EP2281071A1 - Procédé et équipement de fabrication de fonte brute ou d'ébauches liquides en acier - Google Patents

Procédé et équipement de fabrication de fonte brute ou d'ébauches liquides en acier

Info

Publication number
EP2281071A1
EP2281071A1 EP09757365A EP09757365A EP2281071A1 EP 2281071 A1 EP2281071 A1 EP 2281071A1 EP 09757365 A EP09757365 A EP 09757365A EP 09757365 A EP09757365 A EP 09757365A EP 2281071 A1 EP2281071 A1 EP 2281071A1
Authority
EP
European Patent Office
Prior art keywords
reduction
gas
unit
partially reduced
starting materials
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP09757365A
Other languages
German (de)
English (en)
Inventor
Christian Boehm
Jan-Friedemann Plaul
Johannes Leopold Schenk
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Primetals Technologies Austria GmbH
Original Assignee
Siemens VAI Metals Technologies GmbH Austria
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Siemens VAI Metals Technologies GmbH Austria filed Critical Siemens VAI Metals Technologies GmbH Austria
Publication of EP2281071A1 publication Critical patent/EP2281071A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
    • C21B13/002—Reduction of iron ores by passing through a heated column of carbon
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B11/00—Making pig-iron other than in blast furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0046—Making spongy iron or liquid steel, by direct processes making metallised agglomerates or iron oxide
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C21B13/143—Injection of partially reduced ore into a molten bath
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
    • C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
    • C21B2100/66—Heat exchange
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

Definitions

  • the invention relates to a process for the production of pig iron or liquid steel precursors in a smelting unit, in particular a melter gasifier, iron ore-containing starting materials, in particular fine ore, and optionally additives are at least partially reduced in at least one reduction unit by means of a reducing gas.
  • the invention further relates to a plant for the production of pig iron or liquid steel precursors according to the inventive method with a melting unit, in particular a melter gasifier, and at least one reduction unit for reducing iron ore feeds and optionally additives by means of a melting unit with supply of carbon carriers, in particular coal, and oxygen-containing Gas formed reducing gas.
  • a melting unit in particular a melter gasifier
  • at least one reduction unit for reducing iron ore feeds and optionally additives by means of a melting unit with supply of carbon carriers, in particular coal, and oxygen-containing Gas formed reducing gas.
  • pig iron or liquid steel precursors can be made in a smelting reduction process.
  • reducing gas which is produced in a melting aggregate with the supply of coal, for the reduction of iron-containing ores.
  • DE 44 21 673 shows that the reduction gas formed in a melter gasifier can be used in a processed form in a blast furnace, so that the export gas can be used and the process efficiency can be increased.
  • the disadvantage here is that the export gas has a too high calorific value for the blast furnace, so that the achieved process efficiency is limited.
  • An object of the present invention is now to further increase the process efficiency, in particular, the amount of coal required per ton of pig iron or liquid steel precursors is lower, so that a smaller amount of carbon dioxide (CO 2 ) is obtained.
  • a first portion of at least partially reduced feedstocks in the melting unit with supply of carbon carriers, in particular coal, and oxygen-containing gas is melted with simultaneous formation of the reducing gas, the reducing gas fed to the reduction unit and withdrawn after passing through this as the top gas, wherein a second Proportion of at least partially reduced feedstock for reducing and melting is fed to a smelting reduction unit.
  • the at least partially reduced feedstocks are also referred to as low-reduced iron (LRI), these intermediates serving as feedstocks for subsequent process steps of pig iron production or the production of liquid steel precursors.
  • the method it is possible to process an at least partially reduced feedstock, the Low Reduced Iron (LRI), also in a smelting aggregate additional smelting unit, wherein in the smelting reduction unit due to the already partially made reduction saves a significant amount of reducing agent and thus the overall balance the production of pig iron or liquid steel precursors in terms of the necessary process materials, especially coal, are reduced.
  • the productivity of the smelting reduction aggregate can be increased simultaneously. Of the total amount of at least partially reduced feedstocks produced, only a first portion will be present in a melter, e.g. a melter gasifier, processed.
  • the amount of the second portion of at least partially reduced feedstocks in Dependent on the desired top gas quantity and / or the export gas quantity and / or the export gas quality is referred to as the top gas.
  • This top gas can be used after appropriate treatment as an energy source, the processed gas can be used as export gas in other processes, such as energy production.
  • the quality of the export gas is defined by the gas analysis, ie the composition of the export gas and the resulting calorific value.
  • the composition of the export gas depends on the amount of LRI which is processed, for example, in a smelting reduction unit.
  • the reason for this is that when re-using a large amount of the top gas in the reduction unit, the proportions of carbon monoxide (CO) and hydrogen (H 2 ) are always lower and the proportion of CO 2 in the export gas increases.
  • the export gas volume decreases as the proportion of H 2 decreases.
  • the higher LRI production consumes more H 2 , which in turn results in more water (H 2 O). This is separated in the Topgas scrubber.
  • the targeted use of the exported as export gas and optionally treated top gas requires a certain supply quantity, so that the quantity of reduced LRI the Topgasmenge varies and so the reduction process can be adapted to the requirements of the further process of processing the top gas.
  • the amount of the second portion of the at least partially reduced starting materials (LRI) is 0 - 1, 2 times the amount of pig iron obtained in the smelting unit.
  • the second portion can therefore be reduced if necessary to zero or so -A-
  • the amount of the second portion of the at least partially reduced starting materials is 10 - 60%, in particular 20 - 40%, based on the iron content of all iron carriers, which are used in the smelting reduction unit.
  • the LRI used in the smelting reduction unit replaces iron-containing feedstocks. Due to the necessity that in a smelting reduction unit also reducing agents or other process auxiliaries must be used, it has been found to be advantageous if up to max. 60% LRI be used.
  • the technically usual percentages refer to the iron content of all iron carriers in the smelting reduction unit.
  • the degree of reduction in the second portion of the at least partially reduced starting materials and / or in the feedstock used in the melting unit to 40 - 95%, in particular 65 - 75%, adjusted.
  • these reduction rates ensure rapid processing of the prereduced intermediate products in the subsequent smelting unit or in the smelting reduction unit, so that the amount of necessary reducing agents in these units can be kept low.
  • the reduction process or the reduction gas quantity or the composition of the reduction gas can be used to adapt the reduction process in the reduction unit, resulting in a more flexible process which can be stably guided over a wide range of parameters.
  • a specific embodiment of the method according to the invention provides that the at least partial reduction of the iron ore-containing starting materials takes place in a series of 2 to 6, in particular 3 or 4, reduction units connected in series, the reducing gas being passed in countercurrent to the iron ore-containing feedstocks to be reduced. Due to the plurality of reduction units arranged one behind the other, it is possible to more accurately control the temperature control in the individual reduction units, wherein the temperature control can be adapted to the particular charge substance or the degree of reduction. In addition, individual units can be operated as preheating units.
  • a possible embodiment of the method according to the invention provides that the reduction of the iron ore-containing starting materials and optionally of the additives takes place in at least two mutually parallel connected series of series-connected reduction units.
  • the amount of reduced feedstocks can be adjusted or increased accordingly, always using the reducing gas generated in the smelting unit. This has the consequence that at least partially reduced iron-ore-containing starting materials can be produced in such an amount that, in addition to the smelting aggregate, a smelting reduction aggregate can also be supplied.
  • the at least partially reduced starting material is supplied to a compaction, in particular a hot compacting, such as, for example, a hot briquetting.
  • a compaction in particular a hot compacting, such as, for example, a hot briquetting.
  • the compaction reduces the porosity and specific surface area of the reduced feedstocks and largely eliminates the fines.
  • the oxidation during the further processing processing (transport and storage) and at the same time also improves the flow behavior of the compacted substances.
  • Conventional compaction takes place with hot material, so that it can not be cooled in the reduction unit after processing but processed directly.
  • the energy balance is improved and immediate processing in the compaction or subsequently in the smelting unit or in the smelting reduction unit can take place.
  • the hot briquetting has been found to be advantageous.
  • the second portion of the at least partially reduced starting materials is used as iron carrier in the smelting reduction unit.
  • Sinter has the disadvantage that it must first be produced on the basis of sinterable iron ores in a complex process, which leads to very considerable accumulation of problematic gas and dust emissions.
  • LRI second portion of the sinter can be replaced.
  • due to the reduction already made it is also possible to considerably reduce the amount of carbon carriers, in particular coke, required in the smelting reduction unit, so that a substantial cost advantage can be achieved.
  • the at least partially reduced feedstocks can be introduced in the hot state into the smelting unit and / or into the smelting reduction unit, optionally with admixture of cold, partially reduced feedstocks.
  • the hot charging on the one hand, energy can be saved and, on the other hand, by adding cold, partially reduced feedstocks, its temperature can be adapted during charging or during the further processing.
  • a special embodiment of the method according to the invention provides that the at least partially reduced starting materials are hot-compacted and cooled to avoid oxidation processes, in particular by quenching in a water bath become.
  • the at least partially reduced feedstocks are not intended to be processed further, it may be necessary to cool the feedstocks in order to avoid oxidation processes, so that they can also be stored without a protective gas atmosphere.
  • a quench in a water bath has proven to be a cost effective option.
  • the reduction of the starting materials takes place in a, in particular circulating or bubbling fluidized bed in the reduction unit.
  • a fixed bed which is flowed through by a fluid flow, forms a fluidized layer, the so-called fluidized bed, at a certain flow rate. At high flow rates, bubbles form in the fluidized bed.
  • a fluidized bed with a certain volume fraction of solids is formed.
  • the flow rate is less than the rate of descent of the particles. It forms a compact suspension layer with a surface that is stirred up by bursting bubbles.
  • Advantageous is an intensive mixing in the vertical direction.
  • Bubble-forming fluidized beds are used at particle size of the feedstocks to be reduced by ⁇ 8 mm and a mean particle size d 50 of about 0.5 to 2.0 mm.
  • Circulating fluidized beds are used at particle sizes of 0.1 to 1 mm and a mean particle size dso of 0.5 mm.
  • the reduction of the starting materials takes place in a reduction shaft furnace, a rotary kiln or a rotary hearth furnace, wherein the starting materials are used in the form of pellets and / or as lumpy ore and / or as a sinter.
  • the starting materials can be used using different reduction units.
  • a further alternative embodiment of the method according to the invention is found by the reduction of the starting materials takes place in superimposed levels in a reduction furnace floor, wherein the starting materials are forcibly guided by means of a scraper.
  • the forced operation can also process feedstocks that tend to form caking.
  • excess reducing gas is dedusted, washed, optionally mixed with top gas and compressed as recycled gas, for the separation of at least a portion of CO 2 from the recycled gas, fed to a CO 2 -Abborgungsaku and then as product gas into the separator or led directly into the reduction unit.
  • Excess reducing gas which is not directly supplied to a reduction unit, may be reused after a scrubbing operation of solids, after mixing with top gas and after deposition of CO 2 as a high quality reducing gas.
  • the amount of Reduction gas increases and the top gas are used in addition to the use as export gas for further use.
  • a special embodiment of the method according to the invention provides that the pressure in the smelting unit is adjusted by means of a scrubber for washing the excess reducing gas.
  • a scrubber for washing the excess reducing gas.
  • annular gap scrubbers are used to scrub the excess reducing gas so that the change in flow resistance in the scrubber, e.g. by a change in the annular gap of the back pressure and thus the pressure in the melting unit can be easily adjusted.
  • the product gas is particularly advantageously heated before it is returned to the separation device or directly into the reduction unit.
  • the process temperature in the reduction unit can be set specifically or unwanted temperature changes can be avoided. The energy balance of the process is thereby improved.
  • the top gas is cooled and washed before mixing with the excess, dedusted reducing gas, wherein the heat dissipated from the top gas is used to heat the product gas prior to its return to the separator or in the reduction unit.
  • the heat of the top gas is used to adjust the temperature of the product gas, at the same time the hot top gas is cooled down so that it can be used for other uses or treatment steps.
  • the separated CO 2 is removed together with top gas as export gas.
  • the separated in the CO "2 -Abborgungshim top gas is a so-called tail gas from the CO 2 - discharged deposition unit, mostly due to the process small amounts of other Gases are removed with the CO 2 .
  • By mixing with a part of the top gas it is possible to produce a process gas, which can be used as export gas further uses.
  • a possible embodiment of the method according to the invention is achieved by determining the amount of recycled gas and the amount of carbon carriers, in particular coal, in the smelting unit as a function of the amount of at least partially reduced feedstocks.
  • the amount of coal in the smelting unit determines, on the one hand, the temperature in the smelting unit and, on the other hand, the amount of reducing gas available for the reduction.
  • the process materials such as e.g.
  • the coal can be operated in a wide parameter range or quantity range.
  • the reducing gas is partially burned in the reduction unit while supplying oxygen for adjusting the temperature of the reduction unit. This makes it possible to selectively adjust or vary the temperature of the reduction unit and thus the process temperature in the reduction unit.
  • a partial combustion can take place in each reduction unit, so that each reduction stage can be influenced with regard to its temperature and the reducing capacity of the reduction gas.
  • a suitable embodiment of the method according to the invention provides that the starting materials with additives, especially limestone, quicklime, slaked lime, dolomite, calcined or extinguished dolomite or quartz, mixed and preferably dried before its use in the at least one reduction unit, wherein the starting materials and the additives have approximately the same particle size. Due to the advantageous mixture with the excipients, a largely homogeneous reduction is made possible, wherein the particle sizes must be adjusted in such a way that short reduction times and a uniform reduction can be ensured.
  • the previous drying reduces the energy consumption in the reduction unit at high, critical moisture contents of the starting materials (typical values are with a moisture content of over 8%). It has also been shown that drying is advantageous even at lower moisture contents (from about 4% moisture content), since this ensures the flowability of the starting materials in the transport systems and feed containers. With low moisture contents, the starting materials can also be used without prior drying.
  • the capacity of the reduction units can be adjusted so that a larger amount of reduced feedstock is achieved with a melting unit, which also serves as a reduction gas generator.
  • a melting unit which also serves as a reduction gas generator.
  • the downstream hot compacting lumpy at least partially reduced feedstocks can be produced, which form a high-quality feedstock for pig iron production.
  • Due to at least two parallel rows of reduction units connected in series the system can be operated very flexibly. Usually are rows with 3 or 4 reduction units. For example, it is possible to operate only a number of the reduction units for maintenance while the other row is being serviced. Furthermore, it is conceivable to adjust the amount of at least partially reduced starting material in a wide range, wherein the amount of carbon carrier need not or only slightly increased.
  • a possible variant of the system according to the invention provides that one of the devices for H disclosekompakt réelle with a charging container or a reduction shaft, for receiving or further reducing the compacted, at least partially reduced feedstocks is in communication, which is disposed above the melting unit, so that a Charging in the smelting unit is possible.
  • a reduction shaft for charging in the Melting aggregate oxidation of the compacted and at least partially reduced feedstock can be avoided, even if it should lead to delays in the charging in the melter.
  • a very simple solution results when using a charging container, whereby a protective gas can be provided to avoid oxidation processes here as well.
  • the charging from the charging container or from the reduction shaft can take place with the aid of discharge elements such as screw conveyors, scrapers or rotary cell locks by gravity or by means of transport devices.
  • At least one of the devices for hot compacting is connected to a device for quenching the compacted, at least partially reduced starting materials.
  • the immediate quenching and the associated cooling unwanted oxidation processes can be avoided, the shelf life of at least partially reduced feedstocks can thus be significantly increased.
  • one of the devices for hot compacting is coupled to a smelting reduction unit, in particular a blast furnace, an electric downslope furnace or a molten bath furnace such that the compacted, at least partially reduced feedstocks can be introduced into the smelting reduction unit.
  • a smelting reduction unit in particular a blast furnace, an electric downslope furnace or a molten bath furnace
  • the melting unit with the one or more reduction units coupled on the one hand and with another smelting reduction unit so that can be flexibly charged into the smelting unit or the smelting reduction unit.
  • a pig iron production can be achieved at significantly lower CO 2 amount by coupling the aggregates.
  • the type of furnace can be chosen as needed, so that a combination of a plurality of existing plants is possible, for example by adding a smelting unit and the one or more reduction units.
  • a possible embodiment of the system according to the invention is achieved by the melting unit is connected via a line with a separator, in particular a dry dedusting, preferably a cyclone or a reduction cyclone, for the separation of dusts from the reducing gas, the dedusted reducing gas via a reducing gas supply to the Rows of reduction units can be supplied.
  • a separator in particular a dry dedusting, preferably a cyclone or a reduction cyclone, for the separation of dusts from the reducing gas
  • the dedusted reducing gas via a reducing gas supply to the Rows of reduction units can be supplied.
  • Dedusting can improve the gas quality of the reducing gas by eliminating fines and dusts.
  • By using a dry dedusting device it is possible to keep the cooling of the reducing gas low, so that
  • a further possible embodiment of the system according to the invention is achieved by connecting the reducing gas feed line to a scrubber for excess reducing gas in such a way that reducing gas, which is not required in the reduction units, can be removed and washed. This makes it possible to divert a portion of the reducing gas and treat it separately, in particular by a wash, so that solids are largely eliminated. The excess and purified reducing gas can now be supplied to other uses.
  • the scrubber is connected by means of a Rezyklatgastechnisch with a CO 2 -Abborgungsaku, in particular based on an adsorption under pressure change or an absorption process for the separation of CO 2 from the washed reducing gas, wherein the product gas formed over a Product gas line of the separator or the reduction units can be fed.
  • the CO 2 separation unit can be used based on various technologies or the processes mentioned, wherein, in addition to the physical absorption processes, such as, for example, the Rectisol process based on cold methanol as solvent, It is also possible to use chemical absorption processes such as the MEA process based on monoethanolamines and the DEA process based on diethanolamines or else the Benfield process based on a potassium carbonate with an inhibitor. As an alternative to these known processes, it is also possible to use adsorption processes, wherein in particular pressure swing processes are used which use a selective adsorption behavior of a molecular sieve as a function of the pressure. It is particularly advantageous if the lower pressure stage is operated at reduced pressure, as is customary in the vacuum pressure swing process.
  • At least one of the rows of reduction units is connected via a Topgasabtechnisch with the Rezyklat- gas line, so that the discharged from the reduction units top gas with the washed excess reducing gas miscible and can be fed via a compressor of CO 2 -Abborgungsaku.
  • the top gas By including the top gas, it is possible to free the excess reducing gas and the top gas of CO 2 and thus to produce a reducing gas having a high reducing power.
  • the product gas thus obtained can be used as a high-quality reducing gas again for the reduction in or the reduction units, so that a larger amount of starting materials can be reduced without the need for more carbon support must be used in the smelting unit.
  • a particularly advantageous embodiment of the system according to the invention is achieved in that the top gas line and the product gas line each have at least one heat exchanger for cooling the top gas or for heating the product gas, wherein the heat removed from the top gas can be supplied to the product gas.
  • the top gas line and the product gas line each have at least one heat exchanger for cooling the top gas or for heating the product gas, wherein the heat removed from the top gas can be supplied to the product gas.
  • at least one oxide dryer is provided for mixing and drying the iron ore-containing starting materials and optionally the aggregates, this being connected to the rows of reduction units via transport devices and feed containers.
  • Fig. 3 Process example based on a plant according to the invention with a pressure swing process for CO 2 capture in conjunction with a blast furnace
  • Fig. 4 Process example based on a system according to the invention with a vacuum pressure swing method for CO 2 deposition in conjunction with a blast furnace
  • FIG. 1 shows a process diagram or the plant for a direct reduction melting process for fine ores.
  • a smelting unit such as a melter gasifier 1
  • an at least partially reduced fine ore is melted with the addition of carbon carriers, such as coal, whereby reducing gas is formed, which is introduced into the series of reduction units R1 to R4 connected in series.
  • the reducing gas flows in countercurrent to the fine ores to be reduced and optionally additives, which are mixed and dried prior to entry into the reduction unit R4.
  • the at least partially reduced fine ore is made into lumps in a hot compacting 12 and, for the most part, is still introduced into the charging vessel 26 while hot and melted in the melting unit 1 to form pig iron RE.
  • the charging tank can also be designed as a reduction shaft. Further details on the reduction gas treatment will be explained in more detail with reference to FIG. 2.
  • FIG. 2 shows a process diagram or a plant for the direct reduction melting process for fine ores according to the invention.
  • the system has two rows of reduction units R1 to R4 connected in series, which are arranged and connected in parallel, so that, analogously to the scheme according to FIG. 1, the reducing gas in the reduction units is conducted in countercurrent to the feedstocks, which are at least partially reduced by the reducing gas become. Both series are supplied via reduction gas lines by means of reducing gas from the smelting unit 1.
  • the method according to the invention can also be operated with a system according to FIG. 1, the reduction being operated only in a series of reduction units connected in series.
  • the reducing gas is produced by adding carbon carriers, such as lumped coal K or fine coal FK or coal dust KS into the melting unit 1. Fine coal or coal dust are injected into the smelting unit. The pig iron RE is withdrawn from the smelting unit 1 together with slag.
  • carbon carriers such as lumped coal K or fine coal FK or coal dust KS
  • the reducing gas After purifying the reducing gas in a dry separator, e.g. a cyclone 2, the reducing gas is fed to the reduction units. In the separator 2 separated solids are recycled to the melter 1.
  • a dry separator e.g. a cyclone 2
  • Excess reducing gas is supplied after cleaning in the separator 2 a scrubber 3 and further purified.
  • the scrubber can be designed, for example, as an annular gap scrubber, it being possible to control the flow through the scrubber via the setting of the annular gap, so that the pressure in the smelting unit 1 can be regulated via the scrubber 3.
  • the washed reducing gas can now be mixed with top gas, which is withdrawn from the reduction unit R4, and fed as recycled gas by means of a compressor 4 to a CO 2 -Abscheide worn 5.
  • Deposited gas fractions, which predominantly have CO 2 are discharged as tail gas via the tail gas line 6, the tail gas line 6 discharging into the export gas line 7 so that excess top gas can be removed together with tail gas as export gas EG.
  • the purified from CO 2 recycled gas is passed as product gas via the product gas line 8 either in the separator 2 or directly into the reduction units R1.
  • the top gas can be cooled by means of a heat exchanger 9, 9a, wherein the heat thereby extracted is fed to a heat exchanger 10 and used to heat the product gas. Furthermore, the top gas can be cleaned after the cooling in the heat exchanger in scrubbers 16, 16a.
  • the reducing gas and optionally also product gas are fed to the reduction units R1. These flow through the reduction units in countercurrent to the starting materials E and optionally the additives Z.
  • the reduction unit R4 is operated as a preheating unit for preheating the feedstocks and the aggregates.
  • the starting materials and the additives are first mixed in an oxide dryer 11 and dried and fed via suitable means the reduction units R4.
  • the at least partially reduced feedstocks and, if appropriate, the additives are discharged from the reduction units R1 of the two rows and fed to two devices for hot compacting 12 and 13, so that lumpy material, such as e.g. Briquettes, is generated.
  • LRI Low Reduced Iron
  • the LRI can be used directly in a hot state in a smelting reduction unit 15, which is advantageously a blast furnace.
  • cold LRI or blends of hot and cold LRI can be used in the smelting reduction aggregate.
  • the at least partially reduced starting materials and optionally the additives can be introduced as briquettes or in another particulate form as iron carrier instead of sinter in the smelting reduction unit, so that at least a portion of the sinter can be saved. This makes it possible that in the sintering process at the sintering plant large amounts of sinter and / or pellets and / or lump ore can be saved.
  • the saving of sinter is particularly advantageous, since the exhaust gases produced during sintering and the coke required for this purpose can be significantly reduced. Furthermore, the amount of coke required in the blast furnace can be reduced because the LRI introduced instead of the sinter lowers the specific energy consumption. At the same time, the specific power of the blast furnace can be increased by the reduced specific coke consumption. Based on a concrete example according to FIG. 3, a possible process route will be exemplified below.
  • the plant consists of a series of 19 reduction units connected in series, which are connected to a melting aggregate, in a concrete case with a melter gasifier 1.
  • This piece of equipment known as FINEX ® plant 18th
  • the melter gasifier 1 is connected to a further row 21 of reduction units connected in series.
  • the at least partially reduced feedstocks and additives produced in this series are referred to as low-reduced lron (LRI). Accordingly, this part of the plant 20 is referred to as LRI plant.
  • the LRI plant will also operated with reducing gas from the melter gasifier 1, so that the two rows of reduction units are operated substantially parallel to each other.
  • the LRI usually has a degree of reduction of 60 to 70%.
  • Suitable starting materials are concentrates of ores 22, in particular iron ores, in question, based on naturally occurring ores with the accumulation of iron ore, an ore concentrate is produced.
  • sintered ores 23 are used. These are ores, which are usually added to a sintering plant and have small particle sizes, ie fine ores are attributable.
  • coal 24 and aggregates 25 are used, wherein the coal is used in the melter gasifier for generating the reducing gas and for melting the pig iron.
  • the 2.2 million tonnes LRI can be fed to a smelting reduction unit such as a blast furnace to replace sinter.
  • a smelting reduction unit such as a blast furnace to replace sinter.
  • an export gas EG with an energy content of about 364 MW is generated, which can be supplied to an external use eg in a power plant.
  • Coke and aggregates can thus be produced in a blast furnace about 4 million tonnes of pig iron.
  • the sintering plant can be dimensioned smaller or sintering waste gases and coke required for sintering can be reduced.
  • Another advantage is that the amount of coke required in the blast furnace can be correspondingly reduced, whereby with an LRI use of 40 to 50% of the iron content of all iron carriers, it is possible to save about 150-200 kg of coke per ton of pig iron.
  • the total amount of iron in about 25 is - generated 75% higher than the blast furnace - 40% above the melting unit the FINEX ® plant and approximately at the 60th.
  • the reduced consumption of coke and a total of carbon carriers falls in the process of the invention less export gas, so that a more efficient overall process can be ensured at a lower environmental impact. This considerable cost advantages per ton of produced pig iron can be achieved.
  • the stated quantities are influenced by the type of CO 2 capture device used.
  • FIG. 4 shows the effect of a modified CO 2 separation device. If, instead of a pressure swing process for the separation of CO 2 from the recycled gas, a vacuum pressure swing method is used, then the amount of LRI that can be generated with the plant, can be significantly increased. By adjusting the quantities of concentrate, sintered ore and aggregates, it will be possible to increase the volume of LRI from approximately 2.2 million to 2.8 million tonnes, whereby the export gas volume can be reduced. The necessary amount of carbon carriers remains unchanged. The calorific value of the export gas EG is reduced when the vacuum pressure change procedure. The process uses an even more effective separation of CO 2 , which is achieved by lowering the minimum pressure to near vacuum level.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Manufacture Of Iron (AREA)
  • Treatment Of Steel In Its Molten State (AREA)

Abstract

L'invention porte sur un procédé de fabrication de fonte brute ou d'ébauches liquides en acier dans un équipement de coulée (1), en particulier dans un gazéificateur de fusion, dans lequel des matières premières contenant du minerai de fer, et éventuellement des agrégats, sont réduits au moins partiellement dans au moins un équipement de réduction (R1, R2, R3, R4) à l'aide d'un gaz de réduction. Selon l'invention, une première partie des matières premières au moins partiellement réduites sont fondues dans l'équipement de coulée (1), par apport de porteurs de carbone et d'un gaz contenant de l'oxygène, avec formation simultanée du gaz de réduction. Le gaz de réduction est envoyé à l'équipement de réduction (R1, R2, R3, R4) et, après avoir traversé ce dernier, est soutiré en tant que gaz de tête, une deuxième partie des matières premières au moins partiellement réduites étant, pour réduction et fusion, envoyées à un équipement de réduction par fusion (15).
EP09757365A 2008-06-06 2009-04-27 Procédé et équipement de fabrication de fonte brute ou d'ébauches liquides en acier Withdrawn EP2281071A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT0092008A AT506837B1 (de) 2008-06-06 2008-06-06 Verfahren und vorrichtung zur herstellung von roheisen oder flüssigen stahlvorprodukten
PCT/EP2009/055047 WO2009146982A1 (fr) 2008-06-06 2009-04-27 Procédé et équipement de fabrication de fonte brute ou d'ébauches liquides en acier

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EP2281071A1 true EP2281071A1 (fr) 2011-02-09

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US (2) US8632622B2 (fr)
EP (1) EP2281071A1 (fr)
JP (1) JP2011522126A (fr)
KR (1) KR20110015689A (fr)
CN (1) CN102057060B (fr)
AR (1) AR072053A1 (fr)
AT (1) AT506837B1 (fr)
AU (1) AU2009254062B2 (fr)
CA (1) CA2726957A1 (fr)
CL (1) CL2009001362A1 (fr)
MX (1) MX2010013382A (fr)
RU (1) RU2490333C2 (fr)
TW (1) TW201002828A (fr)
UA (1) UA102690C2 (fr)
WO (1) WO2009146982A1 (fr)
ZA (1) ZA201100017B (fr)

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AT507955B1 (de) 2009-02-20 2011-02-15 Siemens Vai Metals Tech Gmbh Verfahren und anlage zum herstellen von substitutgas
AT508953B1 (de) 2009-10-16 2011-07-15 Siemens Vai Metals Tech Gmbh Verfahren und vorrichtung zur chargierung in ein einschmelzaggregat
AT509073B1 (de) * 2009-12-23 2011-06-15 Siemens Vai Metals Tech Gmbh Verfahren und vorrichtung zur bereitstellung von reduktionsgas aus generatorgas
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AT509735B1 (de) * 2010-05-11 2012-03-15 Siemens Vai Metals Tech Gmbh Verfahren und vorrichtung zur herstellung von zumindest teilweise reduzierten metallerzen und/oder metallen
KR101289217B1 (ko) * 2010-12-28 2013-07-29 주식회사 포스코 일관제철시스템 및 일관제철방법
AT510565B1 (de) 2011-06-21 2012-05-15 Siemens Vai Metals Tech Gmbh Vorrichtung zur regelung von prozessgasen in einer anlage zur herstellung von direkt reduzierten metallerzen
AT511888B1 (de) 2011-09-13 2013-06-15 Siemens Vai Metals Tech Gmbh Vorrichtung zur energieoptimierung in einer anlage zur herstellung von direkt reduzierten metallerzen
AT511992B1 (de) * 2011-09-29 2013-12-15 Siemens Vai Metals Tech Gmbh Verfahren und vorrichtung zur herstellung von wasserstoff aus bei der roheisenerzeugung anfallenden gasen
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KR101376138B1 (ko) * 2012-12-27 2014-03-19 주식회사 포스코 용철제조장치 및 용철제조방법
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TW201002828A (en) 2010-01-16
JP2011522126A (ja) 2011-07-28
US8632622B2 (en) 2014-01-21
AU2009254062B2 (en) 2014-01-16
US9181594B2 (en) 2015-11-10
US20140042677A1 (en) 2014-02-13
CL2009001362A1 (es) 2010-06-04
AT506837A1 (de) 2009-12-15
CN102057060B (zh) 2015-03-11
ZA201100017B (en) 2012-03-28
AT506837B1 (de) 2010-03-15
CA2726957A1 (fr) 2009-12-10
KR20110015689A (ko) 2011-02-16
AU2009254062A2 (en) 2011-01-27
RU2010153663A (ru) 2012-07-20
AU2009254062A1 (en) 2009-12-10
MX2010013382A (es) 2011-04-05
WO2009146982A1 (fr) 2009-12-10
CN102057060A (zh) 2011-05-11
US20110138965A1 (en) 2011-06-16
UA102690C2 (ru) 2013-08-12
RU2490333C2 (ru) 2013-08-20
AR072053A1 (es) 2010-08-04

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