• 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. METHOD OF RESTORING CRUSHED IRON ORE TO THE SPANGE IRON, including a countercurrent of material loaded from the top of the shaft furnace with gas in the reduction, intermediate and cooling zones, recirculation, cooling and purification of waste gas in the reduction circuit, as well as reforming the water vapor mixture and methane, characterized in that, in order to reduce the cost of reforming, reforming is carried out by supplying a mixture of steam and gas preheated to 700-900 ° C to the intermediate zone, while the gas contains 20-30% methane. 2. The method according to claim 1 ,. This means that gas containing 20–30% of methane is added to the cooling zone, and the cooling gas is removed at a controlled rate. 3. Method pop, 1, characterized in that a portion of the cooled gas recirculated from the reduction circuit is added to the cooling zone. 4. A method according to claim .1, characterized in that coke oven gas is used as the methane-containing gas. . §. 5. A method according to claim 1, characterized in that a mixture of coke oven gas is introduced from the reduction circuit into the cooling zone. 6. A method according to claim 1, characterized in that sufficient gas is introduced into the cooling zone in an amount sufficient to lift the gas into. intermediate zone. 7. The method according to claim 1, distinguishing p. ten, that the ratio of the volumes of steam and methane in the feed mixture is
    公开号:SU1128842A3
    申请号:SU802996297
    申请日:1980-10-14
    公开日:1984-12-07
    发明作者:Федерико Прайс-Фалькон Хуан；Рамон Мартинез-Вера Энрике
    申请人:Ильса С.А.(Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the gaseous reduction of iron ore in a vertical shaft furnace with a moving bed in order to produce sponge iron. Gaseous reduction systems are known, including moving bed vertical shaft reactors. The reduction of ore is achieved using a reducing gas, consisting mainly of carbon monoxide and hydrogen, obtained by the talytical reforming of a mixture of natural gas and water vapor. These systems contain a vertical shaft reactor, have a reduction zone in the upper part and a cooling zone in the lower part. The boiling ore is introduced into the upper part of the reactor and passes from top to bottom, first through the reduction zone, where it is brought into contact with the heated reducing gas from the refürging furnace, and then through the cooling zone, where it is cooled with gaseous cooling agent before as derived from the bottom of the reactor. The gas leaving the reduction zone is cooled in order to remove water from it and in most cases most of the cooled waste gas is heated and returned to the reduction zone. A portion of the cooling gas withdrawn from the cooling zone is also cooled and returned to the cooling zone. At the lower end, the reactor is provided with means for regulating the cooling of the cooled sponge iron from the reactor, such as a rotary opening valve, vibrating trough, belt conveyor, or the like. The use of the sponge iron obtained in the reactor as a partial raw material for a blast furnace can increase the furnace output and reduce the furnace need for coke 1J. The closest to the invention of the technical essence and the achieved result is a method of reducing the crushed iron ore, including countercurrent material loaded from the top of the shaft furnace, with gas in the reduction zones, intermediate and in the cooling zone, recycling, cooling and purification of the exhaust gas, as well as reforming ara-methane pj-. A disadvantage of the known methods is the need to create a powerful methane reforming unit in order to produce a reducing gas. The purpose of the invention is to reduce the reforming costs. The aim is to achieve a tag that, according to the method of reducing the crushed iron ore to sponge iron, including a countercurrent of material charged from the top of the shaft furnace, with gas in the recovery, upgrading, intermediate and cooling zones, exhaust gas, cooling and purification of the waste gas, as well as The formation of a mixture of water vapor and methane, the reforming is carried out by preheating a mixture of steam and gas to 700–900 ° C in an intermediate zone, while the gas contains 20–30% methane. In this case, a gas containing 20-30% methane is added to the cooling zone, and the cooling gas is removed at a controlled rate. Moreover, a portion of the cooled gas recirculated from the reduction circuit is added to the cooling zone. In addition, coke oven gas is used as the methane-containing gas. A mixture of coke oven gas from the reduction circuit is introduced into the cooling zone. Sufficient additional gas is introduced into the cooling zone to lift the gas into the intermediate zone. The ratio of the vapor and methane volumes of the feed mixture is (1.01, 5): 1. FIG. 1 shows an installation for carrying out the method / FIG. 2 - t simplified process flow diagram. Vertical moving bed reactor 1 contains reducing zone 2, reforming zone 3 and cooling zone 4. Recoverable iron ore is loaded through the top of reactor 1 through inlet 5, and sponge iron is discharged from the bottom of reactor through outlet 6. Coke oven gas enters the PO system Pipeline 7, on which the flow regulator 8 is installed, and mixed with water vapor, is supplied by mm through line 9 with the flow regulator 10 located on it. Water vapor is introduced in sufficient quantity to react with the methane contained in the coke oven gas in order to convert it to carbon monoxide and hydrogen. . A stoichiometric amount of water vapor is used to inhibit undesired carbon deposition inside the reactor. Usually the molar ratio between water vapor and methane can be in the range of 1:11 .5: 1. A mixture of coke oven gas and water vapor enters the preheater 11, where it is heated to 700–900 0 and from there enters the pipeline to the reactor. The reactor is equipped with an internal partition 12 in the shape of a truncated cone which, with the wall of the reactor, forms an annular space 13 into which the gas mixture flows. From space 13, the gas passes around the lower i edge of the partition 12 to reforming zone 3, where it comes into contact with a layer of iron containing material descending downwards, which at this level of the reactor is substantially reduced to sponge iron. Sponge iron catalyzes the reaction between steam and methane to form carbon monoxide and hydrogen, which are active reducing agents for iron ore, and the reformed gas rises from bottom to top in the reducing zone, where it restores the incoming iron ore. To increase the efficiency of the use of the reducing gas, part of it is recycled. Thus, the gas exiting from the top of the iron-containing layer in the reactor is discharged through line 14 and passes through a mixing cooler 15, where it is cooled to remove water from the bottom. The cooled gas then flows through conduit 16 through pump 17 and through conduit 18 to preheater 19, where it is heated to 750-1000 ° C. From the preheater 19, the preheated gas flows through conduit 20 into the annular space 21 formed by the internal partition 22 and the adjacent side wall of the reactor, and from there moving around the lower edge of the partition 22 flows back into the reduction zone. 2. Thus, flax gas will be restored at station 11 2 in a closed loop, including a cooler 15, a pump 17, a superheater 19, and a reduction zone of the reactor, into which fresh reducing gas is supplied from reforming zone 3. A certain amount of recirculated reducing gas is withdrawn from the reducing gas circuit via line 23 containing the flow controller 24 is directed to the cooling circuit. Thus, the cooled gas from the pipeline 23 enters the pipeline 25 and from there to the lower part of the cooling. reactor zone. The gas flowing through the pipeline 25 enters the annular space 26 formed by the small town 27 having the shape of a truncated cone neper and the adjacent part of the reactor walls. The cooling gas then passes under the lower edge of the partition 27 and is directed upwards through a layer of spongy iron inside the cooling zone. After passing through the cooling zone, the gas enters the annular space formed by a partition shaped as a truncated cone and adjacent the side wall of the reactor, and from there it leaves the reactor through line 28 through a mixing cooler 29, where it is cooled and dehydrated. From the cooler 29, the cooled gas flows through pipelines 30 and 31: to the reception at the pump 32, from where it is discharged into the pipeline 25 and returned to the cooling zone. A portion of the circulating cooling gas is withdrawn from the cooling circuit via conduit 33, on which the flow controller 34 is installed, sent to a storage point or used as fuel. The gas can be withdrawn from line 7 via line 35, on which the flow regulator 36 is installed, and brought to line 25 in order to ensure the supply of fresh gas to the cooling circuit. The invention provides an efficient method for producing and using reformed coke oven gas while directly reducing iron ore to produce sponge iron. Sponge iron can be mixed with a layer of iron ore in a domestic furnace to increase its productivity. In addition, domain. Furnaces are usually placed in places where it is possible to use coke oven gas. Such coking gas is used as a fuel, its value in this process significantly increases due to the fact that it is used as one of the raw materials in a chemical reduction reaction. In addition, by virtue of carrying out a ka-lytic conversion of a mixture of water vapor and methane Yu within the reactor reforming zone, the need for a separate kiln for catalytic reforming is limited, and an exclusively economic stage of gas reforming is provided.
    In cases of using coke oven gas, the increased efficiency of the process is partly due to the fact that the by-product coke oven gas, which can also be used as a fuel, is used as a chemical raw material, and partly because the reforming reaction is carried out in a reducing process. reactor, and not in a separate catalytic reforming furnace 25. In addition, the proposed method facilitates combining the sponge iron plant with existing blast furnaces and coke ovens to ensure an overall increase in the productivity of the blast furnace and improve heat savings.
    In cases where reducing impurities are contained in the gas circulating through the cooling zone, it may be desirable to construct the operation of the cooling zone so as to direct part of the circulating gas ;; from bottom to top in recovery zone .40
    The compositions of the gas flow are shown in table 1,
    Example 1. The temperature at the top of the intermediate zone is equal to 850 ° C, and at the entrance to the reduction zone is 950 ° C. The reduced product has a metal level of 87% and a carbon content of 2.24%. Coke oven gas contains 25%: methane. The ratio of steam / methane is 1.2s1.50
    Example 2. The process is carried out, at T 700 ° C, the ratio of the steam volume to the volume of methane is 1.5: 1
    and gas containing 20% methane is used. The resulting product has a degree of metallization of 80.5% and a carbon content of 3.36%.
    Example 3. The method is carried out at an inlet temperature to the intermediate zone T, the ratio of the steam volume to the volume of methane is 1.0: 1, and the feed gas contains 30% methane. The resulting product has; the degree of metallization is .94.3% and the carbon content is 1.1%.
    At temperatures below 700 s, the reaction of the interaction of CH with a very low conversion rate and the equilibrium is shifted towards the formation of CH, instead of the same decomposition by 2 and CO. If the mixture of vapor and gas is heated to a temperature below 700 ° C, it is necessary to increase the amount of recycled gas to maintain an adequate high temperature to effect reduction. Comparing the F value (4096.7 NCM / To and Fe) in Example 2 with the Fj value (2120.4 NCM / To and Ffe) in Example 1 shows that the dimensions of the compressor and the heater are also doubled. product with low metallization and very high carbon content. If the mixture of steam and methane is heated to a temperature of above 900 ° C, the methane can be decomposed by pyrolysis to form soot. Soot formation can cause serious problems in the process of high pressure and uneven distribution of gases flowing through the reduction zone. Carbon black is also dangerous for heating heater tubes. Temperatures above can also cause sintering and agglomeration problems in a reduction reactor. Steam and methane are mixed with the hot reducing gas inside the reactor.
    From the examples given, the deterioration in the quality of sponge iron obtained at the boundary values of the ratio of steam and methane, equal to (1.0-1.5): 1.9, and their necessity is within the limits of claimed temperatures, is evident.

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    权利要求:
    Claims (7)
    [1]
    1. METHOD FOR RESTORING MILLED IRON ORE TO DOUBLE IRON, including a counterflow of material loaded from the top of the shaft furnace with gas in the reduction zones, the intermediate and cooling zones, recirculation, cooling and purification of the exhaust gas in the recovery loop, and reforming the water vapor mixture and methane, characterized in that, in order to reduce reforming costs, reforming is carried out by supplying a mixture of steam and gas preheated to 7OO-9OO and C into the intermediate zone, while the gas contains 20-30% methane.
    [2]
    2. The method according to p. Characterized in that a gas containing 20-30% methane is added to the cooling zone, and the cooling gas is removed at a controlled speed.
    [3]
    3. The method according to p. ^ Characterized in that a portion of the chilled gas recirculated from the reduction circuit is added to the cooling zone.
    [4]
    4. The method according to p. 1, characterized in that coke oven gas is used as the methane-containing gas.
    [5]
    5. The method of pop. 1, characterized in that a mixture of coke oven gas from the recovery circuit is introduced into the cooling zone.
    [6]
    6. The method according to π. 1, characterized in that an additional gas is introduced into the cooling zone in an amount sufficient to raise the gas c. intermediate zone.
    [7]
    7. The method according to p. 1, different skinny with. I mean that the ratio of the volumes of steam and methane in the supplied mixture is (1.0-1.5): 1.
    SU and , 1128842
    1 1128842
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    同族专利:
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    YU217980A|1983-02-28|
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    DE3036920C2|1985-08-29|
    AU6165480A|1981-04-30|
    JPS5810965B2|1983-02-28|
    SE448470B|1987-02-23|
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    IT8024244D0|1980-08-21|
    FR2467241A1|1981-04-17|
    JPS5662912A|1981-05-29|
    ES8106939A1|1981-09-16|
    YU42678B|1988-10-31|
    MX155124A|1988-01-29|
    PL227208A1|1981-06-19|
    IT1150965B|1986-12-17|
    SE8006646L|1981-04-16|
    BE885707A|1981-02-02|
    GB2063303B|1983-08-10|
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    ES495933A0|1981-09-16|
    GB2063303A|1981-06-03|
    引用文献:
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    US2547685A|1947-11-25|1951-04-03|Brassert & Co|Reduction of metallic oxides|
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    US3799521A|1973-02-01|1974-03-26|Fierro Esponja|Method and apparatus for the gaseous reduction of iron ore to sponge iron|
    US3844766A|1973-12-26|1974-10-29|Midland Ross Corp|Process for reducing iron oxide to metallic sponge iron with liquid or solid fuels|
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    US4160663A|1978-02-21|1979-07-10|Jack Hsieh|Method for the direct reduction of iron ore|MX156697A|1982-05-12|1988-09-27|Hylsa Sa|IMPROVED METHOD FOR THE DIRECT REDUCTION OF IRON MINERALS|
    US4528030A|1983-05-16|1985-07-09|Hylsa, S.A.|Method of reducing iron ore|
    US4556417A|1983-05-17|1985-12-03|Hylsa, S.A.|Process for the direct reduction of iron ores|
    US4897113A|1985-09-23|1990-01-30|Hylsa, S.A.|Direct reduction process in reactor with hot discharge|
    EP0244551B1|1986-05-07|1990-03-14|VOEST-ALPINE INDUSTRIEANLAGENBAU GESELLSCHAFT m.b.H.|Integrated metallurgical plant|
    US5069716A|1989-12-22|1991-12-03|C.V.G. Siderurgica Del Orinoco, C.A.|Process for the production of liquid steel from iron containing metal oxides|
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    CA1336359C|1987-11-02|1995-07-25|Corporacion Venezolana De Guayana |Method and apparatus for the direct reduction of iron|
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    AT505490B1|2007-06-28|2009-12-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR PRODUCING IRON SPONGE|
    CN100523228C|2007-07-31|2009-08-05|张文慧|Method and device for producing sponge iron by using reducing gas prepared from coke oven gas|
    US8496730B2|2010-05-14|2013-07-30|Midrex Technologies, Inc.|System and method for reducing iron oxide to metallic iron using coke oven gas and oxygen steelmaking furnace gas|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/084,750|US4253867A|1979-10-15|1979-10-15|Method of using a methane-containing gas for reducing iron ore|
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