• 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:
    New method for the production of raw iron or so-called metallized iron ore. Biofuels i.e. preferably fuel wood and/or peat is in the final reduction brought into direct contact with the iron containing material in its solid state. Biofuels have very different properties compared to reduction agents on the basis of fossil fuels primarily coal and develop rapidly a reactive reduction gas at a comparatively low temperature. The new raw iron process is carried out with the iron containing material in its solid state of aggregation in different kinds of fluidized bed reactors in different system configurations.
    公开号:SU1012797A3
    申请号:SU813266145
    申请日:1981-03-31
    公开日:1983-04-15
    发明作者:Линдстрем Олле
    申请人:Олле Линдстрём (Швеци )；
    IPC主号:
    专利说明:

    This invention relates to a process for the reduction of fine iron material containing material to produce raw iron or metallized iron ore,
    Numerous attempts have now been made to develop methods for producing raw iron by reducing iron-containing material, such as iron oxides. Crude iron can be further converted during the reduction process or it can remain as a starting material for further processing in steel production.
    -. The reduction proceeds at a temperature below the melting point of iron, and the iron-producing material, and the reducing substance are in a finely dispersed state. Ispol
    The reducing agent is a fossil fuel, such as anthracite, coal, lignite oil or natural gas. These fuels are coked to varying degrees into solid carbonaceous material which is present in the initial mixture along with the jelly containing material.
    The reduction processes are usually carried out in several stages and in different installations, for example, in a modern furnace or in a fluidized bed furnace, and require the use of highly reactive reducing agents and high temperatures.
    The closest to the proposed technical essence and the achievement of the MOMy result is a method that includes the stages of preliminary heating, preliminary and final reduction with gas, which is outgoing from the previous stage of reduction 23.
    The speed of the reduction process, especially the final reduction to metallic iron, depends on the particle size of the iron-containing material, as well as on the reactivity of the reducing agent. The most preferred fossil fuels, such as coal for dust, require relatively high temperatures to achieve sufficiently fast pyrolysis and gasification reactions, which result in reducing reactive with iron-containing material.
    The purpose of the invention is to increase the speed of recovery,
    This goal is achieved in that according to the method of reducing iron-containing material in a finely dispersed state, comprising the steps of preheating, preliminary and final reduction with the gas leaving the previous recovery stage, the final recovery step is carried out with solid biofuel supplied together with the iron-containing material.
    The final reduction stage is carried out with an iron-containing material ground in a ball mill to a particle size of meridor 0.01 mm, with LO-60P C; The extrusions are carried out under pressure. As bio-fuel, plant biomass can be used, obtained as raw material from plantations, for example, fast-growing willow or poplar, waste paper and pulp production (wood and bark) or straw, brown algae, peat and.
    30, FIG. 1 is a flow chart of the method; in fig. 2 and 3 graphs showing the properties of biofuels used in the implementation of the proposed method; on
    35 of FIG. t is a device for carrying out the method.
    The process of reducing iron-containing material, such as iron ore concentrate, includes several stages: the preheating stage, the pre-reduction stage and the final stage of recovery, and these stages can be combined with final processing, each stage can include several intermediate stages.
    Biofuel is added to the final recovery stage,
    Jq. as a result, the iron-containing material is reduced to a bivalent iron (it is reduced to metallic.
    As a result of pyrolysis,
    highly reactive reducing gases and a highly reactive residue, pyrolysis (a substance converted into coal). The remainder of the pyrolysis is often much less than the stage of the final head of the added fuel load during fast pyrolysis, which occurs when compared to the remainder when using fossil fuels (fossil fuels have a significantly higher thermal stability than biofuels). ). Due to a more reactive reducing gas, the reduction process can be carried out at a lower prite rate, which the so-called cladding problem is eliminated. The remaining carbon-converted substance is especially effective for inhibiting the formation of a coating. When the final recovery is carried out at a temperature of l / 600 or lower, it is desirable to recycle a portion of the pelvis from the final recovery stage (see Lig.1). The main part (and sometimes all) of the required heat for the preliminary reduction and final reduction is obtained with a strong preliminary heating of the iron-containing material in the preliminary stages, which is mainly carried out by burning the remaining recovery gas from the preliminary reduction stage. Pyrolysis and gasification reactions also require energy, and these needs can be satisfied in a similar manner. The main advantage of npti with the use of biofuels is that the need for such energy is extremely small (when using biomass, the thermochemical process can be exothermic). It is often desirable to use as much energy as possible, qo holding in the reducing substance in the form of chemical energy. by balancing various processes with direct and indirect heat exchange. The final treatment (see FIG. 1) may contain, for example, the inactivation of the highly reactive raw iron ferrous product obtained during the low-temperature reduction of the fine iron ore concentrate, and smelting in an electric furnace for further purification. The table shows the comparative. chemical composition of biofuels and fossil fuels (coal). The plant biomass has a high oxygen content, which explains its high reactivity at low temperatures. compared with fossil fuels. Peat is a constantly growing mass, very close to biomass in its chemical structure and thermodynamic properties, and as a result, it is more related to biofuels than to fossilized fuels, and therefore can be used in the implementation of the proposed method. It is also possible to mix different types of biofuels, such as peat and wood. Natural biomass has a high water content, which should be reduced as much as possible (up to about 30% by weight) before using biomass as a biofuel. Drying can be easily carried out with the help of alkaline dryers or other means by using the excess heat from the process of creating the "-Goon." The steam generated during the reduction processes can be used to partially gasify the coal-converted substance obtained during pyrolysis. 5 The plots (figs, 2 and 3) demonstrate the different chemistry of the process with the coking of biofuels as compared with the use of solid fossil fuels. In FIG. 2 is a graph explaining the experimental results for comparing the nature of certain reducing substances when they are subjected to pyrolysis with a flash, namely when the temperature rises at a speed of a minute in the argon sphere, the percentage of the restoring substance (calculated on free moisture and free ash) depending on the pyrolysis temperature. As can be seen from the graph of FIG. ., biofuels C peat, bark, poplar and straw) show large weight loss at a much lower temperature compared to coal. FIG. 3 is a graph / explaining the results of ek :: perim} nta compared the gasification rates of certain converted into coal substances when they are subjected to an increasing temperature of gasification in an argon - water vapor atmosphere containing 73 vol., Water vapor. As seen from this graph-graph, the substance converted into coal from the biofuel (poplar) is gasified at a higher rate and at a lower temperature than coal. Selective material may include fine iron containing ore, such as siderite (RePoG), magnetite () and hematite (), Siderite contains iron in a bivalent state, therefore, the pre-reduction stage, is replaced by a stage of calcination to remove carbon dioxide, as iron containing The material can also be used - violet ore or other fine products containing iron oxides, such as dust and shtyb from blast furnaces, steel production and rolling mills. In subsequent purification processes, various pre-additives can be used, for example, alkaline earth metal oxides or carbonates, which are also used to prevent the cladding during the final reduction stage. The particle size of the iron containing material must be less than mm when the method is carried out in one or more conventional fluidized beds, and must be less than 0.5 mm when carried out in so-called fast or circulating fluidized beds. Biofuel particles should be 2-3 times larger than particles of iron-containing material. these particles have a size of about 5 mm to a few centimeters. Thus, it is possible to use wood chips in conventional fluidized beds, while in circulating beds or to recover highly comminuted iron-containing material, such as iron ore concentrate, subjected to spherical grinding, it is necessary to use finely ground wood powder with a particle size of mm. The fast-recovery processes that are characteristic of the invention are promoted if the iron-containing material, as well as the biofuel, are present in a finely ground state. Iron ore concentrate that is industrially available, for example iron concentrate, ores from the mines in Krinua and Malmberget (Sweden) ,. Especially suitable for carrying out the proposed method without special preparation. It is possible to carry out the final reduction stage at a very low temperature in the range of 00-60P C due to further ball milling of the iron ore concentrate to a particle size of 0.01 mm or less, so that the final reduction is carried out to a metallic iron without intermediate transition to the divalent state. the The possibility of final reduction at such a low temperature is determined only by the thermodynamic properties of these fuels. Strongly ground iron powder can in certain cases be directly used for metallurgical processes, such as producing porous iron electrodes for batteries of various types. Direct use of raw iron is possible only if it has such a chemical composition relative to other metals and elements, for example sulfur, which can either be admitted in the final product or can be adjusted by choosing appropriate reaction conditions. The coal-converted substance accompanying the iron ryrbgo powder can either be separated with magnetic separators that separate the iron, or can be left in the product for various purposes, for example, to use the material as a gasket in the manufacture of sintered porous iron products. The potential reactor for the implementation of the proposed method has a single classical fluidized bed, in which the reduction is carried out in a periodic manner. The reactor includes a vessel 1 with a gas distribution plate 2 in its lower part, a gas supply pipe 3, an exhaust pipe 4 for gas, a supply (means 5 for biofuel and discharge means 6 and discharge means g7 for iron-containing material. Fluidized bed R is fluidized by gas supplied through pipe 3 and / or gas, which arises from biofuels during final recovery. The action of the fluidized bed depends on a large number of additional devices, such as valves, connecting pipes and separators. dust, process control indicators, heat exchangers, loading means for fuel, (means for adding air and / or oxygen are not shown). At the first stage of the process, the green powder is loaded into the reactor, heated to 1000-120 ° C with hot gases, which arise when burning a reducing gas, which is removed from the second such reactor, where the preheated iron-containing piston is subjected to a preliminary reduction stage. This second reactor, in turn, receives its reducing gas from the third under the OIHO reactor, in which the preformed iron-containing powder is subjected to a final reduction stage. The pre-reduction in the second reactor starts at a temperature of up to 10 97 credential heating 1000-120 ° C, and then the temperature decreases to / v-SOO C, and at that time begins, the stage of final reduction in this reactor by; loading of biofuels, which results in a further decrease in the temperature of the pre-flow. C. The appropriate conditions for fluidization are maintained by recycling the reducing gas and controlling the loading of the biofuels. Additional heat for regulating the rate of heating is provided by the supply of air and / or oxygen. Carbon dioxide and water are removed in a known manner before recycling the reducing gas. A great advantage is to conduct the process with more than three reactors and in more than three stages of the process. The use of, for example, three reactors connected in series to a preheating stage makes it possible to carry out the process in three different temperature ranges in three reactors, the last reactor of the series being heated by gas leaving the preceding reactor, which in turn heats up outgoing gas from the initial reactor of the series. Thus, it is possible to reduce the temperature of the release of the chopping system to Medium gas, (.. Its level. In addition, the proposed method can be carried out in two fluidized beds, connected in series continuously. In this case, one fluidized bed performs the function of preheating and acts continuously at 1100-120P C by burning the outgoing gas. The preheated material containing iron oxide continuously leaves the preheated layer, in which the e and final recovery. The reducing layer acts upon. The biofuel is supplied directly to the layer along with the recirculated gas and possibly air and / or oxygen. The unloaded recovered material can be sent directly to clean or press the raw iron products. The pre-heated layer can be used in a known manner in a boiler for generating electrical energy, steam and hot water. The reaction time can be significantly reduced if the preliminary and final reduction stages are carried out under pressure, e.g. 0.5-2 MPA. The principle of a batch reactor is particularly suitable for. recovery under pressure. Pressing also provides faster bio fuel loading. Download speed often og. It is limited at atmospheric pressure by the need to limit the gas velocity for optimal fluidization. The reaction time, as well as the bed size, depends on a large number of factors, in particular, on the particle size up to the draft and the temperature of the process. As shown by laboratory ex
    UiF 6OV 900 TtHntpoffypo ffuftMuyo C
    06o3He "ffvt
    iftffjf
    ... peat
    Jmore
    / ptfteaHa m
    .. "SOLONA fi" .2 9710 process may take extra time, h or less, at 800 ° C for about 1 final recovery. Combustion of biofuels depends on the process scheme. Carrying out the process with a single fluidized bed at 300 with simultaneous supply of heat Xa by partial oxidation) Tpe6yet for the preliminary and final reduction stage of 2 tons of biofuel per 1 ton of product (recovery 90%). Most of the energy of the bit-fuel supplied in this way is contained in the outgoing gas, which leaves the system and can be used, for example, to produce energy. Processes designed to maximize the energy of the bitstream. in the system, may require; up to 0.5 tons of bit fuel for 1 product. The process can also be carried out in other types of reactors.
    06know / e and:
    --i- ffrof7o / 6ffrt / p0jfi / 3 CO fcfnnu / w)
    fftO / fOMf0f6 / VHHt / / rVpff / Jt / j)
     corner
    3 (.
    fr
    goG
    - w700
    TfM / tfpo / nyfta fosutpuHotfui / C
    HS
    t
    JOOO (pus.d

    % .CV: Y,: /.
    V. . , /, ",

    . - ... /
    .
    fieL
    权利要求:
    Claims (4)
    [1]
    1. METHOD FOR RESTORING IRON-CONTAINING MATERIAL in a finely dispersed state, including the stages of preheating, preliminary and final reduction with gas leaving each previous stage, characterized in that, in order to increase the recovery rate,. the final recovery stage is carried out with solid biofuels supplied together with iron-containing material.
    [2]
    2. The method according to claim 1, characterized in that the final recovery stage is carried out with iron-containing material, crushed in a ball mill to a particle size of less than 0.01 mm, at 400-600 ° C.
    [3]
    3. The method according to p. 1, or p. 2, characterized in that, at least, the stage of the final war ® formation is carried out under pressure. / notary
    Φν. " f
    The purpose of the invention is to increase the recovery rate.
    The goal is achieved in that according to the method of restoring the iron-containing material in a finely divided state, comprising the steps of · preheating, preliminary and final reduction gas discharged from the preceding one conductive reduction steps, the final reduction step is carried out in solid biofuels supplied together with the iron-containing material.
    The final recovery stage is carried out with an iron-containing howling of its formation carried out under pressure.
    As biofuels, plant biomass can be used, obtained as raw material from plantations, for example, fast-growing willow or poplar, paper and pulp waste (wood and bark) or straw, brown algae, peat, etc.
    In Fig ...... 1 presents a diagram of the method, * in Fig. 2 and 3 “graphs showing the properties of biofuels used in the implementation of the proposed method; 35 of FIG.
    [4]
    4 - a device for implementing the method.
    The process of recovering the iron-containing material such as iron ore concentrate includes nes40Skolko stages: a preheat stage, preliminary step of: Nogo recovery and final 'reduction step, these steps can be followed by the final treatment, each of the stages may involve several intermediate steps.
    At the final stage of recovery, biofuel is added, at 50 . As a result, ferrous material is reduced to ferrous iron (reduced to metallic).
    Pyrolysis produces 55 highly reactive reducing gases and a highly reactive pyrolysis residue (a substance converted to coal). The pyrolysis residue is often significantly less 10
    类似技术:
    公开号 | 公开日 | 专利标题
    US4874427A|1989-10-17|Methods for melting and refining a powdery ore containing metal oxides
    SU1012797A3|1983-04-15|Method for reducing ferrugenous material
    US4806158A|1989-02-21|Process of reducing fine-grained iron-containing material by means of solid carbonaceous reducing agents
    US7198658B2|2007-04-03|Method for producing feed material for molten metal production and method for producing molten metal
    JP4427295B2|2010-03-03|Reducing gas desulfurization method, blast furnace operating method and reducing gas utilization method
    WO2007128370A1|2007-11-15|Process and plant for producing char and fuel gas
    US20050092130A1|2005-05-05|Process and apparatus for the direct reduction of iron oxides in an electrothermal fluidized bed and resultant product
    US4897179A|1990-01-30|Method of producing reduced iron and light oil from ion ore and heavy oil
    US4202534A|1980-05-13|Method and apparatus for producing metallized iron ore
    JP3543837B2|2004-07-21|Method for directly reducing iron oxide-containing raw materials using a solid carbon-containing reducing agent
    EP0196359A2|1986-10-08|Method and apparatus for fluidized bed reduction of iron ore
    CN210916134U|2020-07-03|Iron ore coal-based hydrogen metallurgy device
    US3441480A|1969-04-29|Method for progressive heating of solid particulate materials
    CN1102215A|1995-05-03|Method for producing direct reduced iron
    RU2477755C2|2013-03-20|Method and device for preparation of reducing agent to be used during metal production, metal production process and metal production unit using above described device
    US3585023A|1971-06-15|Method and apparatus for reduction of iron ore
    US20100037729A1|2010-02-18|Blast furnace metallurgical coal substitute products and method
    US4147615A|1979-04-03|Hot sand-coal-cracking to hydrodistillate fuels
    CN210916204U|2020-07-03|Iron ore rotary kiln coal-based hydrogen metallurgy device
    US20050000162A1|2005-01-06|Method and apparatus for gasifying waste automotive tires to produce high quality solid carbon and non-condensable synthesis gas
    EA011974B1|2009-06-30|Pretreatment process an apparatus for solid lump feed material
    US3753683A|1973-08-21|Method and apparatus for carbonizing and desulfurizing coal-iron compacts
    US3615351A|1971-10-26|Direct gaseous reduction of iron oxide
    EP0377636A1|1990-07-18|Congeneration process for production of energy and iron materials, including steel
    KR101607254B1|2016-03-29|Combiner Ironmaking facilities
    同族专利:
    公开号 | 公开日
    WO1980001808A1|1980-09-04|
    BR8008767A|1981-05-26|
    SE7901867L|1980-09-02|
    SE419100B|1981-07-13|
    AU5590680A|1980-09-04|
    US4360378A|1982-11-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2014873A|1933-11-11|1935-09-17|Harry G Wildman|Process of producing sponge iron|
    US2864686A|1955-12-15|1958-12-16|United States Steel Corp|Method of treating iron oxide fines|
    FR1259048A|1960-03-11|1961-04-21|Renault|Method and device for the preparation of iron protoxide|
    GB1021474A|1961-10-26|1966-03-02|Yawata Iron & Steel Co|Method of reducing iron ores|
    SE384225B|1974-03-08|1976-04-26|Stora Kopparbergs Bergslags Ab|METHOD AND DEVICE FOR REDUCTION OF FINELY DISTRIBUTED IRON-CONTAINING MATERIAL|
    SE387366C|1974-12-12|1980-03-27|Stora Kopparbergs Bergslags Ab|SET FOR REDUCING FINALLY DISTRIBUTED METAL OXID CONTAINING MATERIAL|FR2521592B1|1982-02-12|1986-06-27|Armines|PROCESS FOR THE EXECUTION OF REDUCING REACTIONS IN METALLURGY AND PRODUCT USED|
    DE3629589C2|1986-08-30|1992-04-02|Mannesmann Ag, 4000 Duesseldorf, De|
    US5118479A|1990-08-01|1992-06-02|Iron Carbide Holdings, Limited|Process for using fluidized bed reactor|
    US5137566A|1990-08-01|1992-08-11|Iron Carbide Holdings, Limited|Process for preheating iron-containing reactor feed prior to being treated in a fluidized bed reactor|
    BR9106710A|1990-08-01|1993-08-03|Iron Carbide Holdings Ltd|METHOD FOR CONTROLLING IRON LOAD CONTAINER CONTAINING IRON TO IRON CARBIDE|
    US5869018A|1994-01-14|1999-02-09|Iron Carbide Holdings, Ltd.|Two step process for the production of iron carbide from iron oxide|
    US5690717A|1995-03-29|1997-11-25|Iron Carbide Holdings, Ltd.|Iron carbide process|
    US5804156A|1996-07-19|1998-09-08|Iron Carbide Holdings, Ltd.|Iron carbide process|
    US5810906A|1996-08-28|1998-09-22|Iron Carbide Holdings, Ltd.|Method for preheating feed materials for the production of iron carbide|
    AU750751B2|1998-03-31|2002-07-25|Iron Carbide Holdings, Ltd|Process for the production of iron carbide from iron oxide using external sources of carbon monoxide|
    US6818027B2|2003-02-06|2004-11-16|Ecoem, L.L.C.|Organically clean biomass fuel|
    US7632330B2|2006-03-13|2009-12-15|Michigan Technological University|Production of iron using environmentally-benign renewable or recycled reducing agents|
    CN107083478B|2017-05-25|2018-08-28|江苏省冶金设计院有限公司|A kind of method and system preparing metallized pellet using red mud|
    WO2021237308A1|2020-05-29|2021-12-02|Technological Resources Pty. Limited|Biomass direct reduced iron|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE7901867A|SE419100B|1979-03-01|1979-03-01|SET FOR REDUCING FINALLY DISTRIBUTED IRON OXIDE-CONTAINING MATERIAL|
    [返回顶部]