• 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:
    1470938 Reducing iron oxides STORA KOPPARBEEGS BERGSLAGS AB 5 May 1975 [20 May 1974] 18833/75 Heading C5E In a method of reducing particulate material containing iron oxides in a fluidized bed, particulate carbonaceous material containing volatiles is introduced at one or more points in the fluidized bed and the material containing iron oxides is introduced into the bed in the region where the volatiles in the carbonaceous material are driven off and partially gasified and coked. The iron-oxide-containing material may be mixed with the carbonaceous material before introduction. Embodiments employing both stationary and recirculating fluidized beds are described. The carbonaceous material, which preferably has at least 15% volatiles content, may be lignite or bituminous coal.
    公开号:SU850012A3
    申请号:SU752136152
    申请日:1975-05-20
    公开日:1981-07-23
    发明作者:Харальд Коллин Пер；Виделл Бьерн
    申请人:Стора Коппарбергс Бергслагс Актиеболаг(Фирма)；
    IPC主号:
    专利说明:

    Part of the concentrate particles combined with the coke particles, coal should have more than 15% of volatile substances. The best results are obtained with a higher content of volatile substances, for example, in coal such as bituminous and brown. The size of the coal particles depends on the properties of the fluidized bed. In addition, the material containing iron oxides must have a smaller particle size than the carbon-containing material, since it has a larger specific gravity.
    FIG. 1 shows a conventional fluid bed; FIG. 2 - circulating fluidized bed.
    A fluidized bed reactor consisting of a reactor chamber 1, in which bottom 2 is located, distributing gas flow; feed pipe 3 for reducing gas and exhaust pipe 4 for flue gases. The recovered material is discharged through an outlet pipe 5.
    The recoverable material is fed through inlet pipe 6. Powder coal with a high content of volatile substances is continuously fed as an adjustable stream through pipe 7. At the exit of the feeding pipe 7, zone 8 is formed, by which these volatile substances are sublimated, partially gasified and coked. A tube 6 for a material containing iron oxides is positioned so that the material is fed into said zone 8, resulting in the formation of micro particles of coke and concentrate. In the bottom of the chamber of the reactor 2 are .c holes 9.
    FIG. 2 shows a device which uses a circulating fluidized bed, i.e. the layer in which the gas velocity is maintained at such a level that the layer completely fills the reactor chamber and the gas removed from the chamber, which is high in solids, is cleaned in the cyclone, and the particles then return to the reactor chamber. The sizes of the particles of the material processed in the circulating fluidized bed are smaller than the dimensions of “1” in the usual layer.
    The reactor (Fig. 2) consists of a chamber with sections 10, 11 and 12, the upper section 10 of which is connected to a cyclone 13 having a return pipe 14 for returning solid particles separated in a cyclone to the central part
    11 chambers of the reactor. In the lower section
    The material containing iron oxides is set by means of a reducing gas supplied from below. When the specified gas enters
    In the central part of the reactor, it is partially burned along with the coal with the help of air supplied through a series of nozzles 15, which ensures the arrival of heat for the recovery process. Coal with a high content of volatile substances is supplied to the central part 11 through the pipe 16. The volatile substances are sublimated in zone 17 around the inlets. The material containing iron oxides is supplied in the form of a proportional flow into the indicated zones through the feed pipe 18.
    Thus, coke and concentrate microparticles are formed, which are transferred by gas through the upper part of the reactor chamber to the cyclone 13 and return to the central part 11 of the reactor through pipe 14. After one of several circuits in the upper part of the reactor, particles that have already been heated and partially recovered, fall into the lower part 12 of the reactor, where further reduction takes place using a reducing gas, after which they are removed through pipe 19. The flow of solid material fed to the reactor and the flow of material al emogo from the reactor are adjusted in such a way
    5 that the amount of solid material in the reactor remains constant. The exhaust gas from the reactor enters the dispenser 20, in which it mixes with the untreated material supplied by the diverter 21. This material is pre-heated with the help of gases collected in two cyclones 22 and 23. A part of the gas removed from the cyclone 23 is cleaned from CO and HgO in the device 24 and after heat exchange and preheating are used as a reducing gas in the lower part of the reactor (12), while the remaining part 25 is used as industrial fuel.
    The proposed method allows for the recovery of particles in the layer without sticking at temperatures up to 900 ° C. Invention Formula
    A method of reducing iron ore materials in a fluidized bed, comprising inserting materials and coal into the layer, characterized in that, in order to prevent sticking of the reduction product, materials and coal are introduced in adjacent streams, of which one consists of coal with a minimum volatile content, equal to 15%.
    Sources of information taken into account in the examination
    1. Kozhevnikov I.Yu. Beskox metal metallurgy. M., Metallurgists, 1970, p. 53-55.
    权利要求:
    Claims (1)
    [1]
    Claim
    The recovery method is iron ore materials in a fluidized bed, including the input into the layer of materials and coal, characterized in that, in order to eliminate adhesion of the recovery product, the coal is injected by adjacent flows of which are at least 15%.
    materials and, one consists of coal with a volatile content of minus
    类似技术:
    公开号 | 公开日 | 专利标题
    EP0304931B1|1992-04-15|Method and apparatus for gasifying or combusting solid carbonaceous material
    US4336128A|1982-06-22|Combustion of pyrolyzed carbon containing solids in staged turbulent bed
    US4969930A|1990-11-13|Process for gasifying or combusting solid carbonaceous material
    US4145274A|1979-03-20|Pyrolysis with staged recovery
    US3703442A|1972-11-21|Method for the low-temperature distillation of finely granular bituminous materials which form a pulverulent residue in the process
    SU1528324A3|1989-12-07|Method of obtaining cast iron in horizontal reactor
    EP0003117A2|1979-07-25|Two-zone fluid bed combustion/gasification
    US3140862A|1964-07-14|Apparatus for the physical and/or chemical treatment of granular solids or fine dusts
    CA1306641C|1992-08-25|Fluidized bed process and apparatus for carrying out the process
    US4359212A|1982-11-16|Apparatus for reducing finely divided iron oxide material
    US3444048A|1969-05-13|Continuous coking apparatus
    US3020209A|1962-02-06|Plant and process for the production of oil
    US4565139A|1986-01-21|Method and apparatus for obtaining energy
    US3042498A|1962-07-03|Apparatus for roasting sulfides
    JP4785839B2|2011-10-05|Direct reduction equipment and process
    SU850012A3|1981-07-23|Method of redusing iron ore materials in bolling layer
    US5915311A|1999-06-29|Process for the thermal treatment of waste material
    US3145094A|1964-08-18|Process and apparatus for making steel from powdered iron ore
    US5529291A|1996-06-25|Circulating fluidized bed direct reduction system
    US4413573A|1983-11-08|Process for combusting carbonaceous solids containing nitrogen
    US4084958A|1978-04-18|Method of reducing finely grained material containing iron oxides in a fluid bed
    US3046106A|1962-07-24|Iron ore reduction with coke
    JP4785840B2|2011-10-05|Direct reduction process using a single fluidized bed
    EP0117634A1|1984-09-05|Apparatus for contacting fluids and particulate materials
    DE974376C|1960-12-08|Method and device for degassing dusty or fine-grain fuels
    同族专利:
    公开号 | 公开日
    NL7505896A|1975-11-24|
    JPS50159401A|1975-12-24|
    SE7406695L|1975-11-21|
    FR2272176A1|1975-12-19|
    DE2521038C3|1981-09-17|
    DE2521038A1|1975-11-27|
    LU72504A1|1975-08-28|
    GB1470938A|1977-04-21|
    BE829170A|1975-09-15|
    FR2272176B1|1977-12-09|
    AU8094075A|1976-11-11|
    SE384226B|1976-04-26|
    IT1035769B|1979-10-20|
    DE2521038B2|1980-10-09|
    CA1070954A|1980-02-05|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE1186887B|1959-06-18|1965-02-11|Demag Elektrometallurgie Gmbh|Process and device for refining fine-grain iron ores in an electrically heated floating bed made of fine coal|SE419129B|1979-05-29|1981-07-13|Stora Kopparbergs Bergslags Ab|DEVICE FOR REDUCING FINE DISTRIBUTED IRON OXIDE-CONTAINING MATERIAL IN A CIRCULATING FLOAT BED|
    DE3835332A1|1988-10-17|1990-04-19|Ralph Weber|METHOD FOR PRODUCING STEEL FROM FINE ORE|
    AT390622B|1988-10-25|1990-06-11|Voest Alpine Ind Anlagen|METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIG IRON|
    FR2683829B1|1991-11-19|1994-07-22|Siderurgie Fse Inst Rech|CIRCULATING FLUIDIZED BED IRON ORE REDUCTION TREATMENT PLANT.|
    DE10101157A1|2001-01-12|2002-07-18|Mg Technologies Ag|Process for producing a mixture of iron ore and smoldering coke|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE74066951A|SE384226B|1974-05-20|1974-05-20|MAKE REDUCTION OF FINE DISTRIBUTED IRON OXIDE MATERIALS IN FLOAT BED|
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