• 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 direct reduction of iron in a shaft furnace using coal gasification products, including a countercurrent of hot reducing gases and charge loaded from above, recirculation, cooling and purification of top gas and mixing it with gasification products, recycling and cleaning the cooling gas, and also the discharge of the product, which differs in that, in order to increase the efficiency of the process, a part of the stream is separated from the products of gasification of solid fuels, cooled and then mixed again with the main flow to a temperature of 750-1050 ° C, then purified from suspended matter and fed to a mixture containing lumpy oxide material, solid fuel and limestone. 2. Method according to H.1, characterized in that to the gasification product streams to be mixed part of the cooled purified flue gas. 3. A method according to claims 1 and 2, characterized in that the quality of the gasification products has an index of 4-8. 4. Installation for direct reduction of iron in a shaft furnace using gasification products O) coal containing a charge loading and unloading device, a reducing gas inlet nozzle, recirculation contours of top gas and cooling gas from a cooling scrubber, as well as a solid gasifier fuel, connected to the furnace piping, characterized in that, in order to increase the efficiency of the process, the pipeline is equipped with a bypass containing a chiller for separating the gas flow and and it cyclone, wherein bayaas connected to the recirculation loop of the top gas.
    公开号:SU1155162A3
    申请号:SU813335455
    申请日:1981-09-14
    公开日:1985-05-07
    发明作者:Комбс Скарлотт Джон；Уолтер Санзенбахер Чарльз
    申请人:Миндрекс Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the direct reduction of iron oxides in the form of pellets or coarse ore to refined iron in the solid state in a shaft furnace. The closest to the invention to the technical essence and the achieved result is a method of direct reduction of iron in a shaft furnace using coal gasification products, including a countercurrent of hot reducing gases and charge loaded from above, recycling, cooling and clearing the top gas and mixing it with gasification products, recirculation and purification of cooling gas, as well as product discharge. An installation for direct reduction of iron in a shaft furnace using coal gasification gas products contains devices for loading and unloading the charge, a reducing gas inlet fitting, recirculation circuits for top gas and cooling gas with a scrubber cooler, and a solid fuel gasifier connected to the furnace by a pipeline l . The disadvantages of this method are its complexity, as well as the high coal consumption. The main problem, due to which the process recognizes with impractical or requires the consumption of coal in large quantities, is that the hot gas from the rectangular gasifier contains a small amount of reducing agents (CO + H) with respect to oxidizing agents ( ) for its direct and effective use in the direct reduction of iron. The purpose of the invention is to increase the effect of: - process efficiency. This goal is achieved by the fact that with the method of direct reduction of iron in a shaft furnace with is. use of gasification products of coal, including a countercurrent of hot reducing gases and charge loaded from above, recirculation, cooling and purification of blast furnace gas and mixing it with gasification products, recirculation and purification of the cooling gas, as well as unloading the product, from gas ha2 2 Zifikatsii solid fuel separates part of the flow, cool down and mix again with the main stream to a total temperature of 750-1050 ° C, then clear of suspensions and feed the mixture containing couscon oxide material, solid fuel and limestone. In addition, a portion of the cooled cleaned top gas is added to the mixed gasification product streams. At the same time, the quality of gasification products has an index of 4-8. In an installation for direct reduction of iron in a shaft furnace using coal gasification products, containing fir loading and unloading devices, a reducing gas inlet nozzle, recirculation of top gas and cooling gases with a fridge scrubber, and a solid fuel gasifier connected to the furnace by a pipeline, the pipeline is equipped with a bypass containing a chiller for separating the gas stream and a cyclone installed behind it, while the bypass is connected to the recirculation loop of the top furnace about gas. In this method, about 6.1 Gcal of coal is required for gasification, 0.6 Gcal of carbon for the reaction in the furnace, 0.8 Gcal of coal in order to generate electricity for oxygen gas to produce 1 metric. tons of direct reduction iron with simultaneous production of 3.6 Gcal of pure fuel gas. Consequently, to produce 1 metric, a ton of direct reduction iron consumes approximately 3.9 Gcal. In this case, only 80% of the carbon added to the mixture reacts, and the excess carbon is released along with the direct reduction iron and can be separated from the direct reduction iron by magnetic means and recycled to further reduce energy consumption during the process. The drawing shows the implementation of the proposed method. A refractory lined lined countercurrent shaft-type furnace 1 with a reducing atmosphere has a feed funnel 2 mounted above, into which iron oxide 3 is supplied as oxide deposits.
    311
    and / or natural lumpy ore, carbon (coke) 4 and limestone to 5 with a memorial particle size of 5-30 mm. The feed materials are lowered into the furnace through the feed pipe 6 to form charge 7 inside the furnace. The reduced iron pellets and / or lump product, unreacted carbon, calcium sulfide and unreacted lime to the HJHI lime are drained from the bottom of the furnace through the discharge pipe 8 using a discharge conveyor 9, the speed of movement of which controls the rate of flow of charge of charge 7 through the furnace 1.
    The clean hot reducing gas is supplied to the furnace 1 through the inlet pipe 10 for the hot reducing gas, and then through a plurality of gas outlet openings 11 located in the wall of refractory brick 12 in the middle part of the furnace. The hot reducing gas moves inwards and then upwards in the opposite direction with respect to the descending charge (along arrow 13). The CO-rich exhaust gas (blast furnace gas) leaves the charge 7 near the furnace top at level 14 formed by the angle of repose of the materials entering through the feed pipe 6 for oxides through the flue pipe 15, is cooled and cleaned of dust in the refrigerator-scrubber 16 and removed is from; systems in the form of clean heating gas through a pipe 17.
    The lower portion of the furnace 1 has a cooling recirculation circuit of the flue for cooling the reduced iron before it is discharged, consisting of an inlet 18. for the cooling gas connected to the cooling gas distribution device 19 in the furnace 1, the cooling gas trap 20 located above the distribution device inside the furnace, the gas discharge pipe 21 and the internal gas recirculation system consisting of a scrubber cooler 22, recirculation gas blowers 23 and adjacent pipelines.
    The fossil fuel gasifier 24 has an oxygen injector 25 connected to it, a steam injector 26 and a nozzle 27 for fossil fuels. Oxygen or oxygen and steam
    5162CH
    pos; blunt through ddg gasification injectors of gasification of fossil fuel chip coal, lignin or charcoal in the gasifier 24 with the goal of 1 g of radiation 5 VIY hot coal, which leaves the gas generator through the pipe 28 and then goes to the separator 29,
    The inorganic residues of combustion 10 after gasification are removed from the gasifier 24 through an ash removal unit (not shown). The main part of the hot gas from the gasifier in the pipe 28 is passed through the heated opening 30, which creates resistance to the flow and forces a smaller part of the hot gas to pass through the discharge pipe 31 and the refrigerator 32. Then the cooled gas passes through the pipe 33 and the control valve 34 before mixing with hot gas in the pipe 35. The temperature of the mixed gas from the gasifier in the pipe 36 is measured by a thermocouple 37, which is connected to a control device 38 that controls the position of the valve 34. In some cases, the cooled Exhaust flue gas (at the outlet) can be partially or fully reQ circulated in conduit 39 as released gas. The waste gas contains solidified particles from the blowing agent, which are removed in the cyclone 40. The sprayed waste gas is discharged from the cyclone through pipe 41 through an inlet for reducing gas.
    Countercurrent shaft furnace is recognized as the most efficient medium for the production of iron from reprocessing plants. In such furnaces, hot reducing gas is used to heat the incoming cold iron oxide to a reducing temperature, as well as to obtain reducing agents (CO + 11) necessary for the chemical reduction of iron oxide to refined iron. The experience of the industrial operation of natural gas installations showed that, in order to fully utilize the chemical efficiency of a countercurrent shaft furnace with a reducing atmosphere, the reduction potential of a hot gas, i.e. its quality, which is defined by; The ratio of reducing agents (CO + P) and oxidizing agents (CO2 + H20) must be at least 8. 511 When gasifying solid solid fossil fuels like coal or lignin in such a blowing agent with partial oxidation, as a blowing agent 2D, which produces hot 1az, Solar, mainly CO, Hj, C02 and IUO, the best indicator of the hot gas produced by industrial methods is 3-4. The invention provides for an increase in the quality of gas in the same furnace shaft in which a direct process takes place, and, thus, there is no need for additional expensive and low-grade equipment. Until now, it was considered impractical to dehydrate carbon oxidation (coke). 950 rats are lower because at low temperatures, the reaction rate decreases. For this reason, the enrichment reactions must be carried out at temperatures from 1350 ° C (the temperature of the gas stream b-flowing from the gasifier) to 950 ° C. and then cool the enriched gas to 815 ° C and below to use it E of the direct reduction furnace. During laboratory studies, it was established that carbon actually reacts with {.O and C02 at a temperature as low as: the reaction will pass relatively long, time. In addition, hot gas from the gas forming agent can be introduced into the shaft of the direct reduction furnace at a temperature exceeding 950 C. but up to 1050 C this does not lead to the gluing of meta particles of the particles in the charge, provided that 5. There is carbon for the d-thermal reaction of the reaction g. The carbon reacts with the cooling of the charge by means of a cooling system. A properly designed shaft furnace of direct recovery requires at least 6 h of silence in the mine of solid material and a correspondingly long period of time; There is gas in it to accomplish reakid direct reduction. By increasing the volume of the furnace, it is possible to envisage even a longer period of being; These long periods of time make it possible to practically carry out the carbon reaction at porma-G1O1 ex.gguatacioi at a temperature during the process of direct reduction in a shaft furnace (750-900 s). And the third is JI and e, t aki ixi about br a z ohm, about b it - a significant reduction in the costs of production: ((d), compared with the known technical specifications, Description the invention in action is based on gasification of a sub-bituminous coal using oxygen, NF, and in the gasifier with a suspended layer of particles, which produces hot gas containing, in the original C0 I, (Yu. i- yO, T; :: g-; ps; p; -pu and gasification in such a city is zoboagzat:; gtg; 400- s; At this temperature y-th,: n, it turns to ash in liquid cocTOfrt f-re ;, water cooled down;, yes, shech: t -; h of the lower part of the gaseous gas generator of slag type. Pr and m :: o, Yar peartipi: or 2 incomplete;.); :: at 1380 C l: 4 ji. Due to sulfur and O and JY1: :; about unreacted g: jc, in, and at the CS, se dd; is up to g of throats ™ Nick 32 nodes of which is gas but g ohl: g7: with g, from skip- Improvements ga.za to 7.1, ijjciGT kakss-goo; 5, Any liquid, per ton of water ghzs 113 113 azo-sample Ki-ic Kari: e.fT hjo-: С 1; о ;;., isiromed, Exhaust J5.:; In the lap 40 drink in the oven 1, GOLY-GYE; gas spreading-ghggs 7 and then stt; -; JV-horned large-scale rhode. -Overdoorly hinged on the shaft of the type of particles, coke and particles to ensure good fluid particles and AOJ & KHiji particle sizes 5 1A; 7 1 and self-made furnace B the furnace In the course of) ;; is heated by hot gazelle. ;; sigma is calcined 3 mts ;, l about-a fire and regegir ui .r with sulfur in: 3occTasfoBWTejibHOM gas with industrial) ap1-; I eat sugar: - Calcium 5a 7.Pe carbon reacts with COj and in reducing gas with a CO and Hj ,. The batch mixture is cooled in the zone of the secondary cooling of the furnace and is discharged through the furnace outlet pipe 8 to the discharge conveyor 9. The product obtained from the furnace consists of direct reduced iron, unreacted carbon, unreacted lime or lime, and calcium sulfide. Direct reduction iron may be magnetically separated for use in electric arc furnaces or simply screened for use in green furnaces. The hot gas containing C02 and N02 fumes is supplied to the engine through inlet ports 11 at a temperature of about 4.8, and CO2 and P2 react with carbon. Due to the durability of the components in the shaft furnace, these endothermic reaction furnaces continue and cool the gas to almost 750 ° C with simultaneous enrichment of the gas in the charge to quality indicator 8, which is suitable for efficient operation of the direct reduction furnace. - In the incoming gas at 950 ° C in the charge of the gas, the sulfur concentration is on the order of 4100 hours per # crone in the specific specified difference of Ts1, coal. Sulfur is in the form. and COS, both of these components react with lime.
    T a b
    persons 28 The combination of a relatively low temperature (950 (.) with o6orar; ieii ii: ;; - i to the lowest oxidizing agents (CO. +)) is removed by removing the ILS COS from the component. Sulfur components, contained in gpze, 1Gredpoche A limestone limestone in a mixture containing lime and iron of direct reduction. As a result, low-sulfur iron of direct reduction is obtained, but the amount of limestone depends on the sulfur content in the coal. The amount formed during the above-mentioned desulfurization reactions is em only a small fraction of the total gas and has a small impact on the quality of the reacted gas: C02 gas, vyslobot-kd.e.chigv) i ho.de kal1111irirovanie nsBecrsir,}; .-) in quicklime, also ok. Only a negligible Obligation of gas quality (both of these nexChlSH.1X inclusions COj + HO are taken into account when compiling 1x1 tables), all tabulated are based on the received4 and () metric.t of direct reduction iron with a metallization degree of 92 % and soda; carbon rust 1.5%. Table 1 presents data on gas consumption and gas quality (the ratio of the reducing agent to the oxidizer) in the areas corresponding to the references in the drawing.
    From the gasifier 28
    On tap31
    Recovery10
    Enriched13
    Spent recovery
    Cooled top fuel outlet
    In standard cubic meters.
    Table 2 presents data on the need for raw materials for the coal gasifier 24.
    table 2
    Table 3 shows the requirements for raw materials and products obtained in the shaft furnace 1 of direct reduction, and Table 4 shows the energy consumption.
    T a b l and c a 3
    54.0
    69.3. 15.1
    19.4
    Continuation of table 1
    1996
    1577
    1.5
    1, A
    1827
    1453
    1.9
    1.7
    Continuation of table 3 25.0
    19.5 72.9
    54.0 43.2 58.3 14.6
    10.8
    Table 4 6.1
    5.1 0.6
    0.4 0.8
    0.6
    111155162
    Continued from Table 4
    . 2.8
    3.6 3.3
    3.9
    Approximately 230 kWh at -30% conversion efficiency.
    Table 5 presents the temperature ha in some areas of the process.
    Table At the outlet from the gas Formation at the exit from the cooling tower at the exhaust gas Forming gas 27 50,07.8 Exiting the refrigerator at the exhaust pipe 33 54.68.5 To the mine41 51.58.0 After reaction with carbon 13 34.47.4
    2
    Prod.zhzhenig. tab. 5 3
    restored41
    950 neither
    After reaction
    13,730 with carbon (in the mine)
    15
    660
    After reaction with coal 17
    40 2Q
    Table 6 Tables 6 and 7 show the results of gas analysis at the indicated sites of the process for a gasifier gas with a quality of 4.1 (low) and a quality of 8.0 (high), respectively. 29,211,70,10,84000 31,93,60,10,94400 30,19,00,10,8. 4100 33,73,70,10,8 At the exit from the direct reduction mine 14 32.8 28.4 Fuel gas at the exit 17 35.8 31.0
    Calorific value of the carrier fuel is 1959 Kcal / Nm (NNU). Gaseous gas 2775, 44.6 inlet V'kod from a refrigerator on a branch pipe 3359, 14.7 4157.94.6 to a mine After reaction with carbon 1361, 13.4 Exit from a direct reduction mine 1433, 530.1 new Fuel gas at the exit 1736 , 432.7
    Calorific value of the carrier fuel is 1904 Kcal / Nm (NNU).
    Continuation of table 6
    Table 7 26.1 11.2 0.11.4 28.5 3.0 0.11.6 30.36.30.10.940t) 0 31.23.60.10.94100 30.65.40.10 , 94000 33,11,40,10,9 23,910,60,11,7 26,03,00,11,8О
    15115516
    The proposed HPP for direct reduction of iron using gas produced by a coal-forming gasifier as a source of reducing agent while simultaneously producing clean fuel gas for further use after its removal from the plant is
    energetically playing, as well as 1.1m as c ioco6 direct. calling a hot gas from a corner (1. gasifier by increasing the reduction ratio of gas from the gasifier through reaction with carbon in the same furnace shaft where the direct reduction of iron takes place.
    权利要求:
    Claims (4)
    [1]
    1. A method for direct reduction of iron in a shaft furnace using coal gasification products, including a countercurrent of hot reducing gases and a charge loaded from above, recirculation, cooling and purification of blast furnace gas and mixing it with gasification products, recirculation and purification of cooling gas, as well as unloading product, characterized in that, in order to increase the efficiency of the process, part of the stream is separated from the gasification products of solid Fuel, cooled and mixed again with the main stream to The temperature 750-1050 C, and then purified from suspensions and fed to the batch containing lumpy oxidic material, solid fuel and limestone.
    [2]
    2. The method according to claim 1, characterized in that a portion of the cooled purified blast furnace gas is added to the mixed gasification product streams.
    [3]
    3. The method of pop. 1 and 2, with the fact that the quality of gasification products has an indicator of 4-8.
    [4]
    4. Installation for direct reduction of iron in a shaft furnace using coal gasification products, containing a charge loading and unloading device, a reducing gas inlet pipe, top and cooling gas recirculation circuits with a fridge-scrubber, and a solid fuel gasifier connected to the furnace by a pipeline characterized in that, in order to increase the efficiency of the process, the pipeline is equipped with a bypass containing a cooler for separating the gas stream and a cycle installed behind it prefecture, the bypass circuit is connected to the top gas recycling.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1052165A3|1983-10-30|Method for reducing iron oxide
    US4260412A|1981-04-07|Method of producing direct reduced iron with fluid bed coal gasification
    RU2405944C1|2010-12-10|Method and device of electric energy generation at gas and steam power plant
    US4423702A|1984-01-03|Method for desulfurization, denitrifaction, and oxidation of carbonaceous fuels
    SU1528324A3|1989-12-07|Method of obtaining cast iron in horizontal reactor
    EA017978B1|2013-04-30|Process for production of direct reduced iron
    EP2798293B1|2019-06-12|Method of producing molten iron in a blast furnace with top-gas recycle
    CZ284106B6|1998-08-12|Process of obtaining electric power simultaneously with the production of liquid pig iron and apparatus for making the same
    SU980629A3|1982-12-07|Method for reducing pulverulent oxides in shaft reactor
    RU2118374C1|1998-08-27|Method and installation for producing cast iron from metal ores
    SU938747A3|1982-06-23|Process and apparatus for reducing iron oxide and producing molten crude iron
    SU1155162A3|1985-05-07|Method of direct reduction of iron in shaft furnace with use of coal gasification products and device for effecting same
    CA1309589C|1992-11-03|Method of producing a clean gas containing carbon monoxide and hydrogen
    CN85106200A|1987-03-04|The direct method of the ferric oxide of reduction in the raw material
    SU1138036A3|1985-01-30|Method of operation of blast furnace and system for producing molten iron and reducing gas
    SU1711677A3|1992-02-07|Method and apparatus for production melted pig iron or intermediately product for steel making
    US4365789A|1982-12-28|Apparatus for the direct reduction of iron in a shaft furnace using gas from coal
    US20150152344A1|2015-06-04|Melt gasifier system
    US4274863A|1981-06-23|Method of treating pollutant-laden gases, especially from a steel-making or coking plant
    US4205830A|1980-06-03|Apparatus for the direct reduction of iron using gas from coal
    SU1145934A3|1985-03-15|Method of obtaining reducing gas for ferric oxide reduction in shaft furnace
    SU1166668A3|1985-07-07|Method of producing reduced iron and reducing gas and device for effecting same
    同族专利:
    公开号 | 公开日
    NZ198327A|1984-05-31|
    IN155080B|1984-12-29|
    ZA815563B|1982-08-25|
    CA1172455A|1984-08-14|
    US4331470A|1982-05-25|
    PH17852A|1985-01-09|
    AU525672B2|1982-11-18|
    GB2083839B|1984-07-25|
    JPS5782417A|1982-05-22|
    BR8105761A|1982-05-25|
    KR840002356B1|1984-12-21|
    PL137834B1|1986-07-31|
    GB2083839A|1982-03-31|
    AT381953B|1986-12-29|
    PL233022A1|1982-08-30|
    TR21578A|1984-10-16|
    PH17080A|1984-05-24|
    BE890196A|1982-01-04|
    KR830006439A|1983-09-24|
    AU7507581A|1982-04-08|
    DE3135914A1|1982-05-27|
    ATA388381A|1986-05-15|
    JPS649376B2|1989-02-17|
    DD201807A5|1983-08-10|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3853538A|1973-07-20|1974-12-10|Steel Corp|Use of reducing gas by coal gasification for direct iron ore reduction|
    DE2438790B2|1974-08-13|1976-09-09|Thyssen Purofer GmbH, 4000 Düsseldorf|PROCESS AND SYSTEM FOR THE REDUCTION OF IRON ORES, IN PARTICULAR IRON ORES PELLETS|
    US4017305A|1975-04-15|1977-04-12|United States Steel Corporation|Process for heat hardening|
    US4173465A|1978-08-15|1979-11-06|Midrex Corporation|Method for the direct reduction of iron using gas from coal|US4608240A|1983-11-04|1986-08-26|Hylsa, S.A.|Method for the desulfurization of hydrocarbon gas|
    IT1177077B|1983-12-02|1987-08-26|Skf Steel Eng Ab|PROCEDURE AND PLANT TO REDUCE OXIDE MATERIAL SIMULTANEOUSLY GENERATING A GAS SUITABLE AS COMBUSTIBLE GAS|
    AT381954B|1984-08-16|1986-12-29|Voest Alpine Ag|METHOD FOR DIRECTLY REDUCING IRON OXIDE MATERIALS|
    AT404600B|1997-03-12|1998-12-28|Voest Alpine Ind Anlagen|METHOD AND DEVICE FOR TREATING REDUCING GAS FOR REDUCING ORES|
    US6149859A|1997-11-03|2000-11-21|Texaco Inc.|Gasification plant for direct reduction reactors|
    AU2014366893A1|2013-12-20|2016-06-09|Tata Steel Limited|Smelting process and apparatus|
    CN104561425B|2015-02-12|2016-04-13|王俊|A kind of gas base method microwave heating continuous industry produces reduced iron powder device and using method thereof|
    CN110438278A|2019-09-11|2019-11-12|武汉科思瑞迪科技有限公司|A kind of Shaft Furnace Direct Reduction Process of gas base and the combination of coal base phase|
    CN110453027A|2019-09-11|2019-11-15|武汉科思瑞迪科技有限公司|A kind of Shaft Furnace Direct Reduction Process of gas base and the combination of coal base phase|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/187,024|US4331470A|1980-09-15|1980-09-15|Method for the direct reduction of iron in a shaft furnace using gas from coal|
    [返回顶部]