• 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:
    The invention relates to a method and apparatus for the production of finely crushed solid matter for use in the production of hot briquettes without a binder from a combustible iron content. The aim of the invention is to increase the efficiency of the process. For this, the finely divided solid material, before briquetting, is blown up by an upward oxidizing heated gas stream and is kept in a fluidized bed. At the same time, the gas flow is regulated so that the material is first heated to the ignition temperature of the materials, and then, due to the oxidation of at least part of the metallic iron, the temperature of the finely divided solid material rises to 450-650 ° C. Finally, the solid material is hot briquetted. A distinctive feature of the invention is that the boiling layer, prior to the start of oxidation, part of the metallic iron is subjected to vibration. The installation contains a fluidized bed reactor, the lower part of which is made in the form of a chamber and equipped with siphon-shaped end caps, worn on the gas supply pipeline and entering the fluidized bed. The reactor is equipped with a vibrator. The chamber is made of several sections, mainly three, having individual gas supply pipelines from below. 2 sec. and 12 hp f-ly, 3 ill., 1 tab.
    公开号:SU1605927A3
    申请号:SU864027867
    申请日:1986-07-28
    公开日:1990-11-07
    发明作者:Каас Вернер；Аут Рудольф；Зайдельманн Лотар；Хеффкен Эрих
    申请人:Тиссен Шталь Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method and apparatus for the manufacture intended for use in production. water processe hot briquettes without a binder from iron-containing hot finely divided particles of the material.
    The aim of the invention is to increase the efficiency of the process.
    FIG. 1 shows an installation for hot briquetting combustible filtered pypi from a CO blower with an oxygen-blowing regeneration unit in FIG. 2 shows section A-A in FIG. 15 in FIG. 3 - installation with four cameras.
    Installation contains pipeline 1, dust bunker 2, from where the converter
    s
    for dust, a scoop conveyor 3 is fed to boiling water reactor 4. The fluidized bed reactor is stretched in length, rests on oscillatory elements in the form of springs 5, has a gas permeable bottom 6, gas supply lines 7 and a casing 8. The fluidized bed reactor 4 is brought into oscillatory motion by exciters of oscillations. Having heated to the briquetting temperature in the reactor 4, the dust from the filters through the outlet 9 is fed to the briquetting press 10, in which the dust from the filters is pressed into the briquettes. The finished briquettes are fed for cooling to the briquette cooler, which is made in the form of an endless belt 11, and the cooling of the briquettes is carried out by flowing ambient air. The heated cooling air is collected by the casing and discharged from. The cooled briquettes end up in a bunker from which they can be taken for use in a steel mill.
    To create a fluidized bed 12, the fluidized bed reactor 4 (Fig. 2) has a chamber 13, the upper wall of which forms the bottom 6 of the reactor 4, performed on permeable gas. For this purpose, gas supply pipes 14 are located in the bottom 6, which project above the fluidized bed mirror. Gas supply pipes are equipped with tips 15 in the form of siphons, which are included in the fluidized bed 12.
    The casing 8 of the fluidized bed reactor 4 has two gas discharge pipes 16 that are equipped with control valves 17. Through the exhaust pipes, the hot exhaust gases are supplied to the dust separator 18 but can also partially flow through the scoop conveyor 3 countercurrently to the supplied dust from the filters and through the connecting pipeline with adjusting flaps, lead to the dust separator 18.
    Thus, the dust from the filters in the scoop conveyor is already preheated. This is especially beneficial when processing cold, coarse filter dust.
    The particles separated from the waste gases in the dust separator 18 fall through a scoop conveyor 3 back into the fluidized bed reactor 4. Hot purified waste gases are fed through pipe 19 to heat exchanger 20. Elements 21 for heating air and inert gas are located in this heat exchanger.
    The installation has pipelines 22 and 23 and three burners 24 for generating hot combustion gases. This is done by burning natural gas in the air, which is supplied through pipes 25 and 26. Burners 24 are connected to the gas supply lines of the fluidized bed reactor 4. The gas supplying pipes 7 are further connected to the heat exchanger elements 21 of the heat exchanger 20. The chamber 13 of the reactor 4 with a bale layer is divided (Fig. 1) into three sections 28, into which the gas exhaust pipes 1 enter. The fluidized bed reactor 4 has therein, temperature measurement instruments 29, by which the temperature of the fluidized bed 12 is measured in separate areas. Measured temperatures are supplied to regulators 17, 30 and 31 in conduits 16 and 27, as well as to fans 32 in conduits 22, 23, 25, and 26, which control (regulate) the temperatures and supplied amounts of hot combustion gases, hot air and hot inert gas.
    The fluidized bed reactor 4 has installation devices with which it is possible to set the inclination of the reactor. The exciters are equipped with an installation device with which you can set the amplitude and. oscillation frequency. The fluidized bed reactor 4 may have four sections 28 (FIG. 3), the first being connected to the casing 3 of the cooling tape 11 by a pipe 34, and the other three sections are connected to the burners 24 (FIG. 1).
    Thus, it is advantageous to use the heated cooling air captured by the casing 33 to pre-heat the dust from the filters in the first part of the fluidized bed reactor.
    By supplying sensitive heat from the outside, metal is iron. The iron is brought to a temperature of fire. The addition of additional heat after the start of oxidation accelerates the process, while the effect of oscillations on the fluidized bed is set to
    channelization and finely divided particles are deliberately transported along the length of the fluidized bed. Preferably, heated air is used as the heated, oxidizing gas stream, while hot combustion gas and / or heated inert gas, preferably heated nitrogen, is supplied to the fluidized bed to supply sensitive heat to the igniting layer.
    The air and / or the inert gas is heated by hot purified exhaust gas leaving the fluidized bed by heat exchange. The heated air, the heated inert gas and the hot combustion gases are supplied to the fluidized bed reactor in at least two, preferably three or more, sections, and the quantity and temperature of the heated air, the heated inert gas and the hot combustion gases can be controlled. (regulated) independently of each other. The temperature of the fluidized bed is measured in more than one, preferably in three locations, and the temperature values are used to control (control) the amount and temperature of heated air, heated inert gas and hot combustion gases supplied to the fluidized bed. The amount of gases introduced into the fluidized bed is controlled so that the total amount of heated air, heated inert gas and hot combustion gas is kept constant.
    If the temperature measured in the fluidized bed rises above a predetermined value, the supply of hot combustion gases and, finally, the supply of heated air decrease. If, on the contrary, the temperatures measured in a fluidized bed decrease below a predetermined level, the supply of heated air increases, and finally increase the supply of hot combustion gases. The residence time of solid materials in the fluidized bed can be set by changing the fluidized bed slope or by changing outside oscillations
    : If the finely divided solid material to be processed is not. It consists entirely of combustible material; a part of finely divided solid material can be replaced by solidly crushed solid fuel. Preferably, in this case, up to 15% or up to 10% of finely divided solid material is replaced by finely divided solid fuel. As coarse solid fuel, coke dust from brown coal and / or fine coal can be used, preferably from the process of preparing flotation tanks. The solid material before entering the fluidized bed can be preheated by means of hot unpurified waste gases from the fluidized bed in countercurrent. The solid material in the first part of the fluidized layer can be preheated heated by cooling air from the briquette cooler.
    The advantage of the invention-1 is that the problems associated with the processing of fine-grained combustible solids into hot briquettes are solved, and the materials can be reduced to the temperature required for combustible briquetting in an economical way, in terms of energy consumption. In particular, combustible dusts of filtration can be recycled, which due to the long transportation route as well as intermediate storage lose the temperature Fu. Dust from filters can be used, the combustible components of which are small due to the operating modes determined by the processes in converters with oxygen blowing. The proposed method is carried out when the filter units are at the beginning of the operating mode or low temperature conditions are in force.
    The table shows the data explaining the proposed method.
    权利要求:
    Claims (14)
    [1]
    1. A method of making hot briquettes without a binder from iron-containing pyrophoric finely dispersed solid materials, B1fluid heating of finely dispersed solid material before briquetting in a fluidized bed due to the heat of heated gases up to 450-650 ° C, hot briquetting and cooling, that, in order to increase the efficiency of the process, the heating of finely divided solid
    The material is first carried out to their ignition temperature by supplying hot waste gas of an inert heated gas, mainly nitrogen, and then to the briquetting temperature by oxidizing a part of the iron-containing pyrophoric finely divided solid material while supplying rising heated air, while air is heated , hot exhaust gases and / or heated inert gas supply to at least two, mainly three, sections of the fluidized bed while keeping their total amount constant, and boiled material is subjected to vibradai.
    [2]
    2. The method according to claim 1, of which there are. that additional heat is supplied to the fluidized bed to reach the briquetting temperature up to.
    [3]
    3. Method according to claims 1 and 2, that is, in that up to 15%, preferably up to 10%, of the pyrophoric finely divided solid material is replaced by finely divided solid fuel.
    [4]
    4. The method according to claims 1 and 3, about the t of which is due to the fact that you use brown coal coke and / or fine coal coal particles as fine solid fuel: and, mainly obtained during the preparation of flotation 1plum.
    [5]
    5. The POP.1 method, characterized in that the finely divided solid material in the first zone of the fluidized bed is heated with air that leaves the cooling stage of the briquettes.
    [6]
    6, Installation for the manufacture of briquettes without a binder of iron-containing pyrophoric finely dispersed solid materials, comprising a fluidized bed reactor with gas supply pipelines from the bottom, a briquetting press located on the discharge side of the reactor, and a cooler equipped with a vibrator located under the reactor and siphon-shaped end caps mounted on the gas supply pipelines, while the lower part of the reactor is filled in the form of
    chambers, the upper part of which forms the bottom of the reactor, and the siphon-shaped caps are located above the bottom of the reactor.
    [7]
    7. Installation according to claim 6, characterized in that the chamber is made of at least two, mainly three, sections with individual gas supply lines from below.
    [8]
    8. Installation in PP.6 and 7, so that the cooler is made with an air trap casing connected by a pipeline with the first section from the loading side of the reactor.
    [9]
    9. Installation on PP. 6 and
    This means that the fluidized bed reactor is equipped with a cap with one or several, mainly two, pipelines for waste gases, on which control valves are installed.
    [10]
    10. Installing pop-ups 6-9, which is equipped with a dust separator connected to. waste gas pipelines.
    [11]
    11. Installation on PP.6-10, characterized in that it is supplied on a scoop conveyor and connecting pipe with a control valve, while separating the dust separator through a scoop conveyor and connecting pipe with a regulating valve connected to the reactor hood
    [12]
    12.Installation according to claims 6-11, which is equipped with a heat exchanger with heat exchange elements for heating air and inert and / or exhaust gas, connected by a pipe with a dust separator,
    [13]
    13. Installation according to claims 6-12, which is equipped with burners located in the gas supply pipelines from the bottom of the reactor,
    [14]
    14. Installation according to claims 6-13, characterized in that the heat exchange elements are connected by pipelines with gas supply pipelines from the bottom of the reactor.
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    Zaka 3458
    Circulation 493
    VNIIPI State Research Committee on the Committee on Inventions and Discoveries at the State Committee on Science and Technology of the USSR n: illJ: i, Moscow, Zh-35, 4/5 Raushsk nab.
    11 production and:) da gel plant Patent, Uzhgorod, st. Gagarin, 101
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