• 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:
    1521499 Direct reduction of ores STORA KOPPARBERGS BERGSLAGS AB 11 Dec 1975 [12 Dec 1974] 50795/75 Heading C7D In the reduction of finely-divided metallic oxide material (e.g. Fe or Ni oxides) with carbonaceous material in a reactor supplied with a gas containing 02 (e.g. air), at least part the off-gas mixture containing CO, CO 2 , H 2 , H 2 O is treated with water (preferably as super-heated steam) to react with CO to form CO 2 and H 2 , whereupon the CO 2 is removed and the gas recycled to the reactor for reduction purposes. The oxide may be iron ore concentrate or calcined pyrites, and the carbonaceous material coke, coal, or anthracite, at least part of which may be replaced by oil. The reactor is preferably a fluidized bed, but may be a rotary furnace. In reaction chamber 1, solids are charged at 6, air at 7, and fluidizing gas at 8, and the metallized product is removed at 11. Gas is separated from the particles in cyclones 2, 3 and exits through pipes 9, 10. The gas in pipe 9 is returned directly to the reactor. Gas from pipe 10 is treated with steam at 12 and iron oxide and/or carbonaceous material and/or Fe-containing material at 13 and passed to cyclone 16 where the solids pass to the reactor 1 and the gas to heat exchanger 19, the gas flow 18 then passing to C02 scrubber 20 (using K 2 CO 3 ) and cooler 27 (for H 2 O removal) prior to returning through exchanger 19 and combining with flow 9 to form the fluidizing gas 8. In another embodiment, Fig. 2 (not shown) there is only one cyclone 2 and one gas conduit 9, the offgas being divided into a portion (33) which is returned directly to the reactor and the remainder (34) passes to a bed (36) of catalyst material (e.g. Cr-Fe) where the H 2 O/CO reaction occurs with steam, the gas flow (37) then treated as flow 18. Typically, 30-70% of the off-gas may be so treated. If desired, all of the off-gas may be treated by combining conduits 9 and 10 in Fig. 1 or by removing conduit (33) in (Fig. 2). The carbonaceous material may be coke breeze, coal breeze or anthracite breeze.
    公开号:SU1031410A3
    申请号:SU752199171
    申请日:1975-12-12
    公开日:1983-07-23
    发明作者:Виделл Бьерн
    申请人:Асеа Актиеболаг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the direct reduction of a material containing a metal oxide, such as iron ore, which can be carried out on the material in a finely dispersed solid form in the presence of a carbon material, such as coal, oxygen and air are supplied to the Kotopor-iy. and the achieved result is a method of reducing iron oxide, which involves loading of oxide and carbon materials, input of oxygen-containing and purified from carbon dioxide and waste gas, discharging the finished product and returning the captured dust Cl to the reactor. Exhaust gases contain reducing substances such as CO and Hg oxidized substances such as COj and H2O. The gases also contain nitrogen, if air is supplied to the reactor. In order to use the reducing substances from these gases, the contents of the oxidized substances must be removed by a single apparatus, and the remainder of the gases must be returned to the reactor. In connection with the washing, the gas must be cooled to a temperature close to the room temperature, and then it must be heated to a temperature approximately equal to that which is in the recovery reactor. A washer for this purpose with additional cooling and heating devices becomes very cumbersome. The purpose of the invention is to increase the efficiency of the process. This goal is achieved in that according to the method of metal oxide reduction, which includes loading of oxide and carbonaceous materials, introducing oxygen-containing and purified from carbon dioxide and water, exhaust gas, unloading the finished product and returning the collected dust to the reactor, it is part of the exhaust gas before it is cooled. saturated with water in the form of superheated steam and passed through a layer of iron oxide and / or carbonaceous material. The amount of water is equivalent to the amount of carbon monoxide to be converted to carbon dioxide, and the reaction with iron oxide and / or carbonaceous material is carried out at 400-800 C. Figures 1 and 2 schematically depict devices for carrying out the process. The device (FIG. 1) contains a circulating fluidized bed reactor, i.e. depicts a fluidized bed reactor with recycling material from a separation device that is many times larger than the net flow of solid material through the bed. The reactor has a reaction chamber 1 and a separating device in the form of two cyclones 2 and 3 with return pipes 4 and 5. The circulating fluidized bed is maintained by supplying a stream of finely dispersed material containing iron oxide to the reaction chamber, for example, iron ore concentrate or calcined pyrite having a particle size of up to 1 mm, a stream of finely dispersed solid carbonaceous material, for example, in the form of coke breeze, anthracite fines or coal fines with a particle size smaller than 3 mm, which can be replaced with liquid carbonaceous material, such as oil, a stream of gas containing molecular oxygen, such as air, and a stream of fluidizing gas. Iron oxide containing material and carbonaceous material are served as a mixture in one stream. B. The amount of carbon material supplied may be half the amount of material containing iron oxide. The gas stream 7 contains molecular oxygen, in this example air, and the fluidization stream is designated 8. The material containing iron oxide, carbonaceous material, the gas stream -7 containing molecular oxygen is supplied to a higher point in the reaction chamber, While fluidizing the stream 8 is fed to the bottom of the reaction chamber. Oxygen causes partial combustion of the carbonaceous material, which maintains the temperature in the reaction chamber at 700-lOpO C. In this case, coking and degassing of the carbonaceous material is also possible, as well as reduction of carbon dioxide and water formed during combustion to carbon monoxide and hydrogen, the latter substances contribute to the recovery of the material containing iron oxide. Solid material in the layer and the gases formed. are separated in cyclones 2 and 3. Gases are discharged through pipes 9 and 10, whereas the solid material returns to the reaction chamber through return pipes 4 and 5, respectively, with their discharge ends close to the air inlet to the reaction chamber . The pre-reduced material is removed to stream 11 from the bottom of the reaction chamber and then passes to a final reduction, for example, in an electric furnace at a temperature above the melting point of iron. The pressure in the fluidized bed reactor is maintained at 1–25 atm. The gas mixture discharged from the fluidized bed reactor contains carbon monoxide, hydrogen, carbon dioxide, water, and nitrogen, i.e., both reducing and oxidizing agents. The partial stream 9 returns to the reaction chamber uneducated, while the other partial stream 10 is processed to convert carbon monoxide to carbon dioxide with simultaneous formation of hydrogen and then removing carbon dioxide from this partial stream. Stream 12 of water vapor and stream 13 of material containing oxide of hot and / or carbonaceous material,. and / or iron-containing material is supplied to the partial flow 10. The partial flow 10 with the feed materials firstly passes through the Venturi tube 14 and from there through the link 15 to the cyclone 16 where the solid material is separated and returned to the reaction chamber 1 the reactor is fed with a fluidized bed along link 17, while the gas is discharged as a current 18. After contact between the gas mixture of the reactor of water vapor and the feed solid material while maintaining the temperature, carbon monoxide reacts with water vapor to form two hydro carbon and hydrogen. The amount of water vapor supplied is sufficient to create such an amount of carbon dioxide in the stream 18 that would be at least equal to the amount of carbon dioxide in both gas streams 10 and 9. After cooling down the heat exchanger 19 carbon dioxide b1 4 in the propellant 20 / to which potassium carbonate can be added from compound 21. Potassium bicarbonate is separated from apparatus 20 through compound 22 and can be regenerated into potassium carbonate in apparatus 23 by means of steam treatment, which is supplied at the bottom of the 24 device. Oles of carbon dioxide and water vapor are then discharged in the upper part 25 of the device. The gas 26 discharged from the device 20 is freed from water in the cooler 27. After passing through the device 27, the gas stream contains, compared to lo gas discharged from the reactor, a greatly reduced amount of monoxide, carbon and carbon dioxide and strengths, an increased amount of hydrogen. The gas is then heated in the heat exchanger 19 before connecting the gas stream 9 to the gas stream B. Gas stream 8 is injected after increasing the pressure in the device 29 into the bottom of the reaction chamber 1 of the fluidized bed reactor through an opening 30 located in it. The gas thus serves as a fluidizing gas and at the same time, due to its composition, also serves as a reducing gas. In order to prevent the accumulation of nitrogen gas in the system, which enters the reactor when air is used to supply oxygen, the gas must be discharged in two parts. This can be done by using a pipe 31 fitted with a valve 32. At the same time as the gaseous nitrogen, the other gases are also withdrawn from the partial flow to a certain extent. Carbon monoxide and hydrogen gas expelled through pipe 31 can be used by burning in a steam boiler. The device (Fig. 2) contains only one cyclone 2. The gas stream 9, flown from it, is divided into two partial streams 33 and. 34 respectively, the first one is returned to the fluidized bed reactor without treatment, i.e. with its content of carbon dioxide and water. Water vapor is supplied to the second partial stream 34 in the form of stream 35, after which this partial stream passes through a layer 36 of solid material, such as a chromium-iron catalyst. The layer is maintained at 400-800 ° C and here carbon monoxide reacts with water vapor to form carbon dioxide and hydrogen. The gas stream 37 discharged from bed 36 is then processed in the same way as (described for gas stream 18 in the device according to Fig. 1, before it is returned to the fluidized bed reactor. Instead of the fluidized bed reactor in the devices According to FIGS. 1 and 2, other reactors or Bpamaer, i.e. furnaces, can be used.The invention has been described for the case when the material containing the metal oxide was a material containing iron oxide, but it can be applied to recover other materials metal oxide-containing metals, such as nickel oxide. When all gas returned to the reactor is saturated with water, a device must be used, corresponding to figure 1, in which pipe 9 is connected to pipe 10, or a device in accordance with figure 2, in which pipe 33 is omitted. Part of the gas mixture from reactor 1 may be sent, for example, to a thermal station for use as fuel, the other part is recycled to the reactor in the manner described above.
    Example. The gas stream 9 leaving the reactor 1 has the following composition, O6;%: 1 of 54, CO 25, CO-, 8,
    p, wOilS.Wj 34, U ita, iil
    Hj 7, HjO 4, CH4 2. 17.5% of this gas stream 33 is returned to the reactor without treatment. The remaining gas .34 is mixed with 20% by volume of water vapor 35 and is passed through catalyst bed 36. The leaving catalyst. Gas stream 37 has the following composition, vol, i M 54,
    12,
    20, H, 19,
    H2O
    CO 13, CO2 CH4 2.
    This gas stream is cooled and treated with 17.7 vol.% Of it in the washer 20 with removal of CO2 and H20, after which the stream 28 returns as a mixture with the untreated gas stream 33 into the reactor. In this mixture the content of sal is only 4 vol.%. Excess gas is released and used by burning it in a steam boiler.
    权利要求:
    Claims (2)
    [1]
    1. METHOD OF METAL OXIDE REDUCTIONS, including loading of oxide and carbon materials, introducing oxygen-containing and purified carbon dioxide and water from the exhaust gas, unloading the finished product and returning the collected dust to the reactor, which differs in that, in order to increase the efficiency of the process, a portion of the exhaust gas is saturated with water in the form of superheated steam before it is cooled and passed through a layer of iron oxide and / or carbon material.
    .: j
    [2]
    2. The method according to claim 1, wherein the amount of water is equivalent to the amount of carbon monoxide to be converted into carbon dioxide, and the reaction with jelly oxide and / or carbon material is performed at ° C.
    0YUTG
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    同族专利:
    公开号 | 公开日
    SE387366B|1976-09-06|
    GB1521499A|1978-08-16|
    SE387366C|1980-03-27|
    US4070181A|1978-01-24|
    DE2552904A1|1976-06-16|
    FR2294237B1|1980-12-26|
    JPS51108605A|1976-09-27|
    SE7415578L|1976-06-14|
    FR2294237A1|1976-07-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US1690916A|1925-07-16|1928-11-06|Westberg Sigurd|Method of reducing oxides to metallic form|
    GB1180637A|1967-09-08|1970-02-04|Foster Wheeler Ltd|The Collection and use of the Blow Gases from Steel Production|
    BE791660A|1971-11-22|1973-05-21|Fierro Esponja|DIVIDED ORE REDUCTION PROCESS AND APPARATUS|
    US3909446A|1972-03-31|1975-09-30|Nippon Kokan Kk|Method of manufacturing high quality reducing gas by two stage reforming processes|
    US3822125A|1972-10-13|1974-07-02|Treadwell Corp|Flash smelting of iron ore and concentrate|SE419100B|1979-03-01|1981-07-13|Lindstroem O|SET FOR REDUCING FINALLY DISTRIBUTED IRON OXIDE-CONTAINING MATERIAL|
    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|
    IN164687B|1984-08-16|1989-05-13|Voest Alpine Ag|
    DE3540541A1|1985-11-15|1987-05-21|Metallgesellschaft Ag|METHOD FOR REDUCING HIGHER METAL OXIDS TO LOW METAL OXIDS|
    FR2683830B1|1991-11-19|1994-04-08|Irsid|INSTALLATION FOR REDUCING THE IRON ORE IN A FLUIDIZED BED CIRCULATING.|
    US5429658A|1992-10-06|1995-07-04|Bechtel Group, Inc.|Method of making iron from oily steel and iron ferrous waste|
    US5380352A|1992-10-06|1995-01-10|Bechtel Group, Inc.|Method of using rubber tires in an iron making process|
    US5397376A|1992-10-06|1995-03-14|Bechtel Group, Inc.|Method of providing fuel for an iron making process|
    US5320676A|1992-10-06|1994-06-14|Bechtel Group, Inc.|Low slag iron making process with injecting coolant|
    US5259864A|1992-10-06|1993-11-09|Bechtel Group, Inc.|Method of disposing of environmentally undesirable material and providing fuel for an iron making process e.g. petroleum coke|
    US6197088B1|1992-10-06|2001-03-06|Bechtel Group, Inc.|Producing liquid iron having a low sulfur content|
    US5354356A|1992-10-06|1994-10-11|Bechtel Group Inc.|Method of providing fuel for an iron making process|
    US5338336A|1993-06-30|1994-08-16|Bechtel Group, Inc.|Method of processing electric arc furnace dust and providing fuel for an iron making process|
    US5958107A|1993-12-15|1999-09-28|Bechtel Croup, Inc.|Shift conversion for the preparation of reducing gas|
    CU23070A3|1999-01-12|2005-07-19|Falconbridge Ltd|REDUCTION OF THE FLUDIZED LAYER OF LATERITE FINE WITH REDUCTION OF GASES GENERATED IN SITU.|
    DE10101157A1|2001-01-12|2002-07-18|Mg Technologies Ag|Process for producing a mixture of iron ore and smoldering coke|
    JP4777642B2|2004-12-22|2011-09-21|大陽日酸株式会社|Method for concentrating and recovering metallic nickel from powder containing elemental nickel|
    AU2013355711A1|2012-12-07|2015-07-23|Nippon Steel & Sumikin Engineering Co., Ltd.|Device for manufacturing direct-reduced iron and method for manufacturing direct-reduced iron|
    RU2721249C1|2019-11-29|2020-05-18|Валентин Николаевич Терехов|Composition of charge for melting of carbon-free iron|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE7415578A|SE387366C|1974-12-12|1974-12-12|SET FOR REDUCING FINALLY DISTRIBUTED METAL OXID CONTAINING MATERIAL|
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