• 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 inhibiting carburization of metal-bearing material in the reduction zone of a vertical shaft, moving bed reactor for the direct gaseous reduction of iron ore to sponge iron. Carburization within the reduction zone is decreased by regulating the water vapor content of the reducing gas in any of various ways, e.g., by adding water vapor in the form of steam to the reducing gas either before it enters the reduction zone, while it is within the reduction zone, or after it leaves the reduction zone or by recirculating a portion of the effluent gas from the reactor and cooling the recirculated gas to a predetermined extent.
    公开号:SU1001863A3
    申请号:SU782687102
    申请日:1978-11-16
    公开日:1983-02-28
    发明作者:Федерико Прайс-Фалькон Хуан；Рамон Мартинес-Вера Энрике；Гуерра-Гарсиа Джильберто；Вильям Маккей Патрик
    申请人:Ильса,С.А. (Фирма)；
    IPC主号:
    专利说明:

    (54) METHOD OF RESTORATION-METAL ORE
    one
    The invention relates to the gas reduction of metal ores to particles in the sponge iron in a vertical moving bed reactor, relates to a method for producing by direct gas reduction with the desired degree of carburization and can be used to process ores other than iron.
    It is known to produce a spongy glue in a vertical shaft reactor with a moving bed, usually consisting of two main operations: ore reduction in the reduction zone using a reducing gas consisting mainly of carbon monoxide and hydrogen with a temperature of about 70 ° -110 ° С, preferably 75О-95ОС; cooling the resulting sponge iron with a gas cooling medium to a temperature in the order of 20 10 -20 ° C, preferably lower than the JSR (- :.
    Carbon is deposited on the metal-bearing particles and in the reaction and in the cooling zones, and under the proper conditions
    deposited carbon | x) d can be reacted to form iron carbide ..
    Use for loading electric arc furnace sponge. iron containing iron carbide provides a number of advantages, first, such sponge iron has a lower melting point, which facilitates its melting in the steelmaking process. Secondly, carbon in the form of iron carbide is much more active than the mass of added carbon, since it is a much more effective reducing agent for the residual oxygen of sponge iron found in an electric furnace. In addition, the reaction of iron carbide the residual bivalent iron oxide in the sponge gland requires less heat than the reaction of elemental carbon with bivalent iron oxide.
    The closest in technical essence and the achieved result to the proposed one is the method of recovering dispersed metal ore, including the restoration of dispersed ore to sponge iron in a shaft furnace, including a countercurrent of hot reducing gas from carbon monoxide and hydrogen with ore in the upper part of the shaft furnace, cooling sponge iron in the lower part of the furnace; recirculation of the top gas, its cooling and dehydration 2.
    The sponge iron obtained by this method is commonly used as SOURCE iron for steel production in an electric arc furnace. Such sponge iron usually contains some date of iron oxide, for example, 10-2 Oz. Because it is not economically feasible to achieve 1OO% - oh metallization of ore in the recovery gas5 reactor. As the metallization of the iron-containing material approaches 10%, the process becomes difficult, time-consuming, and consumes beating amounts of reducing gas to remove residual oxygen from the material. Reduction of the residual bivalent iron oxide with iron carbide leads to the formation of carbon monoxide, the bubbles of which pass through the melt, providing the desired bath placement. The gas ensures the formation of a light, lazy shlak, enveloping the electrodes and reducing radiation loss of heat to the roof and walls of the furnace. Foamy slag creates an added advantage when the furnace is continuously loaded with sponge iron. The sponge iron granules preheated during a slag drop through the slag enter into the reaction even before they reach the molten bath. All this can be achieved without increasing the thermal load of the electric furnace. During operation, the gas reduction plant for the production of sponge iron with a lower than the maximum possible degree of metallization and its carburization to a level that ensures the completion of the recovery in the electric furnace and the efficient use of the high-temperature reduction ability of the furnace promises economic advantages. the inability to regulate the degree of carburization, since the excess on the corner of the fire violates the stabilization of the electric
    the first path of the furnace; 1st furnace, thereby increasing the intensity of the refractory lining of the furnace, there is a need to lengthen the refining period to ensure removal of excess carbon. In many cases, the desired level of carbon in the sponge gland is 1–3% w / w.
    The carbon content in the sponge gland must be maintained within narrow limits.
    Carburizing in the reduction zone is not easy to adjust with the required degree of accuracy, as is) and-is a valid requirement; to the reducing zone is such a regulation condition; work that is capable of providing the desired optimal level of recovery. The optimal reduction conditions usually do not coincide with the optimal carburizing conditions. To some extent, the same problem occurs in the cooling zone if cooling and carburization occur simultaneously in it. When attempting to ensure accurate regulation of carburization in the reduction system, a problem arises4, due to the fact that the degree of carburization that occurs in the reduction zone can be as high as 5, that sponge iron entering into the cooling can already contain more carbon than is required. It is known that carburizing reactions occur favorably at 5OO-700 ° C, and the carburization process tends to occur in the center of the reduction ash. The intensity of carburization in the reduction zone to a large extent depends not only on temperature, but also on the concentration of carbon monoxide in the reducing gas. Although carbon monoxide in the reduction zone is consumed, the reduction zone is often a clearly defined carbon monoxide generator. This is due to the conversion of carbon dioxide in the lower part of the reduction zone to carbon monoxide. Such a reaction is preferable in the lower part of the primary zone for two reasons: due to the relatively high temperature at this point and also due to the cathical influence exerted by the g-iron iron on the reaction. This reaction boosts carbon deposition in pe.-sy.Tij.
    reducing carbon dioxide in the gas and as a result of increasing its carbon monoxide content.
    The purpose of the invention is the regulation of the required degree of carbidization.
    The goal is achieved in that according to the method of reducing metal ore to sponge iron in a shaft furnace, in which a countercurrent of hot reducing gas from carbon monoxide and hydrogen with dispersed ore in the upper part of the shaft furnace, cooling sponge iron in the lower part of the furnace, recirculating the flue gas , its cooling and dehydration, to the hot) y1y reducing steam after entering the reactor is added in the amount of 1-20% by volume,
    A portion of steam in the amount of 1-15% is added to the top of the 1st portion of the reduction zone of the reactor with fresh reducing gas.
    Iron ore is used as metal ore.
    In the implementation of the proposed method, as a result of a decrease in the carbon monoxide content in the X-1emc in the reducing zone of the gas, the formation of elemental carbon and iron carbide indirectly decreases in the reduction zone of the reactor. The content of water vapor in the gas is regulated so as to shift the reaction course, i.e., force jj and
    known equilibrium shift reaction:. COvHj - COj Hi O
    Proper control of the water vapor content in the reducing gas can significantly reduce the formation of carbon in the reduction zone, because the carbon monoxide present in the gas stream reacts to produce carbon dioxide, rather than by reaction, leading to elemental carbon. The carbon content in the sponge gland can thus be reduced below the minimum that is required in the sponge iron product. This creates the possibility of effectively controlling and controlling the carbon content in the spongy iron in the cooling zone without the need for significant intervention in optimizing the reduction process in the recovery zone.
    The external part of the reduction circuit usually contains, in addition to the gas cooler, a circulation pump and a heater for reheating the reducing gas, and the gas flowing out of the reactor passes successively through Portyr. Water vapor can be injected.
    into the circulating gas, for example, just before the gas inlet to the reactor. It can also be introduced directly into the reactor near the top of the reduction zone. Water vapor or steam can be introduced into the enrichment flow of the reducing gas sent to the reducing gas circuit. Separate portions of water vapor can be introduced into two or more bars of the system; However
    in the case of a relatively fresh water vapor in the outgoing reducing gas, its content can be reduced by adjusting the flow of cooling water to the gas cooler.
    The addition of steam to the reducing gas inevitably leads to the dilution of the reducing components of the gas. When adding steam to the recovery area
    the relation of Ii- (“.) is essential
    decreases and, accordingly, decreases the reduction potential of the gas in a part of the reduction zone, i.e., in three points of the system where the last
    and the part of the recovery itself is responsible and where it is important to have high-quality gas.
    The introduction of steam near the top of the recovery zone, where the initial
    The addition of ore, however, creates, as a result of diluting the reducing gas with steam, a relatively small effect on the overall reduction effect. The required reaction of displacing water gas (the above equation) resulting from the addition of steam to the reducing gas is exothermic and, therefore, contributes to the heating of the incoming fresh ore. In addition, the oxide of iron at the top of the layer is a good catalyst for the reaction of the displacement of water gas and forces the reaction to proceed.
    Adding steam to the gas introduced into the reduction zone is associated with some drawbacks, however, in some cases it is advantageous, in particular, when the gas directed to the reduction zone contains significant amounts of methane, for example, in the case where for replenishing the reducing gas, the gas is a reformed gas, enriched by a meta relatively relatively easy recovery of ioM Jura with natural gas or when coke battery batteries are used for replenishment. In this case, the steam reacts with methane and additional amounts of reducing components are formed: carbon monoxide and hydrogen.
    In some cases, it has proved expedient to resort to a compromise procedure, i.e. add a little up to
    Any steam enters the reducing gas entering the reactor and a large part of the steam to the upper part of the buzzing body located in the reduction zone of the reactor.
    FIG. 1 shows a schematic of a moving bed vertical shaft reactor; in fig. 2 - a similar system, designated for the modification of the method according to the invention. The vertical shaft reactor 1 with the recovery zone in its upper part also has a cooling zone 2 in the lower part. Reactor 1 has proper thermal insulation and is lined with refractory material from the inside. The ore particles to be processed are loaded into the reactor 1 via the loading pipeline 3. The loaded ore can be lumpy or consist of pre-formed granules. The ore is lowered through the reduction zone, where it is reduced to a sponge iron with a reducing gas blown up, then passes through a cooling zone 2, in which oh; It is awaited by an upward cooling gas, and leaves the reactor through an outlet 4. The central part of the reactor has a protrusion 5, the upper end of which, together with the annular jacket 6, forms an annular chamber 7, into which a reducing gas flows through pipe 8. This device serves to distribute the reducing gas at the periphery of the reactor. The reducing gas flows upward through the reduction zone 9 and leaves the reactor through line 10. The lower oblique part of the protrusion 5 enters the distribution chamber 11, forming an inlet chamber 12 for the cooling gas, into which the cooling gas flows through line 13. KAtviepa provides the distribution of cooling gas at the periphery of the reactor. The cooling gas flows upwards through the cooling zone into the annular outlet chamber 14 for cooling gas, outlined by BHCTyitoM 5 and a truncated cone-shaped partition 15, Chamber. 14 is intended for storing the cooling gas BEsepxy of the cooling zone and directing the gas to the exhaust gas pipe 16.
    The gas destined for the reduction of the ore is supplied from a suitable source 17 of the reducing gas. Usually catalytic reforming, which provides for the reforming of a mixture of natural gas and / container to produce carbon monoxide and hydrogen. In another embodiment 15, coke oven gas used in TOM is used; the form in which it exits the furnace or after reforming. The reducing gas can also be derived from a gaseous hydrocarbon source, is a system of non-natural gas poisons, or from liquid hydrocarbons or coal. The reducing gas from source 17 flows through conduit 18 to the reducing gas circuit, i.e. to a flow controller 19 located in conduit 20 to providing a predetermined flow rate of reducing gas entering reactor 1. The reducing gas is supplied through conduit 2.0 to heater 21, where it is heated to 750-850 ° C and further along conduit 8 to reactor. The gas exiting the reactor flows through conduit 10 to the loading cooler 22 in order to condense part of the water contained in the gas and remove dust. The gas flowing out of the cooler 22 follows one of two paths. In one case it flows through the pipe 23 into which the control valve 24 is embedded, and through the back pressure regulator 25, and then blown into the atmosphere or taken to the proper storage location. as fuel. On another route, gas from cooler 22 can be recirculated through pipe 23, through pipe 26, circulating pump 27, pipe 28 from valve 29, back into pipe 20 and the reduction zone of the reactor. The bulk of the gas flowing out of the cooler is recirculated through conduit 26 of the reducing gas loop 26 and only a fraction of the gas is removed from the loop through pipe 23 for use as fuel, for storage or for blowing into the atmosphere. The reduced ore is cooled by a cooling gas in the cooling zone 2 of the reactor. The cooling gas enters the system. pipe ZO, equipped with a pressure valve and control {{yum. 51 {outcome flow. It is theoretically possible to use many cooling gases, including hydrogen, methane or other hydrocarbon gases, carbon monoxide and their mixtures, carbon dioxide or nitrogen. According to the invention, the sponge iron is exposed in the cooling zone to the desired controlled level. For this, the cooling zone must contain a significant amount of carburizing components. In some cases, it is desirable to have a cooling gas used for replenishment with the same composition as the replenishing reducing gas coming from source 32. For this purpose, the pipe 17 is connected to the pipe AOR by a pipe 33 equipped with a shut-off valve 34. Upon entering the circuit, the gas is cooled to the gas blower 35, the discharge side of which is connected to the pipe 13, containing an automatic flow rate regulator 36. The gas leaving the cooling zone through pipe 16 passes through cooler 37, where it is cooled and dehydrated. Then, through pipe 38, it is returned to the inlet of gas blower 35. The cooling gas can be released from the cooling circuit through pipe 39, in which there is a pulp stream 40. In some cases, the composition of the cooling gas is such that it is advantageous to direct it to the reducing gas circuit. For this purpose, the pipe 39 is connected to the transfer pipe 41, equipped with a shut-off valve 42 connected to the pipeline 26. Thus, the gas removed from the cooling circuit can be introduced into the reducing gas circuit. In the case of the undesirability of the transfer selected - it has a cooling groove into the reducing gas circuit, the exhaust gas can be passed through the valve 43 of the pipe 39 into the pipe 23 and further released into the atmosphere, stored or used for fuel. According to the invention, the water-gas shift reaction, usually occurring in the upper part of the reduction zone, is accelerated by injecting water into the circuit with a reducing gas. Usually, steam is introduced into the system via feed pipe 44 and flows through conduit 45, having valve 46, into inlet chamber 47, from which a part of the ore body is introduced through nozzles 48 to the top of HQ5, and the waste gas is reduced in reducing reactor ash. Steam can also flow from pipe 44 through pipe 40, having a valve 50, to pipe 51 and then through heater 21 to the ngokuy part of the reduction zone 9. In addition, part of the steam can be introduced into the recovery loop through nozzles 48, and the second, insignificant part of the steam can be fed into pipeline 2O through pipeline 49. The amount of steam used depends on factors such as the water content of the recirculated gas flowing through pipeline 28, the temperature of the Gas fed to the reactor, the rate of ore passing, the Amount added of steam is about 1-20. %, the amount of injected through pipe 49 and the steam circuit can be 1-5 mol.% of the circulating gas, and the amount of steam injected through the pipeline 45 - 3-15 mol.% of the circulating gas. In the system shown in FIG. 2, an isolated catalytic reactor is included in the reducing gas circuit. The gas flowing out of the reduction zone 9 flows through pipe 10 and through the catalytic reactor 52, and then through pipe 53 flows into cooler 22. Steam is supplied to reactor 52 through pipe 54 equipped with valve 55. In this form of the invention, a separate unit is required. But the reaction between steam and reducing gas can be controlled independently of the reaction in the reduction zone of the reactor. The table shows the data for a number of examples of use with and without added steam. Letters F - p designate flows, expressed in standard units of flow rate, at each of the five indicated points of the system: P - pipeline 18; f (2 - pipeline 2O; f3 - pipeline 13; 4 pipeline 45; Pg - pipeline 49. The flow rate parameters given in the table were obtained by randomly estimating the added gas per ton of ore (example 1) of SO with flow rate indicators. All other indicators The flow rates shown in the table show the flow rate per 1 ton of ore in relation to the aforementioned initial estimate. Comparison of examples 1 and 2, on the one hand, and examples 3-7, on the other hand} 1y, clearly shows that WATER Vapor in circulating reducing g of substantially reduces carburization in the reduction zone and thereby creates the possibility of adjusting the effective extent. carburization in the cooling zone, allowing the latter to carry out more precise control.
    权利要求:
    Claims (2)
    [1]
    1. Method of reducing metal ore to sponge iron in a shaft furnace, including a countercurrent of hot reducing gas from carbon monoxide and hydrogen with a dispersed ore in the upper part of the shaft furnace, cooling the sponge iron in the lower part of the furnace, recirculating the collar gas, cooling it and dehydrating , characterized in that, in order to achieve the required degree of carburization, steam in an amount of 1-2% by volume is added to the hot reducing gas after entering the reactor
    [2]
    2. The method according to claim 1, about 1 ml and so that part of the steam in the amount of 1-15% is added to the upper part of the reduction zone of the reactor with fresh reducing gas.
    3, the method according to claim 1, of which is that iron ore is used as a metal ore.
    Sources of information taken into account in the examination
    1. US patent number 3765872, CL. From 21 to 13/02, 1974.
    2. US Patent No. 3844766, class C 21 B 13/02, 1974. 23
    25
    iS
    Sitl
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1001863A3|1983-02-28|Process for reducing metal ore
    US4046557A|1977-09-06|Method for producing metallic iron particles
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    US4253867A|1981-03-03|Method of using a methane-containing gas for reducing iron ore
    US5618032A|1997-04-08|Shaft furnace for production of iron carbide
    US4246024A|1981-01-20|Method for the gaseous reduction of metal ores using reducing gas produced by gasification of solid or liquid fossil fuels
    US3827879A|1974-08-06|Method for the gaseous reduction of metal ores
    CA1152749A|1983-08-30|Method of making sponge iron
    US4753677A|1988-06-28|Process and apparatus for producing steel from scrap
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    US4370162A|1983-01-25|Method for the gaseous reduction of iron ore to sponge iron
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    US4702766A|1987-10-27|Method of increasing carbon content of direct reduced iron and apparatus
    US4428772A|1984-01-31|Method for reducing metal ore
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    CA1075913A|1980-04-22|Method and apparatus for producing metallic iron particles
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    同族专利:
    公开号 | 公开日
    NO783733L|1979-05-21|
    GB2011474A|1979-07-11|
    JPS5499705A|1979-08-06|
    DK509278A|1979-05-18|
    AR218512A1|1980-06-13|
    RO76263A|1981-03-30|
    DD140479A5|1980-03-05|
    ZA786210B|1979-10-31|
    IT1109261B|1985-12-16|
    MX152014A|1985-05-24|
    US4150972A|1979-04-24|
    CA1105710A|1981-07-28|
    DE2850053A1|1979-07-05|
    BR7807464A|1979-07-24|
    SE7811329L|1979-05-18|
    GR72090B|1983-09-13|
    JPS638161B2|1988-02-22|
    ES475213A1|1980-05-16|
    IT7851902D0|1978-11-15|
    GB2011474B|1982-10-06|
    IN150496B|1982-10-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2546266C2|2009-07-31|2015-04-10|Хил Текнолоджиз, С.А. Де К.В.|Method of producing direct reduced iron with limited emissions of co2 into atmosphere|DE246153C|
    GB501424A|1936-02-11|1939-02-23|Tadeusz Chmura J|Method for simultaneous production of iron and carbondioxide|
    US3844766A|1973-12-26|1974-10-29|Midland Ross Corp|Process for reducing iron oxide to metallic sponge iron with liquid or solid fuels|US4216011A|1979-04-23|1980-08-05|Hylsa, S.A.|Method and apparatus for the secondary gaseous reduction of metal ores|
    US4224057A|1979-08-20|1980-09-23|Hylsa, S.A.|Method for carburizing sponge iron|
    US4261734A|1979-09-04|1981-04-14|Hylsa, S.A.|Method of making sponge iron|
    US4253867A|1979-10-15|1981-03-03|Hylsa, S.A.|Method of using a methane-containing gas for reducing iron ore|
    US4270739A|1979-10-22|1981-06-02|Midrex Corporation|Apparatus for direct reduction of iron using high sulfur gas|
    US4246024A|1979-10-31|1981-01-20|Grupo Industrial Alfa, S.A.|Method for the gaseous reduction of metal ores using reducing gas produced by gasification of solid or liquid fossil fuels|
    US4528030A|1983-05-16|1985-07-09|Hylsa, S.A.|Method of reducing iron ore|
    US5110350A|1983-05-16|1992-05-05|Hylsa S.A. De C.V.|Method of reducing iron ore|
    US4556417A|1983-05-17|1985-12-03|Hylsa, S.A.|Process for the direct reduction of iron ores|
    US4725309A|1986-03-17|1988-02-16|Hylsa, S.A.|Method and apparatus for producing hot direct reduced iron|
    US5296015A|1990-01-09|1994-03-22|Hylsa S.A. De C.V.|Method for the pneumatic transport of large iron-bearing particles|
    US5181954A|1991-01-14|1993-01-26|Hylsa S.A. De C.V.|Method for coating iron-bearing particles to be processed in a direct reduction process|
    AT400578B|1994-03-24|1996-01-25|Voest Alpine Ind Anlagen|METHOD FOR PROCESSING FINE ORE|
    AT402733B|1994-06-23|1997-08-25|Voest Alpine Ind Anlagen|METHOD FOR DIRECTLY REDUCING IRON-OXIDATING MATERIAL|
    IN2014CN02080A|2011-08-20|2015-05-29|Hyl Technologies Sa De Cv|
    US10508314B2|2015-06-24|2019-12-17|Midrex Technologies, Inc.|Methods and systems for increasing the carbon content of sponge iron in a reduction furnace|
    US10316376B2|2015-06-24|2019-06-11|Midrex Technologies, Inc.|Methods and systems for increasing the carbon content of sponge iron in a reduction furnace|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/852,535|US4150972A|1977-11-17|1977-11-17|Controlling carburization in the reduction of iron ore to sponge iron|
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