• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A novel process for producing molten pig iron or steel raw material is described. The pig iron is initially at least partly reduced to sponge iron by means of a reducing gas and is then melted in a melting gasifier, being optionally finally reduced. Apart from the sponge iron, the melting gasifier is supplied with coal at least partly degassed by a hot gas and oxygen-containing gas. The hot gas used for this purpose is formed from the gas produced during degassing and a supplied, oxygen-containing gas. The latter is preferably constituted by air, which can be preheated by the gas produced during degassing.
    公开号:SU1711677A3
    申请号:SU874203825
    申请日:1987-12-14
    公开日:1992-02-07
    发明作者:Хаук Рольф；Папст Геро
    申请人:Фоест-Альпине Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the extra-domain production of iron and steel.
    The purpose of the invention is to increase the efficiency of the process.
    The drawing shows a plant for reducing iron ore, in which iron ore is converted to molten iron. ./ Iron ore and possible additional substances are introduced into the recovery shaft furnace 1 through the charging device 2. Through the lower outlet 3, sponge iron obtained by reducing iron ore is withdrawn. In order to carry out the reduction process, a reducing gas is supplied to the reducing shaft furnace 1 in the so-called plane Boostle through the inlets 4, which flows upward against the oxidized iron ore descending in the reducing furnace 1 and is reduced by direct reduction into sponge iron. The reducing gas contains reducing components, such as CO and H2. Further, it has the necessary recovery temperature of 750-950 ° C. The burnt reducing gas as top gas is discharged through one upper outlet 5 of the reduction shaft furnace 1 and cleaned by VJ 41

    with
    In the scrubber 6, it is also equally free of COz, after which it is further applied in the usual manner.
    Sponge iron enters from the reduction shaft furnace 1 through the dip pipes into the melter gasifier 7. It flows from above onto the vortex layer, which is maintained by means of the oxygen-containing gas injected into the lower zone melting gasifier 7. Then from above to the melting gasifier through the filling hole. Stage 9 receives coke, and coal through the filling opening 10.
    By burning: coke, as well as coal, under the influence of oxygen-containing gas in the vortex layer, such heat is generated that the sponge iron is melted. In the molten state, it is finally reduced by means of carbon, so that a molten iron is collected at the bottom of the melting gasifier 7. Liquid slag is collected above the molten iron. These two melts are discharged at predetermined intervals through different outlet openings 11, preferably located at different heights.
    During the combustion of coke and coal in the melter gasifier 7, a further gas containing reducing components, preferably CO, appears, which is discharged through an outlet 12 in the head of the melter gasifier 7 and is cleaned in a cyclone 13, after which it as a reducing gas through the inlets 4 is sent to the reduction shaft furnace 1. The solids separated in the cyclone 13 from the gas return at the height of the vortex layer again to the melting gasifier 7.
    The coke entering the melter gasifier 7 is produced from coal with a high content of volatile components, for example, more than 40% (combustible mass of fuel). In this case, the coal through the inlet 14 enters the degassing reactor 15, in which the coal is exposed to hot gas and thereby degassed. The hot gas is blown through the inlets 16 in the bottom of the degassing reactor 15 so that a vortex layer is preferably formed in the degassing reactor 15. A number of inlets 16 arranged at the same height are provided, which are made in the form of nozzles and are connected by an annular conduit as well as generator 17 mountains of
    gas with combustion chambers. The inlets 16 may be made of ceramic nozzle stone.
    Hot gas generator 17 contains
    combustion chamber in which combustible gases are burned with air. These combustible gases consist, at least in large part, of the gases produced during the degassing process. These gases are removed.
    through the top outlet 18 of the degassing reactor 15 and first fed into the cyclone 19. The solids separated in the cyclone 19 pass directly through the conveyor 20 to the melting gasifier 7. Purified in
    cyclone 19 gas enters the heat exchanger 21, in which the air used to form hot gas is preheated to a temperature of 300-400 ° C. After passing through the heat exchanger 21 parts
    waste gas degassing reactor
    15, line 22 is directed to a hot gas generator. The amount of this used for the production of hot gas flue gas degassing reactor
    15 is determined according to the requirement for a hot gas for the degassing process. Waste waste gas is removed through conduit 23 and is used for other purposes.
    Air is supplied to line 24 through heat exchanger 21 and then blown into the combustion chamber of the hot gas generator 17. Part of the preheated air branches off through line 25 and is fed to the upper zone of the degassing reactor 15. Thus, the temperature of the gas generated therein can be regulated so that there was no formation of tar. Speaker through release 18
    the waste gas has, for example, a temperature of approximately SOO0.
    Blown through inlets
    16 hot gas results in a degassing reactor 15 to form a vortex layer.
    The incoming coal from above is degassed and dried in this vortex layer. Desalting agent, such as dolomite or limestone, may be added to the coal.
    for desulfurization, it is withdrawn either with a current or with exhaust gas through an outlet 18 of the degassing reactor 15.
    Coke enters through pipe 26, which enters the bottom of the degassing reactor 15, from it into the melting gasifier 7. In order to remove coke from the degassing reactor 15, several radially passing screw conveyors are located above it at the bottom.
    The gas pressure in the degassing reactor 15 is preferably set to match the gas pressure in the melter gasifier 7. This prevents gas exchange between the melter gasifier 7 and the degassing reactor 15, and there is no need for an expensive lock system.
    In addition to the flue gas from the degassing reactor 15, top gas from the reduction shaft furnace 1 can also be used as a combustible gas to produce hot gas if the flue gas from the degassing reactor is not sufficient to achieve sufficient degassing. Due to this, it is avoided that special energy is supplied for this case or part of the coal intended for degassing must be burned. .
    The flue gas from the reduction shaft furnace 1 is usually also partially returned to the reduction process, while it is, after removal of G02, mixed into the reduction gas before being blown into the reduction shaft furnace. When returning the flue gas without the CO 2 removal process to the gasifier, it is recommended that all the coal intended for introduction into the melter gasifier 7 is degassed first in the degassing reactor 15, i.e. no additional coal is introduced through the inlet 10. However, if no flue gas return is provided, then only a part of the coal must be degassed before being introduced into the melter gasifier 7. Part of the coal, for example 50%, can then be introduced through the inlet 10 after the drying process directly into the melter gasifier 7.
    In addition to coal degassing, the degassing reactor can also be used for the preliminary reduction of iron ore. This ore is additionally supplied to the coal in the degassing reactor and is preheated and pre-reduced therein and then directly, together with the coke, enters the melter gasifier. This solution can be carried out instead of pre-reduction in the reduction shaft furnace or also in addition to this. The ore previously recovered in the degassing reactor can also, if it is fine-grained, be captured with a degassing waste gas and then separated in a cyclone. From it, it then enters the melting gasifier and is blown into the vortex layer formed in it. For the preliminary reduction of iron ore in the degassing reactor, several vortex layers can also be formed in it.
    Example. A case of mixing in a melter gasifier 80% of high-temperature lignite coke from a degassing reactor and 20% lignite briquette with 17% G20 and 7% slag is given. For the production of 25.9 t / h of high temperature lignite coke, 62.4 t / h of briquette is required. For heat generation for degassing, 20% of the initially produced degassing gas is required. From here, the following material flows are obtained: 40 t / h cast iron; 19,000 m3 / h Oa; 56,000 m reducing gas; 60 t / h ore; 21,500 m3 / h amount of air; 46,500 m / h export gas from the degassing reactor; 11,500 m3 / h combustible gas; 5800 m3 / h gas from the degassing mine; 25.9 t / h high-temperature coke; 62.4 t / h brown coal briquette; 6.9 t / h brown coal briquette.
    The effluent gases leave the degassing reactor 15 at 600-900 ° C, preferably at 800 ° C. The temperature depends on the type of coal that is degassed. The gas emitted is coke oven gas and consists of 60% H2, 28% CH / i; 4% C0.4% SpNt, 24%. . .
    Air is used as the gas containing oxygen, which is admitted to the heat exchanger 21 at an external temperature of 24 ° C and leaves it at about 600 ° C. In the same way, the evolved gas passes through the heat exchanger, loses, respectively, the temperature and therefore flows through conduit 22 with a temperature of about 650 ° C.
    The oxygen-containing gas (preheated air) and the evolved gas are introduced into the hot gas generator 17 in a ratio that ensures that oxygen is not in excess (stoichiometric ratio of 0.95). The hot gas enters the degassing reactor 15 with a temperature of about 900 ° C.
    权利要求:
    Claims (7)
    [1]
    1. A method of producing molten iron or an intermediate product for steel production, including coal degassing with gases obtained by burning heated waste and oxygen-containing gases, preliminary reduction of iron ore to sponge iron, subsequent final reduction and melting due to the supply of degassed coal and oxygen-containing to the melter gasifier gas and gas recirculation characterized in that. that, in order to increase the efficiency of the process, gases obtained in the degassing process are used as the off-gas supplied to combustion with oxygen-containing gas.
    [2]
    2. Method according to paragraphs. 1 and 2, which is based on the fact that the oxygen-containing gas supplied to the combustion is heated by the gas obtained in the degassing process.
    [3]
    3. Method according to paragraphs. 1-3, that is, so that coal degassing is carried out in a fluidized bed.
    [4]
    4. Method according to paragraphs. 1-3, characterized in that the pressure in the degassing chamber is set equal to the pressure in the upper part of the melter gasifier.
    [5]
    5. The method according to claim 1, characterized in that the gas obtained from the pregeneration zone is additionally added to the gas obtained by the degassing process.
    130
    five
    0
    five
    [6]
    6, An apparatus for producing molten iron or an intermediate product for steel production, comprising interconnected shaft reduction furnace and a melter gasifier having an oxygen-containing gas input unit, a degassing reactor, having coal and heated air and gas input units and an exhaust gas output node and connected to the melter gasifier by a coke supply pipeline, a cyclone, a heat exchanger and a gas recirculation system, from the fact that, in order to increase the efficiency of the process, The facility is equipped with a hot gas generator with flue chambers connected to the reactor-degasser heated gas input unit and through a cyclone and a heat exchanger with its exhaust gas output unit.
    [7]
    7. A device according to Claims B., characterized in that the heated air inlet unit is located in the zone of location of the exhaust gas outlet unit.
    24 21- - °
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    同族专利:
    公开号 | 公开日
    SE8704893L|1988-06-24|
    ZA878869B|1988-08-31|
    DD274055A5|1989-12-06|
    LU87077A1|1988-04-05|
    KR880007747A|1988-08-29|
    ATA333487A|1994-06-15|
    DE3644775C2|1988-11-17|
    DE3644775A1|1988-07-14|
    JPS63255310A|1988-10-21|
    GB8727079D0|1987-12-23|
    AU8229887A|1988-06-23|
    AT398783B|1995-01-25|
    SE8704893D0|1987-12-08|
    US4857105A|1989-08-15|
    IT8723187D0|1987-12-23|
    BR8707022A|1988-08-09|
    IN168757B|1991-06-01|
    AU607729B2|1991-03-14|
    IT1224408B|1990-10-04|
    GB2199339B|1990-08-08|
    GB2199339A|1988-07-06|
    引用文献:
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    RU2591908C2|2010-04-26|2016-07-20|Прайметалз Текнолоджиз Аустриа ГмбХ|Method for production of cast iron or liquid steel intermediate products|US3414480A|1965-10-01|1968-12-03|Hydrocarbon Research Inc|Fractional vapor product absorption of fluidized lignite carbonization|
    US3661543A|1969-11-26|1972-05-09|Exxon Research Engineering Co|Fluid coking process incorporating gasification of product ore|
    DE2931472A1|1978-09-18|1980-03-27|Ford Werke Ag|METHOD FOR GASIFYING COAL|
    DE2843303C2|1978-10-04|1982-12-16|Korf-Stahl Ag, 7570 Baden-Baden|Process and plant for the production of liquid pig iron and reducing gas in a melter gasifier|
    US4248626A|1979-07-16|1981-02-03|Midrex Corporation|Method for producing molten iron from iron oxide with coal and oxygen|
    US4316739A|1979-07-16|1982-02-23|Midrex Corporation|Method for producing molten iron|
    GB2116580B|1982-03-12|1985-04-11|British Gas Corp|Gasifying coal in fixed bed ash-slagging gasifier|
    AT376243B|1983-01-19|1984-10-25|Voest Alpine Ag|METHOD FOR MELTING AT LEAST PARTLY REDUCED IRON ORE|
    JPH0360884B2|1984-09-12|1991-09-18|Kobe Steel Ltd|
    AT380697B|1984-11-07|1986-06-25|Voest Alpine Ag|METHOD FOR MELTING AT LEAST PARTLY REDUCED IRON ORE AND DEVICE FOR CARRYING OUT THIS METHOD|
    DE3503493C2|1985-01-31|1987-10-22|Korf Engineering Gmbh, 4000 Duesseldorf, De|
    DE3504346C2|1985-02-06|1986-11-27|Korf Engineering GmbH, 4000 Düsseldorf|Method and device for the production of sponge iron particles and liquid pig iron|
    DE3737271C2|1986-12-23|1991-10-10|Deutsche Voest-Alpine Industrieanlagenbau Gmbh, 4000 Duesseldorf, De|AT394201B|1989-02-16|1992-02-25|Voest Alpine Ind Anlagen|METHOD FOR GENERATING COMBUSTIBLE GASES IN A MELT-UP CARBURETTOR|
    DE4037977C2|1990-11-29|1992-09-24|Deutsche Voest-Alpine Industrieanlagenbau Gmbh, 4000 Duesseldorf, De|
    US5238486A|1991-02-19|1993-08-24|Kremenets Yury D|Method and furnace for production of liquid iron|
    GB2281311B|1993-03-29|1996-09-04|Boc Group Plc|Metallurgical processes and apparatus|
    GB9325418D0|1993-12-13|1994-02-16|Boc Group Plc|Method and apparatus for producing iron|
    KR100910723B1|2002-11-14|2009-08-05|주식회사 포스코|Hot coal relay apparatus of contiguous interfurnace|
    US20050151307A1|2003-09-30|2005-07-14|Ricardo Viramontes-Brown|Method and apparatus for producing molten iron|
    CN108485723B|2018-04-24|2021-06-08|东北大学|System and process for recycling inflammable and explosive inorganization diffused gas|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3644775A|DE3644775C2|1986-12-23|1986-12-23|
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