• 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:
    1. A method of producing blast furnace iron and reducing gas in an exhaust gasifier, comprising loading particles of sponge iron, coal, additives, blowing oxygenated gas over a melt from above, characterized in that, in order to increase profitability, a boiling layer of coal with a height is formed in the melt gasifier, 5 m, the temperature of which in the lower zone is maintained in the range of 2000-2500 0, and the temperature in the upper zone is in the range of 1000-1400 C, while the temperature of the particles of the supplied iron is maintained at 500-950 ° C. 2. Method POP.1, which differs from I in that the temperature of the purged oxygen or oxygen-containing gas is maintained at 200-8.00 ° C. 3. The method according to Claim 1, which differs ;, u and u with this, that gas is blown out of nozzles located along the perimeter of the gasifier, so that the speed of the rising flow, referred to the normal state, is less than O, 4 m / s. 4. A device for producing blast iron and reducing gas in a melt gasifier containing a melt gasifier in the form of a vessel lined with heat-resistant material (L material, with openings for supplying coal and sponge iron, reducing gas, slag and iron, nodes in the form of nozzles for introducing oxygen-containing gas, characterized in that, in order to increase profitability, the section between the melting furnace and the gasification devices of Gas5 from the boiler is made in the form of a cylinder with an extended upper part New, and nodes in the form of nozzles for introducing oxygen-containing cm of the holding gas are located in its lower part along the perimeter and / nli at different heights. 5. The device according to Claim 1, which is equipped with at least one lance for blowing in water vapor and / or hydrocarbons.
    公开号:SU1169995A1
    申请号:SU792822601
    申请日:1979-10-03
    公开日:1985-07-30
    发明作者:Вебер Ральф；Эльснер Эмиль；Машланка Вальтер；Роллингер Бернт；Зандерс Герхард
    申请人:Корф-Шталь Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to a method for producing a pig iron and a reducing gas in a production of a melt gasifier.
    The problem was solved by known methods, on the one hand, to create a high temperature in the melt gasifier for melting the sponge iron, and, on the other hand, to obtain an economically high quality reducing gas.
    The closest in technical essence and the achieved result is a method for producing blast iron and reducing gas in a melt gasifier, including loading from above sponge-iron particles, coal and, if necessary, additives, blowing oxygen-containing gas over the melt and a device for carrying out the method containing melt gasifier in the form of a vessel lined with a heat-resistant material with holes for the supply of coal and sponge iron, the output of reducing gas, the release of slag and iron, knots to enter the oxygen-containing gas.
    The gas leaving the smelting vessel in a special reforming zone in which excess fuel is combusted with oxygen is subjected to an enrichment treatment. Granular or powdered coal is supplied to the burners and technical oxygen is preferably used as the oxygen-containing gas. Since there is an oxidizing atmosphere in the melting vessel to create the required melting temperature, for the protection of the molten iron from re-oxidation and to improve the recovery, sponge iron is mixed in with the supplied sponge or coal is separately introduced into the melting vessel. Additional carbon is absorbed by the liquid slag and the liquid metal and, under the influence of the high temperature in the melting vessel, contributes to the further reduction of the iron oxide, while simultaneously the molten iron is protected from reverse oxidation.
    The disadvantage is that only burners can be used for burners; pretreated granular or powdered coal and pretreatment causes high costs, and the sponge iron particles loaded into the melting vessel, while they fall into the melt zone, fall into the oxidizing atmosphere, in which small sponge iron particles are completely oxidized, so that the method is suitable only for processing lump sponge iron. A special reforming zone is required to enrich the reducing gas.
    The aim of the invention is to increase profitability.
    The goal is achieved by the method of producing blast furnace iron and reducing gas in the melt gas, including loading sponge iron particles, coal, additives, and blowing oxygen over the melt, forming a boiling bed of carbon with a height of 1.53, 5 in the melt gasifier. m, whose temperature in the lower zone is maintained in the range of 20002500 C, and the temperature in the upper zones in the range of 1000-1400 C, while the temperature of the particles of iron supplied is maintained at 500-950 C.
    The temperature of the purged oxygen or oxygen-containing gas is maintained at 200-800s.
    Gas is blown from nozzles located along the perimeter of the gasifier so that the speed of the rising flow, referred to the normal state, is less than 0.4 m / s.
    In a device for producing blast furnace iron and reducing gas in a melt gasifier containing a melt gasifier in the form of a vessel lined with heat-resistant material, and openings for supplying coal and sponge iron, gas for reducing gas, slag and iron, nodes in the form of nozzles for oxygen-containing gas, the area between the smelter and the gasifier's charging devices is made in the form of a cylinder with an expanded upper part, and the nodes in the form of nozzles for introducing oxygen-containing gas are located s in its lower part around the perimeter and / or at different heights.
    The device is equipped with at least one lance for blowing in water vapor and / or hydrocarbons.
    The invention is based on the fact that with the aid of a hot fluidized bed
    a coal of sufficient height in the melting vessel not only can be reached in the lower region of the fluidized bed, the temperature is between 2000 and sufficient for molten iron, even lumpy spongy iron, and that this boiling coal layer retards the lumpy spongy iron so that the residence time in the fluidized bed is sufficient for the coal in the order of several seconds in order to heat it in the heat exchange with the fluidized bed of coal by several hundred degrees, as a result of which it is possible to melt very quickly s highly inhibited and thus the slag suspended in the sponge iron. Fine-grained sponge iron in a fluidized bed of coal for such a long time that it is already melted or heated to the necessary extent. Particularly favorable conditions are created if the sponge iron is supplied already heated, for example, at a temperature of 750 ° C, directly from the reduction unit. To create a very high temperature in the hot zone, preheated oxygen is blown into it, i.e. oxygen, which is preheated, for example, up to 350-450 C., an excess amount of carbon particles from the neighboring area of the fluidized bed of coal is drawn into this oxygen flow. This results in a highly radiating flame that provides good heat transfer to the molten sponge gland. Due to various endothermic reactions, the temperature of the fluidized bed of carbon
    decreases from the high temperature zone up to a value between 1000 and 1400 ° C, so that the reducing gas leaves the vessel to melt at about that temperature. The temperature and composition of the reducing gas can also be controlled by injecting water vapor or hydrocarbons approximately in the middle of the height of the fluidized bed of coal. These temperature conditions make it possible to immediately coke the supplied coal, with larger pieces of coal falling apart, so that even when using unclassified coal with a particle size of 12 mm, a fluidized bed is formed, in which
    The coke particle size generally lies between 2 and 3 mm. If coke breeze or lignite is used, then the size of the particles must be chosen in such a way that the required boiling coal layer is obtained. The mode of carrying out the process ensures complete cracking of heavy hydrocarbons and guarantees, with a sufficient height of the fluidized bed, between 1.5 and 2.5 m, the composition ha: a, whose share of CO and H is more than 85%. Thus, without additional enrichment, a high-quality reducing gas is obtained and cheap coal can be used without costly preliminary preparation. To cool the fluid bed of coal, fine ore can also be added, which takes part in fluidization, is reduced and melted in a fluid bed of coal. If thin ore of non-ferrous metals is added, it can thus be used to alloy the melt.
    The resulting high-quality reducing gas can be used as a reducing gas in such a reduction unit as a direct reduction shaft furnace. However, it can also be fed to the blast furnace in order to replace high-quality coke with a reducing gas in the blast furnace process. Thus, one kilogram of coke can be replaced by 3-4 nm CO / H.
    0
    at 1000 C. Thus, up to 20% of coke can be replaced by reducing gas. The reducing gas can also be used for other purposes.
    FIG. 1 is melting
    gasifier for carrying out the method; in fig. Figure 2 shows schematically the use of a melt gasifier in the process of producing blast iron from iron ore.
    The melt gasifier 1 has a lower section 2, in which there is a blast furnace and slag, a middle section 3 for a fluidized bed, coal and an extended upper section 4. Compared with practical experiments of a melt gasifier, the average section 3 provided for a fluidized bed It is 2.5 m and the height of the upper section is from 4 to 3 m. The inner diameter in the middle and lower regions is 3.2 m. For the production of blast-iron on and slag in the region of the lower section 2, holes 5 and 6 are provided for blowing oxygen gas pipes and nozzles 7 (of which only one is shown above the slag mirror) and for injecting water vapor or hydrocarbons the pipes and nozzles 8 are approximately in the middle of the height of section 3. In this example, hole 9 , for supplying sponge iron, as well as for removing gas reducing hole 10. Sponge iron particles are supplied in the middle section 3 of the melt gasifier, where a boiling bed of coal is formed with a high temperature zone 12 in the lower part adjacent to the bed and 13, a fluidized bed region yi- l. Here, the temperature varies between 2000 and 2500 ° C. The temperatures of the fluidized bed of coal decrease upwards from the high temperature zone and in the upper region of the fluidized bed of coal, to which space 14 is added to calm, reach values between 1000 and 1400 ° C. Through the opening 9, coal is continuously supplied, which then flows through the space to calm the boiling coal. Coal can be supplied with lumps of up to 12 mm or more, since larger pieces of coal due to the high temperatures strike gas and remove them. Therefore, coke particles of 2 and 3 mm in size and of a specified temperature are present in the coal bed. For blown through the nozzles 7 (if possible preheated to temperatures between 350 and 450 ° C) -oxygen, the coke particles in excess in the gasifier are heated, there are an excess of heated coke particles, due to which highly radiating flames of a given temperature are obtained, which favor the melting of spongy iron. The supply of oxygen in practical experiments was carried out at a speed of 20-40 m / s. The rate of raising the coal of the gas carrier in the fluidized bed, taking into account the smallest possible carryover of coal, could be maintained below 25 cm / s. The sponge iron introduced through the opening 10 noticeably slows down in the fluidized bed of coal and, before entering into the high temperature zone 12, is heated not several hundred degrees. The speed then drops so much that the slag layer no longer breaks through, and the sponge iron floats on the slag and quickly melts in the region of very high temperatures on the surface of the slag layer or inside it. With a height of the fluidized bed of coal 11 and. spaces 14 for comfort respectively. 2 m; the height of the slag layer is 0.3 m; the temperature in the high temperature zone 12 is 2200 s and in the upper region of the fluidized bed 11 coal 1200 s, i.e. with an average temperature of the fluidized bed of coal 1700 ° C, an average diameter of coal particles of 3 mm forming the fluidized bed and an average diameter of sponge iron particles of 10 mm, which are added with a temperature of 750 ° C, they fall almost unchecked for less than 1 second through space 14 for comfort, whereby their temperature only increases slightly, and the fall rate increases from 0 to 6 m / s. Sponge iron particles are braked in a hot fluidized bed of 11 coal from 6 m / s to 0.6 m / s, due to which the residence time here rises to about 3 seconds. At the same time, the sponge iron particles are heated from 750 ° C to 1000 ° C by heat exchange with a boiling bed of coal. They fall at a reduced rate on the slag layer, which has a temperature of about 1700 ° C and in a very short time is melted on or in the slag layer. The braking effect and the desired residence time in the fluidized bed of coal are determined by the supporting pressure of the coal particles and the lifting force. The retaining pressure and lift, and thus the residence time, depend on the supplied amount of oxygen-containing gas and coal, on the ratio of these quantities with each other, as well as on the size of coke particles in the fluidized bed coal, which should not be less than the minimum size. 1 mm. The residence time along with the height of the fluidized bed of coal depends on the size of the particles of spongy iron, which should not exceed 30 mm, and on the speed of falling
    71
    particles of spongy iron when entering the fluidized bed coal. The heat exchange between the particles of sponge iron and the fluid bed of coal and the heating of particles of sponge iron in the fluidized bed of coal, along with the residence time, depend on the temperatures in the fluid bed and on the size of the particles of sponge iron. For particles larger than 3 mm, thermal radiation from the high temperature zone has a significant effect on the surface temperature. Fine-grained particles of spongy iron, for example, with a size of up to 3 mm, participate in fluidization until they, already being liquefied in the lower zones of the fluidized bed of coal, do not settle in the bath. Thus, in a melter gasifier, fine-grained sponge iron can also be melted.
    The reducing gas in the exhaust gasifier 1, which consists mainly of CO and H, and leaves the gasifier through the opening 10 with a temperature that approximately corresponds to the temperature in the upper region of the fluidized bed of coal, i.e. . Depending on the grade of coal or a mixture of different coals, the desired composition and temperature of the reducing gas coming out of the melt gasifier are obtained. Because of the Boudoir reaction, on the one hand, and the limitation of the softening point of coal ash, on the other, it is necessary to maintain a temperature of about 1200 ° C in the area of the fluid bed of coal. By injecting water vapor or hydrocarbons through the nozzles 8, the composition can be shifted to a higher H content while reducing the temperature of the boiling bed of coal.
    Oxygen nozzles located along the perimeter of the melted gasificato are predominantly directed obliquely downwards towards the molten spongy iron. Such nozzles are provided in two planes with different angles of inclination. Since the optimum setting of the nozzles varies with the height of the slag mirror, it is possible to adjust the angle of the nozzles. However, by continuously removing blast furnace and slag, it is also possible to maintain the slag mirror constantly at the same height.
    699958
    The launch of the process is possible due to the introduction of a coke frame, in which falling particles of sponge iron are trapped and then they can be melted in the high temperature zone. The nozzles 7 should not be directed towards the center of the fluidized bed of coal. They can also be located eccentrically. Thanks to this
    10, depending on the size of the melt gasifier in the middle section 3, uniform gasification can be achieved. If the diameter of this section is very large, for example, it exceeds 4 m, then along with nozzles inserted from the side, nozzles from the middle are also provided. For the production of liquid blast furnace iron from oxide iron ores above the melt gasifier 1 there is a shaft furnace 15 of direct reduction to which the reducing gas obtained in the melt gasifier is supplied, after it is in the heat exchanger
    25 16 gave some of its heat to preheated oxygen for the melt gasifier and was released in the cyclone 17 from trapped coal particles. In the reduction shaft furnace 15, the reduced iron ore enters as a sponge iron heated to about 750 ° C in the melter gasifier 1 and melts into blast furnace iron there.
     Layer height can be in
    in the range of 1.5-3.5 m. If the lower limit is not reached, oxygen can break through, and creating a height of more than 3.5 m is uneconomical.
    0 The temperature in the lower layer region, i.e. in the zone where oxygen is injected, it should be 2000-2500 ° C. If the lower limit is not reached, it becomes difficult to melt the spongy
    5 iron, and the temperature rise above 2500 C is not economically feasible.
    The temperature of 1,000-1,400 ° C is maintained in the upper part of the fluidized bed.
    0 layer In this case, if the temperature is not reached 1000 ° C, the CO content in the produced gas is increased, and the temperature lAOO is limited by the profitability of the method so that
    5 to prevent the formation of clots; when fed to a subsequent unit, the reducing gas must be supplied with a temperature of 800 C.
    91
    The temperature of the supplied sponge iron corresponds to ZOO-EZO C. Moreover, at a temperature below, subsequent melting slows down, and if exceeding 930 ° C, the formation of cakes is possible.
    With an increase in the speed reduced to normal levels above 0.4m / s, the entrainment of fines increases unacceptably.
    A gas containing oxygen can be blown into the room temperature. If it is blown at a temperature of 200 to 800 ° C, then it is possible to reduce the consumption of oxygen. Increasing the oxygen temperature below is unprofitable, and above 800 ° C those are not practically realizable .. I & M, Into the head gasifier 9 t / h of coal is fed through the opening 9, and 10 t / h of spongy iron through the opening 10, 6000 oxygen is blown in through the nozzles 7, with 1800 gas coming out through the opening 10 and 9 t / h of pig iron is formed. The gas has the following composition,%: 70 CO; 24 2 4N, Cast iron composition,%: 96 Fe; 3.2 C; 0.16 S, the rest silicon, manganese and microelement temperatures at the lower zone of 2100 ° C, respectively, in the middle part of the fluidized bed, 1600 ° C, and the temperature of the crude exhaust gas is 1100 ° C, pressure
    6999510
    3.3 atm, height of the elevated bed angle 2.3 m, height of the restful space 4 m, temperature of the sponge iron supplied, Gas flow rate was
    0.23 m / s. If, in this example, oxygen is blown with temperature, its consumption can be reduced from 6,000 to 3,300 m (normal) per hour,
    The speed of the rising, gas stream within the fluidized bed (boiling) coal layer is determined by the amount of oxygen blown in, the quality of the coal used and the cross-section of the gasifier. When using low calorific coal, a higher temperature is required to achieve the indicated temperatures in the high temperature zone (from 2000 to 20 2300 C).
    oxygen consumption than when using higher quality coal, which leads to a higher rate of uplifting gas flow, 25 However, it should be limited
    value of 40.4 m / s, referred to. normal, otherwise, the removal of particles of coal will become undesirably large. If a
    If the limitation to the value of 4 m / s is not enough, then the melting unit capacity of the melting unit should be reduced accordingly.
    // / / / / / / / // // // y /
    (HZ -.C o)
    Fiyo.1
    权利要求:
    Claims (5)
    [1]
    1. A method of producing blast furnace iron and reducing gas in a smelter gasifier, comprising loading from above particles of sponge iron, coal, additives, blowing oxygen-containing gas over the melt, characterized in that, in order to increase profitability, a boiling coal layer of height 1 is formed in the smelter gasifier, 5-3.5 m, the temperature of which in the lower zone is maintained in the range of 2000-250СГС, and the temperature in the upper zone is in the range of 1000-1400 ° С, while the temperature of the particles of supplied iron is maintained at 500-950 ° С.
    [2]
    2. The method of pop. 1, characterized in that the temperature of the purged oxygen or oxygen-containing gas is maintained equal to 200-8.00 ° C.
    [3]
    3. The method according to claim 1, characterized by the fact that the gas is injected from nozzles located around the perimeter of the gasifier so that the velocity of the rising flow, referred to the normal state, is less than 0.4 m / s.
    [4]
    4. A device for producing blast-iron and reducing gas in a melting gasifier, containing a melting gasifier in the form of a vessel lined with heat-resistant material, with openings for supplying coal and sponge iron, an outlet for reducing gas, slag and cast-iron exhaust, and nozzle assemblies for introducing oxygen-containing gas, characterized in that, in order to increase profitability,
    G169995 the section between the smelting furnace and the loading devices of the gasifier is made in the form of a cylinder with an expanded upper part, and the nodes in the form of nozzles for introducing oxygen-containing gas are located in its lower part along the perimeter and / or at different heights.
    [5]
    5. The device according to claim 1, characterized in that; that it is provided with at least one lance for. blowing water vapor and / or hydrocarbons.
    类似技术:
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    US3108869A|1963-10-29|Ore reduction furnace and method
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    同族专利:
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2843303A|DE2843303C2|1978-10-04|1978-10-04|Process and plant for the production of liquid pig iron and reducing gas in a melter gasifier|
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