• 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 METHOD FOR RESTORING IRON ORE TO A SPONGLE IRON IN A MINE REACTOR, including the production of reducing gas by gasifying solid or liquid fuel, its subsequent forming in a mixture with steam, countercurrent gas and solid material, sequential treatment in heating, reduction and cooling zones, recirculating gas, reducing flow of gas. , cleaning of impurities and brewing reducing gas, characterized in that, in order to increase the productivity of the furnace and save fuel, the mixture of fractional products and steam is heated to 300-600 ° C and reforming is carried out in the heating zone; in this case, before being fed into the recovery zone, the gas is cleaned of carbon dioxide impurities. 2. A method according to claim 1, characterized in that a portion of the cooled reducing gas is supplied to the cooling zone. 3. A method according to claim 1, characterized in that the gas recirculated after reforming is cooled and water is removed from it. u 00 00 co
    公开号:SU1128843A3
    申请号:SU802999796
    申请日:1980-10-30
    公开日:1984-12-07
    发明作者:Федерико Прайс-Фалькон Хуан；Рамон Мартинез-Вера Энрике
    申请人:Групо Индастриал Альфа С.А (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the reduction of iron ore to sponge iron. ,
    The production of sponge iron in a conventional 15-bed vertical shaft reactor consists of two main operations: reducing the ore with: using a suitable hot gas in the reduction zone of the reactor and then cooling the sponge iron with a gaseous cooling agent in the cooling zone reactor. The reducing gas is usually gas, consisting mainly of carbon monoxide and hydrogen, in the gas. thrown into the reactor at temperatures in. within 850-1100 ° С, preferably 900-1000 ° С. Hot reducing -az can be introduced into the reactor in the lower part of the reduction zone and flow upwards through the reactor in countercurrent to the ore falling down from the top, or alternatively, hot reducing 25 gas can be introduced into the upper part of the reduction zone and It is in the same direction as the ore moving from top to bottom. In the art, it is generally known to cool the sponge iron by introducing the cooling gas at a relatively low temperature into the cooling zone of the reactor and passing the cooling gas upwards through the reactor, causing the temperature of the cooling gas to decrease and the temperature of the sponge iron to drop.
    The closest in technical f essence and the achieved result 40 to the invention is a method of reducing iron ore to iron sponge in a shaft reactor, including the production of reducing gas by gasifying solid or liquid 45 fuels, subsequent reforming in smog steam, countercurrent gases and solid material, which successively undergoes treatment in the heating, reduction and cooling zones, recirculation, cooling, purification from impurities and heating of the reducing gas. The reducing gas used in the direct reduction of iron ores is obtained from a number of sources, 55 for example by catalytic reforming of hydrocarbons and water vapor.
    Systems that use natural gas and water vapor to form a reducing gas require the use of catalytic reforming units. In known processes in which solid or liquid fuels are used to produce a reducing gas, in contrast to those in which natural gas is used, additional equipment is needed to enrich the gas so that it can be used effectively for reduction purposes.
    The aim of the invention is to increase furnace productivity and fuel economy.
    The goal is achieved in that according to the method of reducing iron ore to iron sponge in a shaft reactor, including obtaining a reducing gas by gasifying solid or liquid fuels, then reforming it in a mixture with steam, countercurrent gases and solid material, sequential processing in the zones of heating, reduction and cooling , recirculation, cooling, purification from impurities and heating of the reducing gas, the mixture of gasification products and steam is heated to 300–600 ° C, reforming is performed in the n overheating and before entering the zone is purified of carbon dioxide gas reduction of impurities.
    A portion of the cooled reducing gas is supplied to the cooling zone.
    The gas recirculated after reforming is cooled and water is removed from it.
    A characteristic feature of the proposed method is the creation of a zone inside the ceactor for reforming the reducing gas obtained in the corresponding gasification installation. Since the rate of gas diffusion into ore particles is essentially independent of temperature, but depends mainly on the concentration of hydrogen present in the reducing gas, the reducing gas must have a relatively high hydrogen content. According to the invention, the reducing gas, which can be obtained by gasifying coal with oxygen and steam, is mixed with water vapor and heated.
    The heated gas mixture is introduced into the reactor and reformed in a heating zone located in the upper part of the reactor in order to obtain a higher desired ratio between H2 and, CO. In the reforming zone, the ratio between Nl and CO, which usually ranges from about 0.5: 1 to 1: 1, increases to an acceptable value for reduction of iron ore, i.e. ranging from about 2.5: 1 to 5: 1 using the reaction of water vapor and carbon monoxide.
    The iron containing material in the reactor acts as a particularly effective catalyst for this reaction. The gas coming out from the gasification plant of liquid fossil fuel contains,%: H 6.1 | CO 46.9, 20 CO2 4.3, N2 1.4 i CH 0.4, 0.9.
    The gas from the gasification unit of solid fuel contains, vol.%: H2 30.45 CO 58.3-, COj 10.0; Nj 1.0, CH 0.0, HjO 0.3., 25
    A higher ratio between H-l and CO is desirable due to the fact that the rate of reduction reaction with the use of hydrogen is higher compared to the reaction of Q-days with the use of carbon monoxide, due to which the ore residence time is reduced reactor. In addition, since more CO. It tends to precipitate elemental carbon on the ore; an increased amount of hydrogen minimizes this precipitation. A change in CO content also provides better control. carburizing .4Q
    The reformed gas obtained in the upper part of the reactor is removed from the reactor reforming zone into the external circuit, where it is cooled, compressed with t and sent through the absorption pad 45 to remove carbon dioxide. The reformed and treated gas is then sent to a preheater, into the cathore it is heated to an elevated temperature in the range of about 750-50, after which it is introduced into the reducing zone as a reducing gas. The reducing gas passes through the reducing zone of the reactor in contact with the metal ore, due to which the ore is reduced, after which it is removed from the reducing
    zones and cooled to remove water from it. The cooling reducing gas is then combined with the flow of the reformed and treated gas to be returned to the reduction zone of the reactor.
    According to the proposed recovery gas obtained in the gasification system of the fuel, it can be used more efficiently and economically for the reduction of metal ores. In this case, the reducing gas is reformed inside the reactor, as a result of which the need for separate reforming units or a reactor is limited, which leads to energy savings and capital costs.
    FIG. 1 shows the sponge iron plant in FIG. 2 is a process flow diagram of the production of sponge iron.
    The vertical moving bed reactor 1 contains a reforming zone 2 in its upper part, a cooling zone 3 in the lower part, and a reducing zone 4 located between the cooling reforming zones. The reactor 1 is insulated from the outside and inside. It is lined with a refractory material by a known method.
    The crushed ore is processed and introduced into the reactor 1 through the charging nozzle 5. The ore loaded into the reactor can be in the form of either pieces of prepared granules or in the form of their mixtures. Near the lower part of the reforming zone 2, the reactor is equipped with an annular injection chamber 6, which passes around the outer circumference of the reactor, so as to provide here a device with which the heated gas mixture of reducing rk3a and water vapor is introduced into the reactor. The vertical partition 7 together with the wall of the reactor limits the annular space 6. The ore moves down through the reforming zone, where it is heated and partially restored due to the vertically rising reformed gas.
    The iron ore coming out of the reforming zone and entering the reduction zone 4 mainly consists of iron oxide. Near the hearth of the reducing zone 4 there is a second annular injection chamber 8, similar to the injection chamber 6, through which the reformed and treated reducing gas can be introduced into the reactor. A truncated cone-shaped partition 9 is also provided, which, together with the reactor wall, bounds the annular space 8. As a result of the reduction achieved in the reduction zone, the ore coming out of this zone and entering the cooling zone 3 is highly metallized and has a low carbon content. Near the bottom of the cooling zone 3 there is another annular injection chamber 10 through which, if desired, a substantially inert cooling gas can be introduced into the reactor. A truncated cone-shaped partition 11 is also provided, similar to partitions 12 and 9. As the gear iron moves down through the cooling zone 3, it is cooled by the cooling gas passing through it and exits through the outlet of the reactor 13. The reducing gas is obtained in unit 14 gasification and coal, and feed through conduit 15 at a rate regulated by flow regulator 16 into conduit 17. Water vapor passing through conduit 18 and regulated by flow regulator 1-9 is mixed with gas from gasifier 14 coal days and sent to the pipeline 20. The gaseous mixture enters through the pipeline 20 into the heating serpent Evik 21 of the preheater 22, where it is heated to a temperature within the range of 300-600 ° C. pressure chamber 6. Gas passing through pressure chamber 6 enters the reactor near the reforming zone 2. By entering the reactor reforming zone, the heated mixture is reformed to obtain a higher and more desirable ratio between hydrogen and carbon monoxide. The reformed gas rises up through the reforming zone and is discharged near the upper bottom of the reactor through the outlet 24 and pipe 25. Part of the reducing gas produced in the coal gasification unit 14 is introduced at a low temperature into the cooling zone of the reactor to cool sponge iron. However, if a low carbon content in the sponge iron is required, a practically inert gas from a suitable source can be used as the cooling gas. If all or part of the cooling gas supplied to the cooling zone of the reactor is supplied from the coal gasification system, in this case, part of the cooling gas leaving the cooling zone of the reactor can also be sent to the reduction loop. The reformed gas leaving the reactor through line 25 enters the mixing cooler 26, into which water is introduced through line 27 to cool and remove water from it. The gas exits the cooler 26 through the pipeline 28 and enters the pipeline 29 which is connected to the suction side of the pump 30. A part of the gas flow passing through the pipeline 28 can be directed through the pipeline 31 to the desired location of use (not shown). Pipeline 31 is provided with a back pressure regulator 32 having a control valve 33 so that it can be adjusted to maintain the required positive and constant pressure in the system in order to increase the efficiency of reactor 1. The gas mixture entering pump 30 is directed through line 34, and it enters the absorber 35 carbon dioxide (absorber). The carbon dioxide in the stream entering the absorber 33 is removed by a method known in the art — by appropriately absorbing the medium introduced into the absorber 35 via conduit 36. In the gas exiting the absorber through conduit 37, only small amounts of carbon dioxide are contained. The gas flowing through the pipeline 37 enters the pipeline 38 and flows through the pipeline 39 into the heating coil 40 of the preheater 41. Where it is heated in the preheater 41 to a temperature in the range of 850-1000 s and preferably in the range of 850-900 ° C. The preheated gas leaves the preheater 41 and is directed through conduit 42 to the injection chamber 8, through which it enters the reactor near the hearth of the reducing zone 4.
    The reducing gas passes from the bottom up through the reduction zone and enters the injection chamber 43, through which it enters the reactor. The flow of reducing gas s leaves the reactor through conduit 44 and is directed to a mixing cooler 45, into which water is introduced through conduit 46 in order to cool and increase the efficiency 10 of removing the flow from the reformed gas. The gas leaves the refrigerator 45 through the pipeline 47, and part of it enters through the pipeline 48 to the suction side of the pump 49. Part of the gas, 15 flowing through the pipeline 47, enters through the pipeline 50 To the destination. Pipeline 50 is provided with a counter-pressure regulator 51 having an adjustable fixed position 20 so that it can be adjusted to maintain the required positive and constant pressure in the system in order to increase the efficiency of the reactor 1.25
    The gas is pumped by pump 49 into the discharge pipe 52 and mixed with the reformed gas exiting the carbon dioxide absorber through pipeline 37. The combined gas stream then passes through pipelines 38 and 39, through heater 41 and pipe 42, from which it returns to the lower part of the recovery zone 4. 35
    An inert additive gas, preferably nitrogen, can be supplied from a suitable source. (Not shown) via pipeline 53 in an amount controlled by flow regulator 54
    The inert gas passing through conduit 53 then enters via conduit 55 into the injection chamber 10 and into the reactor near the bottom of the cooling zone 3. Immersing the shape of a truncated cone, partition 11 along with the wall of the reactor, limits the annular compartment 10. Additional the inert gas passes from the bottom upwards through the cooling zone 3 of the reactor and is led out through the - 50 annular chamber 56. The outgoing cooling gas passes through conduit 57 to the mixing cooler 58, to which conduit 59 is fed
    water to cool and remove water from the waste gas. The gas leaves the cooler 58 through conduit 60 and enters s duct 61, which is connected to the suction side of pump 62. Part of the gas flow through conduit 60 can flow through conduit 63 to the place of use (not shown). Pipeline 63 is also provided with a backpressure regulator 64 having an adjustable mounting position so that it can be adjusted to maintain the desired positive and constant pressure in the system in order to increase the efficiency of the reactor 1.
    The gas is then supplied by pump 62 through conduit 65, where it can be displaced with additional inert gas passing through conduit 53 embedded into conduit 66. This gas flow is then returned through conduit 55 and through the discharge chamber 10 to cooling zone 3 reactor. Alternatively, a portion of the gas flowing through conduit 65 is sent to a reducing circuit through conduit 67 in an amount controlled by flow controller 68 and mixed with the reformed and treated gas passing through conduit 38.
    Part of the gas from the gasification unit 14 — the angle can be directed through the pipeline 69 in an amount controlled by the flow controller 70. This hectare then flows through conduit 55 into the discharge chamber 10 to the lower one. part of the cooling zone 3.
    In tab. 1, examples 1-3 show the material balance of the process carried out at three different temperatures T (at the entrance to the upper zone of the reactor, where CO interacts with water.
    in the three examples, all conditions are kept constant, with the exception of temperature T. Comparison of examples shown in table 2.
    As can be seen from the table. 2, the decrease in temperature T. improves metallization and reduces the amount of exhaust gas, but increases the amount of C02 to be absorbed.
    Table 1
    Tl

    gazifietoti
    权利要求:
    Claims (3)
    [1]
    METHOD FOR RESTORING IRON ORE TO SPONTANE IRON IN A SHAFT REACTOR, including obtaining reducing gas by gasification of solid or liquid fuel, its subsequent reforming in a mixture with steam, backflow of gases and solid material, sequential processing in heating, recovery and cooling zones, recirculation cooling, purification from impurities and maturation of the reducing gas, characterized in that, in order to increase the productivity of the furnace and save fuel, the mixture of gasification * products and steam is heated to 300-600 C and carry out reforming in the heating zone, while before applying to the recovery zone, the gas is cleaned of carbon dioxide impurities.
    [2]
    2. The method of pop. ^ characterized in that part of the cooled reducing gas is supplied to the cooling zone.
    [3]
    3. The method of pop. 1, characterized in that the gas recirculated after reforming is cooled and water is removed from it.
    1 1128843 2
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    同族专利:
    公开号 | 公开日
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    引用文献:
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    US4536213A|1984-09-10|1985-08-20|Mildrex International, B.V.|Reforming of higher hydrocarbons for metal oxide reduction|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/089,902|US4246024A|1979-10-31|1979-10-31|Method for the gaseous reduction of metal ores using reducing gas produced by gasification of solid or liquid fossil fuels|
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