• 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 process for producing pig iron from iron ore concentrate, at which in a reactor vessel iron ore concentrate, coal, oxygen gas and slag formers are injected beneath the surface of a molten iron bath. According to the invention, the ratio CO2/CO in the waste gas (11) from the reactor (2) is caused to increase to a value higher than corresponding to the condition of equilibrium at atmospheric pressure. Hereby a greater heat development is caused to take place in the bath for a certain coal amount. The injected amount of coal in relation to injected amount of concentrate is predetermined to be sufficient for finally reducing pre-reduced iron ore concentrate (4) in the reactor (2). According to the invention, CO and H2 in the waste gas is passed to a pre-reduction step (1), where unreduced iron ore concentrate is pre-reduced and thereafter can be injected into the reactor. According to a preferred embodiment, the reactor (2) is pressurized to cause the CO2/CO ratio to increase.
    公开号:SU1429940A3
    申请号:SU843816613
    申请日:1984-11-01
    公开日:1988-10-07
    发明作者:Аксельссон Карл-Леннарт；Торссел Кристер
    申请人:Ипс Интерпроджект Сервис Аб (Фирма)；
    IPC主号:
    专利说明:


    SP
    The invention relates to a process for the manufacture of iron, more specifically, but for a process for the production of iron in which a reactor is used, where reagents are injected below the level of the surface of the molten bath.
    The aim of the invention is to increase productivity and save coal.
    FIG. 1 is a flow chart of the implementation of the proposed method; in fig. 2 shows a diagram of the dependence of fractions 02, CO and CO on the level of a bath and pressure.
    I The method is carried out in the following manner. .
    I Stage 1 pre-recovery may contain a two-stage or three-stage fluidized bed, to which I continuously feeds the concentrate ore in the form of concentrate or microgranules, which must be preheated, for example, up to 250 C in the device Preheating. The requirements for material loading are made of mixing it with coal or coke. As the gas exits from stage 1 of the pre-reduction, a certain part of the gas containing CO-CO - -H ,, must be cleared of dust in cyclones and recycled to the preheating device. The remaining part of the exhaust gases is recycled through the gas treatment unit 3 to the pre-reduction stage 1. The pre-reduced iron ore concentrate passes through a possible path through the pre-accumulation unit to stage 2 of the final recovery.
    When a shaft furnace is used as a pre-reduction stage, a preliminary heating device is not required.
    Stage 2 of the final reduction contains a ceramic-lined reactor containing a bath of carbon-containing iron with a carbon content exceeding 1% at temperatures of 1400-1550 ° C. In the reactor serves pre-recovered concentrate of iron ore 4, coal 5, gaseous oxygen 6 and a substance that creates slag 7 (for example, Cao). In addition, a chiller is supplied if necessary.
    0
    five
    0 5 Q Q

    five
    0
    five
    8, which may be, for example, water. These materials are preferably fed to the reactor through injection nozzles at the bottom of the reactor, i.e. below the surface of the iron bath. The pre-reduced iron concentrate, however, can be fed through injection nozzles above the surface of the bath or through the donkey line.
    The pig iron 9 and the slag O formed in stage 2 of the final reduction can be removed continuously or periodically by conventional methods.
    The exhaust gas 11, formed in stage 2 of the final reduction, passes to the gas treatment unit 3, where the gas is partially cleaned of CO by washing AND, and partially cooled by generating steam 12 of the feed water 13 and partially cleaned of dust. CO, washed and cooled, is released freely into the atmosphere 14
    The gas treatment unit 3 also includes heat exchangers to increase the temperature of the gas after it has been cooled in connection with washing with CO and dust extraction.
    The reducing gas 15 leaving the treatment unit 3 mainly contains CO and N. The gas 15 rushes to the - stage. 1 of pre-reduction, on which it is oxidized so that it mainly contains COj and. The exhaust gas 16 from the pre-reduction stage 1-1 returns to the gas treatment unit 3, where the remaining amount of CO is recovered and returns to the pre-reduction stage 1 as a reducing gas 15.
    In unit 3 for treating gas, the exhaust gas of 1 G from the reactor was dust free. Dust 17 is injected into the reactor in step 2 of the final reduction.
    When the CO content in the exhaust gas P is relatively high, the exhaust gas 11 can be directed directly from the reactor to the pre-reduction stage. While being mixed with the reducing gas 15, which passes through the preliminary recovery stage.
    It is not cleaned from CO by washing in the gas treatment unit 3.
    In the south, a cooler 18 may be provided to cool the pre-reduced iron ore concentrate 4,
    Hj-jewTCH two possibilities to increase the ratio to the value of j, which exceeds the value corresponding to the equilibrium conditionally at atmospheric pressure.
    One of these possibilities is TOMj, which creates a pressure in the reactor that exceeds atmospheric pressure to as high as 50 bar, and preferably from about 2 to about 10 bar.
    The reactor in accordance with the invention is sealed, since, if desired, it is possible to increase the mass flow through the reactor without increasing the volumetric flow. This makes it possible to create such an amount of gas that significantly exceeds the amount of gas at atmospheric pressure.
    The invention, based on the first opportunity, is based on the fact that the increased pressure affects the kinetic conditions in the iron bath in the reactor so that there is not enough time for the formation of equilibrium in accordance with the reaction
    COj + C
    . 2CO
    with the pressure reached
    Figure 2 shows the oxygen fraction, 00.2 k CO, as a function of bath level and pressure. Chart can
    Level vank; and pressure should be chosen by the specialist from the appropriate terms, as seen only as a matter of principle, since the fractions determine the reactor volume, injection rate, capacity of the reactor and the required oxygen injected into the exhaust gas — honest CO in the exhaust gas for
    the subsequent pre-reduction stage, based on the requirements from the bottom of the reactor. The oxygen potential is high and the oxygen gas oxidizes the coal in the bath to CO. During the residence of the gas in the reactor, CO is reduced by coal in the bath to the SO reaction (1), Reaction
    H O-g. CO. + H2- (2)
    Determines the ratio, When the gas leaves the bath, before equilibrium is reached, the generated heat of combustion is used for recovery. The increased pressure leads, as can be seen from the short-circuit diagram, to the fact that the amount of CO. in relation to the amount of CO, t. is magnified when the level of the bath is above about 0.4 m.
    50
    55
    Stems max to reduce the cost of the process.
    Increasing the ratio in the exhaust gas by sealing the reactor results in more heat being generated in the bath for a certain amount of coal supplied when the C-s- + Oj-C02 reaction is highly exothermic. Relatively less visible amount of coal, thus, with an increase in pressure will create sufficient heat resistance for recovery, h of pre-reduced iron concentrate
    ten
    15


    about

    9940
    These lines show the values of the fractions obtained for the kinetic conditions arising under atmospheric pressure. The dashed lines show the corresponding fractions at an elevated pressure of 10 bar. The higher the pressure and rate of injection, the stronger the kinetic effect.
    Thus, with the help of the reactor sealing it is possible to ensure such CO content. relative to CO in the exhaust gas, is somewhat higher, than at at; - surfer da1 egngn. At a temperature of approximately 1.2 m and a total pressure of 10 bar, an exhaust gas is created with a ratio of approximately г S UEC can be seen from the figure, the level of vantage can be chosen so that the ratio can be significantly higher or substantially lower.
    The total pressure B of the reactor is set, according to the pre-naraeMONry method, by means of an appropriate pressure control device so as to establish the ratio in the exhaust gas at a predetermined required level,
    The metal bank level is established by introducing an appropriate amount of material that is injected and discharged from the reactor in a suitable manner so as to set the ratio in the exhaust gas to a predetermined desired level,
    Level vank; and pressures must be chosen by a hastily expert from the corresponding conditions, for example,
    thirty
    35
    DO P keobhodr south volume of the reactor, the capacity of the reactor and the required number of 45
    50
    55
    Stems max to reduce the cost of the process.
    Increasing the ratio in the exhaust gas by sealing the reactor results in more heat being generated in the bath for a certain amount of coal supplied when the C-s- + Oj-C02 reaction is highly exothermic. A relatively smaller amount of coal, thus, with an increased pressure, will create sufficient heat cure for recovery, h of prereduced iron concentrate.
    ore, than it would be in the case of atmospheric pressure, due to the specified kinetic effect, to which, in addition, the effect of; displacement to the left of the reaction is added (O. Mixing: reaction (1) to the left at elevated pressure relative to equilibrium will be only part
    in increasing the ratio of C0, / C0 in comparison with the amount of CO in the exhaust gas
    with the described kinetic effect.
    Gaseous oxygen 19 is injected through a nozzle to the surface and used for pre-reduction. Preliminary formation suggests that the pas of the final recovery stage is achieved when the carbon-containing bath of iron is in equilibrium at atmospheric pressure. The most efficient heat generation is achieved when heat is generated in the bath, which is ensured when the final recovery stage is carried out during sealing.
    used for pre-recovery. Preliminary restoration assumes that the pas of the stage of final restoration
    in the reactor when the reactor is operating. nor is it necessary to regenerate it to atmospheric pressure. At atmospheric pressure, the ratio is very small in the exhaust gas above the bath surface in the reactor. By burning the surface of CO and CO with the help of gaseous oxygen, a large amount of heat, co-; The torus propagates from the bath surface down into the reactor bath and is used there. The ratio in exhaust gas 11 from stage 2 of final recovery is substantially higher than the corresponding equilibrium condition on the surface of the bath when atmospheric pressure prevails and oxygen gas is not added.
    thirty
    Pour only pre-reduced iron ore concentrate.
    The invention is driven as a result
    20 to low coal consumption, low gas and dust relative to the amount of pig iron produced as compared to known processes using a reactor.
    25 The invention may be modified in various ways based on the particular design of the various components used, and it may also vary and vary.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The ratio is necessary, based on the amount of CO required for stage 1 of the preliminary recovery. The amount of CO must match or. only slightly exceed the amount required to pre-reduce unreduced iron ore concentrate. In determining this amount, it is necessary to take into account the amount of hydrogen gas in the exhaust gas, since hydrogen is also a reducing gas.
    The basic idea of the invention is to create a sufficient amount of heat in the final reduction stage to melt and recover the pre-reduced iron ore concentrate. Low coal consumption is provided by a greater degree of combustion of the effluent gas from the final reduction stage than
    thirty
    Pour only pre-reduced iron ore concentrate.
    The invention is driven as a result
    20 to low coal consumption, low amounts of gas and dust relative to the amount of pig iron produced as compared to known processes using a reactor.
    25 The invention may be modified in various ways based on the particular design of the various components used, and it may also vary and vary.
    Invention Formula
    . The method of producing pig iron from iron ore concentrate, which injects prereduced iron ore concentrate and coal into the reactor from above, and slag formation and oxygen gas under the surface of the molten iron bath in the reactor, increasing the CO / CO ratio to the waste gas inside the reactor to 0, 05–3.0, exceeding the ratio corresponding to the equilibrium state between the carbon in the bath and the ratio of C02 / CO on the surface of the bath at atmospheric pressure; cleaning the exhaust gas about CO and supply of purified gas containing CO and H to the pre-reduction stage, characterized in that, in order to increase productivity and save coal, the ratio is increased by setting the total pressure in the reactor above 55 bar and reaching 50 bar preferably 2-10 bar.
    35
    40
    45
    50
    I
    1.5
    I 1. f.o
     - iBapo f,
    ten
    O.CH fjjaiftfUi) (ffUQ.i
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    同族专利:
    公开号 | 公开日
    AU571209B2|1988-04-14|
    AT42766T|1989-05-15|
    EP0122239A3|1986-12-30|
    PL146762B1|1989-03-31|
    JPH0414162B2|1992-03-12|
    BR8405819A|1985-02-20|
    AU2651184A|1984-09-28|
    US4591381A|1986-05-27|
    SE435732B|1984-10-15|
    JPS60500722A|1985-05-16|
    PL246490A1|1984-10-08|
    EP0122239B1|1989-05-03|
    SE8301159L|1984-09-03|
    WO1984003521A1|1984-09-13|
    DE3478034D1|1989-06-08|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3936296A|1970-02-25|1976-02-03|Campbell Donald L|Integrated fluidized reduction and melting of iron ores|
    DE2401909C3|1974-01-16|1985-06-27|Fried. Krupp Gmbh, 4300 Essen|Process for the production of steel|
    IT1038230B|1974-05-22|1979-11-20|Krupp Gmbh|PROCEDURE FOR THE PRODUCTION OF STEEL|
    DE2520938C3|1975-05-10|1980-03-06|Eisenwerk-Gesellschaft Maximilianshuette Mbh, 8458 Sulzbach-Rosenberg|Process for the continuous production of a reducing gas consisting essentially of carbon monoxide and hydrogen|
    DE2713864A1|1977-03-29|1978-10-05|Wijk O|Prodn. of clean gas contg. hydrogen and carbon mon:oxide - by gasification of coal in metal melt|
    US4238226A|1979-07-16|1980-12-09|Midrex Corporation|Method for producing molten iron by submerged combustion|
    LU82227A1|1980-03-05|1981-10-30|Arbed|METHOD AND DEVICE FOR PRODUCING LIQUID IRON|
    DE3024977A1|1980-07-02|1982-01-28|Klöckner-Humboldt-Deutz AG, 5000 Köln|METHOD FOR PRODUCING REACTION GAS|
    DE3031680C2|1980-08-22|1988-02-25|Kloeckner Cra Technologie Gmbh, 4100 Duisburg, De|
    US4434003A|1980-12-15|1984-02-28|Geskin Ernest S|Steel making method|
    SE426403B|1981-05-20|1983-01-17|Ips Interproject Service Ab|Carbon gasification process|
    DE3318005C2|1983-05-18|1986-02-20|Klöckner CRA Technologie GmbH, 4100 Duisburg|Process for making iron|SE458688B|1985-07-23|1989-04-24|Ips Interproject Service Ab|PROCEDURE AND ESTABLISHMENT FOR PREPARATION OF RAJAJARS FROM ANNUAL OXIDIC MATERIAL|
    JPS62167811A|1986-01-20|1987-07-24|Nippon Kokan Kk <Nkk>|Melt reduction steel making method|
    DE3629589C2|1986-08-30|1992-04-02|Mannesmann Ag, 4000 Duesseldorf, De|
    MX170052B|1987-12-07|1993-08-05|Kawasaki Heavy Ind Ltd|METHOD OF REDUCTION BY FOUNDRY OF MINES CONTAINING METAL OXIDES|
    CA2006253C|1988-12-20|1998-08-11|Rodney James Dry|Pre-reduced iron oxide|
    US5183495A|1989-12-04|1993-02-02|Nkk Corporation|Method for controlling a flow rate of gas for prereducing ore and apparatus therefor|
    AT403926B|1996-07-10|1998-06-25|Voest Alpine Ind Anlagen|METHOD FOR GENERATING A REDUCING GAS FOR THE REDUCTION OF METAL ORE, AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT403929B|1996-07-10|1998-06-25|Voest Alpine Ind Anlagen|METHOD FOR GENERATING A REDUCING GAS FOR THE REDUCTION OF METAL ORE, AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AUPO122796A0|1996-07-25|1996-08-15|McLaughlin, Darren Neville|Mac's mini spit|
    US7238222B2|2005-03-01|2007-07-03|Peterson Oren V|Thermal synthesis production of steel|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE8301159A|SE435732B|1983-03-02|1983-03-02|PROCEDURE FOR THE MANUFACTURING OF IRON|
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