrated into the thermal cycle of the combined-cycle power plant, including steam-gas power plant (PTU). crushing and drying of coal, oxidizing gasification to produce a low calorific generating gas, purification of the gas from solid particles and sulfur compounds and the use of purified gas as a gas-steam power plant fuel. A part of the air after the high-pressure compressor of the PTU is used for a three- countercurrent process of thermochemical processing of coal, in which in the first stage the dried and ground primary coal was subjected to pyrolysis due to the heat of the gasification products coming from the second stage, to form pyrolysis products in the form of vapor from coal tar and pyrogas, which are withdrawn from the first stage together with gasification products, and semi-coke, which is sent for processing to the second stage by oxidative gasification with a mixture of air and combustion products.

[0016] US 6162265 A discloses a process for preparing an irreversibly dried coal wherein a first fluidized bed reactor with a bed whose density is about 30-50 pounds per cubic foot (480-801 kg / m 3< ) and whose temperature is about 480-600°F (249-316°C) is contacted with a coal with a moisture content of from about 15-30%. liquid phase water, inert gas, and air. The comminuted and dewatered coal produced in the first fluidized bed reactor is then passed to a second fluidized bed with a density of about 30-50 pounds per cubic foot (480-801 kg / m 3< ) and a temperature of about 215-250°F (102-121°C), to which water, inert gas, and about 0.5-3.0 weight percent of mineral oil with an initial boiling point of at least about 900°F (482°C) is also fed, the temperature of the comminuted and dewatered coal is reduced to the temperature of from 215-250°F (102-121°C) in less than about 120 seconds.

[0017] US 4052170 A discloses a process for removing pyrite particles form coal by pulverizing and fluidizing a coal in the presence of (a) heated air, followed by removing pyrite particles with a high-gradient magnetic separator; or (b) a hot, inert gas form which condensables are separated, followed by countercurrently further heating the coal in a succession of fluidized stages with hot oxygen-containing gas to a temperature at which the pyrite particles are sufficiently converted to pyrrhotite, magnetite, and gamma-hematite, and removing the pyrite minerals by magnetic separation means.

[0018] US 2595365 A discloses a continuous process for process of carbonizing carbonizable solids which comprises forming a deep single substantially continuous downwardly moving bed of finely divided carbonized solid fuel in an upright carbonizer, continuously feeding the carbonizable solid to the upper part of said bed, maintaining said bed in a fluidized condition by passing upwardly therethrough a stream of gas comprising, near the lower part of said bed, steam introduced at that point and, at a higher level in said bed steam, combustion supporting gas and gaseous combustion residues, causing said bed in its downward travel to pass through the interstices of large size bodies maintained as a pack in two separate zones in the path of said bed, recovering from above said bed vaporous products of the carbonization of said carbonizable solid and recovering carbonized solid from the lower portion of said bed below the point of introduction of steam into said bed. The flow of materials and the feed of steam and combustion supporting gases are so regulated that throughout the upper portion of the bed above the upper packed zone, the finely divided material is maintained at a carbonization temperature above the plastic range of said carbonizable solid and between 900-1400°F (482-760°C), in the next lower zone including the upper packed zone, the finely divided material is maintained at a temperature between about 1600-2000°F (871-1093°C), and in the lowermost zone, including the lower packed zone, said material is quenched with steam.

[0019] RU 2518624 C2 discloses a device and method for thermal coal preparation using coal with a moisture content from zero to the natural particle size of up to 40 mm. The device consists of two communicating chambers. The first chamber consists of coal feeder, fire grate to remove separated ore, device to feed blow air at the temperature not over 400°C and to add flue gas to 100%, waste gas removal system and coal layer transfer pipe. The second chamber consists of the device of initial blowing at the temperature not higher than 400°C, device of secondary blowing to afterburning of combustible components for coal thermal decomposition and coke gasification at 600-1000°C, heat energy recovery system, flue gas removal system, and coke discharge pipe.

[0020] The objective of the provided technical solution is to create a method of producing a reducing agent for silicon manufacturing, capable of substituting scarce and expensive reducing agents utilized in manufacturing high quality silicon.

[0021] The technical result of the invention is lower iron content in the reducing agent for manufacturing high quality industrial silicon.

[0022] The invention relates to a method of processing lignite coal with an iron content in the ash of no more than 5% to produce a reducing agent for manufacturing industrial silicon, which includes heat treating said lignite coal in a fluidized bed at a temperature of 700-850°C by blasting at high speeds with a mixture of air and water vapor to provide for the transition of iron-containing compounds in the lignite coal to a magnetic form; cooling the resulting reducing agent; and then magnetically separating same over the course of 100-120 hours, immediately after the cooling stage, at a magnetic field induction of at least 1.1 T.

[0023] The lower the content of the mineral part in the starting coals and its iron concentration, the more likely the product is to have a low iron content.

[0024] The starting lignite coal contains iron primarily in the form of pyrite, marcasite, siderite, and hematite. In light fractions, iron is represented by hydroxides within clay minerals. When processing lignite coals into semi-coke, said mineral compounds pass into the final material and undergo phase transitions, depending on the conditions of the occurring redox processes at high temperatures.

[0025] Thus, pyrite (marcasite) FeS 2 -iron disulfide, present in the starting coal, decomposes upon heating into iron sulfide and sulfur. The following reactions occur upon heating iron sulfide in oxygen:         4FeS + 7O 2 = 2Fe 2 O 3 + 4SO 2      (1)         3Fe 2 O 3 + H 2 = 2Fe 3 O4 + H 2 O     (2)         Fe 2 O 3 + 4H 2 = 3Fe + 4H 2 O     (3)

[0026] Siderite (spathic iron ore) contains iron primarily in the form of carbonate (FeCO 3 ). Under high temperatures, the carbon dioxide being eliminated renders the material porous, while easing its reduction.

[0027] Hematite and magnetite (Fe 2 O 3 , Fe 3 O 4 ). The reduction of hematite and magnetite upon heating with carbon produces fine-crystalline iron oxide that readily transforms into Fe. The zone of transition from FeO to Fe practically merges with the Fe 3 O 4 -FeO zone. It has been found that the reaction rates of Fe 2 O 3 -Fe 3 O 4 and Fe 3 O 4 -FeO at 700-750°C are rather close.

[0028] The process of reduction of iron oxides:         3Fe 2 O 3 + CO = 2Fe 3 O 4 + CO 2      (4)         Fe 3 O 4 + CO = 3FeO + CO 2      (5)         FeO + CO = Fe + CO 2      (6)         FeO + C = Fe + CO     (7)

[0029] The process of iron reduction from oxides proceeds step-wise by sequential transition, from higher to lower oxides, according to the following scheme: Fe 2 O 3 -Fe 3 O 4 -FeO-Fe (above 570°C) or Fe 2 O 3 -Fe 3 O 4 -Fe (below 570°C). Upon low-temperature reduction of hematite (<800°C), magnetite, as an intermediate oxide stage, has a noticeably different composition than stoichiometric. An analysis of the reduction products has demonstrated that there is an entire set of magnetites with varying stoichiometry. The appearance of nonstoichiometric magnetite at low temperatures and its absence at high temperatures of hematite reduction confirm the presence of the limiting influence of solid-phase processes in reduction products.

[0030] The reduction rate depends on the nature of the oxide and the nature and properties of the reducing agent, which can be, for example, lignite coal and its derivatives (semi-coke). Thus, an avalanche increase in the reduction rate is observed when good contact of oxides with semi-coke carbon is ensured. Therefore, when using semi-coke formed in the process of lignite coal carbonization, the efficiency of the process, as for any solid-phase reaction, will depend on the contact between the semi-coke and the oxide being reduced, which is locked with carbon. The reduction process is also affected by the reactivity of lignite coal semi-coke and its content of volatile components. Any lignite coal may be used to produce the reducing agent. However, the most promising one is lignite coal from the Kansk-Achinsk basin due to the large reserves (the predicted resources being 309.9 billion tons, or 23.4% of Russian coal resources), low ash (3.4-22.3%) and insignificant iron content.

[0031] It is known that magnetic separation is most efficient for materials containing iron impurities in the form of magnetite Fe 3 O 4 , which has strong magnetic properties. In the provided technical solution, the reactions of reducing iron oxides to magnetite (and / or any other magnetic form of the processed lignite coal) proceed upon heating the lignite coal in a fluidized bed at 700-850°C to form the reducing agent (semi-coke), which has, in aggregate, the following properties (composition, wt.%): • Ash (A d< ):5.0-8.0%;• Fe 2 O 3 content in ash:0.8-1.2%;• Volatiles (V daf< ):13.0-15.5%;• Bound carbon (C):75.0-80.0%;• Reactivity:at least 8.1 cm 3< / (g·s);• Specific electrical resistivity:at least 1.37×103 Ohm·cm;• Specific area:120-500 m 2< / g.

[0032] The method is implemented as follows. Lignite coal having a size of up to 10 mm is supplied with a screw to a gas distributor plate. The coal is subjected to heat treatment (semi-coking) in a fluidized bed at a temperature of 700-850°C. Coal fluidization is achieved using a mixture of air and water vapor supplied under the gas distributor plate. The water vapor supply under the plate prevents its clinkering in case of thermal abuse.

[0033] The particles of the starting coal supplied to the lower part of the fluidized bed experience high-speed heating, releasing water and resin vapors, as well as decomposition gases in the process. Each coal particle is surrounded by a cloud of protective atmosphere, blocking air oxygen access to its surface. Combustion of the evolving gases and vapors occurs at the periphery of the gas cloud. Thus, in the lower part of the fluidized bed, the surface of coal particles is not subjected to ashing by air oxygen, which ensures the required content level of the reducing carbon (yield).

[0034] High-speed heating is accompanied by intense grinding of coal particles as a result of their thermal destruction and crushing in collisions. It also ensures good contact of iron oxides with carbon, providing high rates of their reduction and transition of iron compounds in the lignite coal to magnetic forms.

[0035] Particle grinding is accompanied by a decrease in their apparent density due to the release of water and resin vapors from the particle pores. Therefore, the finer and lighter particles of the formed semi-coke move to the upper part of the fluidized bed, where the semi-coking continues, accompanied by the release of decomposition gases and resin vapors, but not as vigorously as in the lower part of the fluidized bed.

[0036] While in the lower part of the fluidized bed, the coal particles are in a vapor air medium with substantial oxygen content, and the gas medium in the upper part consists of combustion products with the admixture of semi-coking gas. The oxygen content in this medium is not high, and thus no ashing of the surface of the forming semi-coke particles occurs.

[0037] In the upper part of the fluidized bed, water vapors induce semi-coke activation, increasing the semi-coke surface and enhancing its reactivity in chemical reactions.

[0038] Along with the coal, the rock and locked coal settle in the lower part of the fluidized bed, where due to their higher density, they are removed from the fluidized bed onto the gas distribution plate and are periodically unloaded from it.

[0039] The low-energy gas exiting the fluidized bed is passed to the separation space of the unit. Large semi-coke particles carried from the bed settle back into the fluidized bed, while the gas exits the unit to be stripped from semi-coke fines in a cyclone. The semi-coke fines are added to the semi-coke unloaded from the unit, and the forming low-energy gas is burned in the furnace of the waste-heat boiler.

[0040] The subsequent magnetic separation in the separator lowers the iron content to acceptable levels, ensuring high quality of the reducing agent.

[0041] Example 1. The reducing agent was produced using lignite coal of the Berezovskoe deposit supplied to the fluidized bed boiler. The material was processed in different temperature intervals: 550-700, 700-850, and above 850°C. At temperatures of 550-700°C, the produced reducing agent (semi-coke) had insufficient pyrolysis, high content of volatiles, and low magnetic susceptibility.

[0042] At temperatures above 850°C, the yield was reduced. Therefore, the 700-850°C temperature range is optimal.

[0043] Experiments have demonstrated that prolonged storage of the pyrolyzed lignite coal semi-coke resulted in lower efficiency of subsequent separation of the iron-containing magnetic fraction from the lignite coal semi-coke.

[0044] Example 2. The maximum decrease of the iron content in the carbon material (down to 0.11 wt.%) after passing it through a magnetic separator was observed immediately after the pyrolysis. After 5 days, the iron separation efficiency dropped to 0.15 wt.%. When separating the pyrolyzed product with a storage time of less than 100 hours, the efficiency of iron separation was less than 0.11 wt.%.

[0045] The efficiency of iron extraction depended on the magnetic field induction magnitude. There is an optimum level of magnetic field induction magnitude, below which the efficiency of separating the magnetic fractions decreases. Excessively high magnetic field induction is economically impractical since the equipment cost rises. Low magnetic field induction magnitude results in increased iron content in the magnetically treated reducing agent.

[0046] Example 3. The produced reducing agent was separated in a magnetic field. For magnetic field induction magnitude higher than 1.1 T, the iron content in the magnetically treated semi-coke reached 0.11 wt.%. At a lower magnetic field induction magnitude (0.8 T), iron content amounted to 0.2 wt.%.

Claims

1. A method of processing lignite coal with an iron content in the ash of no more than 5% to produce a reducing agent for manufacturing industrial silicon, which includes heat treating said lignite coal in a fluidized bed at a temperature of 700-850°C by blasting at high speeds with a mixture of air and water vapor to provide for the transition of iron-containing compounds in the lignite coal to a magnetic form; cooling the resulting reducing agent; and then magnetically separating same over the course of 100-120 hours, immediately after the cooling stage, at a magnetic field induction magnitude of at least 1.1 T.