SU1582991A3 - Method and installation for producing metals and alloys - Google Patents

Abstract

The invention relates to metallurgy, specifically to the production of metals or metal alloys, mainly ferroalloys. The purpose of the invention is the expansion of technological capabilities. In order to obtain metals having a high affinity for oxygen, a coal layer is formed of three stationary layers A, B C. Layer A consists of degassed coal and is located above the liquid layer of reduced metal 3 and slag 4. Next, oxygen is introduced into the middle layer B or containing oxygen gas through pipes 8 to obtain a hot reducing gas, and at some distance above this into the middle layer B fine oxide oxide raw material is introduced through nozzles 9. In the uppermost layer C, combustible gases are introduced through burners 10 from part check coal and oxygen or oxygen-containing gas. Exhaust gases from reactor 1 through gas outlet 11 enter cyclone 12 to clean coal dust particles. The latter from cyclone 12 are fed through the metering device 13 to the burners 10. From cyclone 12, line 16 leads to another cyclone 17 for cleaning hot gases. With the line 16 through line 18 is connected to the hopper 19, containing fine-grained oxide material. Gas from line 16 serves as a transport medium. The oxide material 20 and from there is supplied via line 21 to the nozzles 9. 2 c. and 5 hp f-ly, 2 ill.

Description

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Above the liquid layer of reduced metal 3 and shpak 4. Next, oxygen or oxygen-containing gas is introduced into middle layer B through pipes 8 to obtain a hot reduction ras, and at some distance above this, fine-grained oxide source is introduced into middle layer E material through nozzles 9. Combustible gases from particles of coal and oxygen or oxygen-containing gas are introduced into the uppermost "Q layer C" through burners 10. Exhaust gases from reactor 1 through gas outlet 11 enter cyclone 12 for jc

The invention relates to the field of metallurgy, specifically to the production of metals or metal alloys, mainly ferroalloys.

The purpose of the invention is the expansion of technological capabilities.

The invention makes it possible to obtain metals and metal alloys in the reactor, in particular ferroalloys such as ferromargane, ferrochrome and ferrocilium, from lumpy oxide raw material, and the metal has such a high affinity for oxygen that it reacts with elemental carbon only above 1000 ° С

The coal bed (layer) is formed of three stationary 11 layers (A, B, C), with the lower layer (A) of degassed coal covering the liquid (sludge of reduced metal and slag); oxygen or hydrogen gas containing oxygen is introduced into the middle layer (B) in order to obtain a hot reducing gas consisting mainly of CO, and at a certain distance from the place where the gas was introduced into the middle layer fine-grained oxide was introduced. raw material; Combustible gases from particles of coal and oxygen or oxygen-containing gas are introduced into the upper layer (C).

A predominantly fine-grained starting material with a grain size of up to 6 mm is used.

It is advisable to use charcoal with pieces of 5–100 mm, in particular 5–30 mm, to form stationary layers.

cleaning dust particles ang. The latter of the cyclone 12 are fed through the metering device 13 to the burners 10. From the cyclone 12 the main line 16 leads to another cyclone 17 for the purification of hot gases. With the line 16 through line 18 is connected to the hopper 19, containing fine-grained oxide material. Gas from line 16 serves as a transport medium. The oxide material 20 and from there, via line 21, is supplied to the nozzles 9, 2 s. and 5 hp f-ly, 2 ill.

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The preferred option is the thickness of the middle and upper stationary layer of 1-4 m.

From the exhaust gas passing through the reduction zone, coal dust particles are predominantly in a hot state, together with oxygen or oxygen-containing gas, are supplied to the burners directed to the upper stationary layer.

The particulate gas released from the carbon can be used as a transport medium for the fine oxide material.

Such coal is used as coal, which, after degassing, retains a lumpy character, so that when using lumps of 5–100 mm, mainly 5–30 mm, after degassing, at least 50% of the degassed coal obtained has the same size 100 mm or 5-30 mm) p and the remainder in the form of pieces of a smaller fraction.

The method retains the known advantages of the reduction process in shaft furnaces where the energy of fossil substances is used — heat exchange in countercurrent, metallurgical reaction in a stationary layer with elemental carbon, which is needed to reduce non-precious metal oxides, as well as good separation of metal and slag. Coking or coal degassing can be carried out without forming a resin or other condensable compounds. The carbon formed during degassing acts as an additional reducing agent to the reducing gases formed from coal.

Oxide material can be pre-reduced in anticipation of /. that is rational in the production of ferroalloys, where part of the starting material from iron oxides is available for reduction.

The advantage of this method is that the reduction of oxides such as silicon, chromium, manganese can be carried out without the use of electrical energy.

FIG. 1 shows an installation for carrying out the method; in fig. 2- temperature profile in the reactor.

The installation contains a shaft-type reactor 1 equipped with a refractory lining 2. The bottom of the reactor zone serves to receive molten liquid metal 3 and molten liquid spat 4. The reactor has an outlet 5 for metal and 6 for slag. In the upper part of the reactor there is a feed opening 7 for feeding lumpy coal. Above a settler for liquid metal and slag, a stationary coal layer is formed, consisting of three layers: A - degassed coal, through which gases are not passed, layer B of degassed coal above it, penetrated by gases and above it, layer C permeated by gases.

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In the side walls of the reactor 1 holes for blowing through oxygen pipes 8 or oxygen-containing gas are made. These pipes are located in the boundary zone between impermeable gases of stationary layer A and stationary layer B. At some distance above them, namely in the zone from the middle to the upper part of the stationary

layer B, holes for nozzles are made, 45 through which a fine-grained oxide source is blown into the middle layer B

material. In the boundary zone between layer B and layer C there are holes for the burners 10, into which 50 a mixture of dust particles of coal and oxygen or oxygen-containing gas is introduced. From the upper part of the reactor 1, a gas outlet 11 is withdrawn, supplying the exhaust gases to the cyclone 12 for the purification of the secondary gases. The dust particles of coal suspended in suspension in the exhaust gas are separated in the cyclone 12 and from the discharge end of the cyclone.

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wherein the metering device 13 is provided, is supplied by the main 14 to the burners 10. A gas containing oxygen is supplied through the main 15 to the burners 10. The dosing device 13 can adjust the filling level of the cyclone 12 and take into account its separation effect.

From the top of the cyclone 12, line 16 leads to another cyclone 17 for cleaning hot gases. With the highway 16 through the highway 18 is connected to the hopper 19, containing fine-grained 5 oxide source material. Gas from line 16 serves as a transport medium. From the cyclone 17, the fine-grained oxide raw material is carried to the supply line 20 and from it via the line 21 is supplied to the nozzles 9 for injection.

From the upper end of the cyclone 17, line 22 leaves, through which excess exhaust gas is discharged. It can be cooled and compressed and blown through line 23 into line 21 as a transport means.

The method is carried out as follows.

The coal loaded in the upper part of the reactor 1 is degassed in the stationary layer C. The heat required for degassing, on the one hand, is supplied by hot reducing gases rising from the stationary layer B, on the other hand, this heat is obtained by the heat of combustion of solid particles burned in burners 10 with an oxygen-containing gas. The vertical extent of layer C is chosen in such a way that the gas leaving the layer C has a minimum temperature of 950 ° C, as a result, it is guaranteed that the resin and other condensable compounds are cracked, and clogging of the stationary layer C is prevented. 1–4 m. The vertical length of 1–4 m turned out to be also rational for stationary layer B. Coal degassed in layer C., when lowered, forms stationary layer B at the bottom.

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The fine-grained oxide starting material is pre-reduced with a hot reducing gas and volatile dust in the additional cyclone 17 and again separated from

gas. Saturation of hot reducing gas with fine-grained coal-containing dust can be rational, since coal reacts with C02 formed during reduction to form CO, thereby preserving the intensely reducing nature of hot gas (coming out) from reactor 1, fine-grained oxide starting material Separated after pre-reduction with volatile dust, melted in layer B, and reduced with elemental carbon. The heat required for melting and recovery is provided by the gasification of hot degasified coal with oxygen-containing gases supplied to the reactor through pipes 8 for injection. The molten liquid metal arising in the stationary layer B and the molten molten slag flow downwards and below layer A are collected and expelled. released from the reactor.

FIG. 2 shows the temperature profile along the height of the reactor-1, with the height parameters plotted on the ordinate, and the temperature on the abscissa. The solid line corresponds to the temperature curve of the injected coal, and the dashed line to the temperature curve of the circulating gas, Marked height 8 is a contour of injection pipes 8, height 9 represents the level of nozzles 9 for injection of fine-grained oxide raw material (ore), height 10 represents the return of coal particles with burners 10, the height 24 represents the upper limit 24 of the stationary layer, and the height 11 represents the gas outlet 11 and the charging opening 7 for coal.

Claims (7)

Invention Formula 1, a method for producing metals and alloys, mainly ferroalloys, including the reduction of crushed oxide material in a reduction zone containing coal, injecting oxygen or oxygen-containing gas into the coal bed, separating coal particles from the exhaust gases and supplying them with oxygen or oxygen-containing gas in burners, characterized in that, in order to expand the technological capabilities, the recovery zone in height consists of three stationary layers of coal A, B, C, while oxygen or oxygen containing This gas is blown at the interface between the lower layer A consisting of degassed coal and the middle layer B into which fine-grained oxide material is blown above, and a combustible mixture of particles of coal and oxygen or oxygen-containing gas is introduced into the upper layer of coal. 2. A method according to claim 1, characterized in that the fine-grained oxide material has a fraction to 6 mm 3. A method according to claim 1, characterized in that for forming stationary layers A, B, C, coal of a fraction of 5-100 mm is used, preferably 5-30 mm. 4. Method according to paragraphs. 1-3, characterized in that the thickness of the middle and upper layers B and C is maintained from 1 to 4 mm. 5. Method according to paragraphs. 1-4, characterized in that the waste gas from the reactor, purified from coal particles, is used as a transporting medium for fine-grained oxide material, 6. Installation for the production of metals and alloys, mainly ferroalloys, containing a shaft-type reactor with a refractory lining, in the upper part of which holes are made for charging coal and for gas extraction, the side walls of the reactor in the reduction zone are provided with pipelines for injecting oxygen or oxygen-containing gas, and the bottom of the reactor is made of metal and slag outlets, a cyclone for separating coal particles from exhaust gases, the outlet end of which is connected to burners by a pipeline, is distinguished by and in that, for the purpose of expansion of technological capabilities, the side wall of the reactor is further provided with openings connected to ducts for injecting fine-grained oxide material located in the area above the restored fines pipelines feeding oxygen or oxygen-containing gas, and the burners are located in the side wall of the reactor above the pipelines for injecting the oxide material. 7. Installation according to claim 6, characterized in that the feed hopper with oxide material is connected to the pipeline connecting the cyclone. for flue gas and burner cleaning to preheat the oxide material, the discharge end of which is connected to the pipeline to inject the oxide material into the reactor. t woo 2000 2