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    公开号:AT510273A4
    申请号:T0036911
    申请日:2011-03-17
    公开日:2012-03-15
    发明作者:Robert Dipl Ing Millner；Jan-Friedemann Dipl Ing Dr Plaul
    申请人:Siemens Vai Metals Tech Gmbh；
    IPC主号:
    专利说明:

    % 2010P21665AT • ♦ ♦ * • ♦ • »• * r · · · 1
    description
    Method for regulating the calorific value of exhaust gases from pig iron or synthesis gas plants 5
    FIELD OF THE INVENTION
    The invention relates to a method for heating value control of exhaust gases from plants for pig iron production with integrated 10 C02-deposition, wherein at least a portion of the exhaust gas discharged as export gas from the plant for pig iron production, optionally collected in an export gas container and subsequently thermally utilized in a gas turbine, said the exhaust gas from the gas turbine is fed to a waste heat steam generator for generating steam. The invention can also be used for heating value control for synthesis gas from plants for synthesis gas production with integrated CO 2 separation plants, wherein at least a portion of the synthesis gas discharged as export gas from the plant for syngas production, but not collected in an export gas container, but subsequently thermally utilized in a gas turbine is, wherein the exhaust gas from the gas turbine is supplied to a waste heat steam generator for generating steam. The invention also relates to a system for carrying out the method according to the invention.
    PRIOR ART For the production of pig iron, by which also the production of pig iron-like products is to be included, there are essentially two known common processes: the blast furnace process and the smelting reduction. 35 In the blast furnace process, pig iron is first produced from iron ore with the aid of coke. In addition, scrap can also be used. Thereafter, steel is produced by further processes from pig iron. The iron ore is called lump ore,
    2 010P21665AT 2 • · · · ► * * I * · »I1 · • I · € ♦» 4 < * j < i < * ··· * «
    • * * I »· l < 4 M ········································
    Pellets or sinter together with the reducing agents (usually coke, or coal, for example in the form of a
    Fine coal indisposition plant) and other constituents (limestone, slag formers, etc.) are mixed to form the so-called Möller and then charged into the blast furnace. The blast furnace is a metallurgical reactor in which the Möllersäule reacts in countercurrent with hot air, the so-called hot blast. By burning the carbon from the coke, the necessary heat for the reaction and carbon monoxide or hydrogen, which is a significant part of the reducing gas and flows through the Möllersäule and reduces the iron ore. The result is pig iron and slag, which are tapped periodically.
    In the so-called oxygen blast furnace, which is also referred to as a blast furnace with top or top gas recirculation, in the gasification of coke or coal oxygen-containing gas with more than 90% by volume of oxygen (02) is blown into the blast furnace. For the gas leaving the blast furnace, the so-called top or blast furnace gas, a gas purification must be provided (for example, dust collectors and / or cyclones in combination with wet scrubbers, bag filter units or hot gas filters). Furthermore, in the oxygen blast furnace usually a compressor, preferably with aftercooler, provided for the recirculated top gas in the blast furnace and a device for CCb removal, according to the prior art usually by means of pressure swing adsorption.
    Further options for the design of a blast furnace process are a heater for the reducing gas and / or a combustion chamber for the partial combustion with oxygen.
    The disadvantages of the blast furnace are the demands on the feedstock and the high emission of carbon dioxide. The iron carrier used and the coke must be lumpy and hard
    2010P21665AT 3 • * · · · «+ < ························································································ "enough to leave enough voids in the piling column to ensure that it flows through the wind. CQ2 emissions represent a heavy environmental impact. Therefore, there are efforts to replace the blast furnace route. These include iron sponge production based on natural gas (MIDREX, HYL, FINMET®) and the smelting reduction process {COREX® and FINEX® processes).
    In the smelting reduction, a melter gasifier is used in which hot liquid metal is produced, and at least one reduction reactor in which the carrier of the iron ore (lump, fine ore, pellets, sinter) is reduced with reducing gas, the reducing gas in the melter gasifier by gasification of Coal (and possibly a small proportion of coke) is produced with oxygen (90% or more).
    Also in the smelting reduction process are usually
    Gas purification systems (on the one hand for the top gas from the reduction reactor, on the other hand for the reduction gas from the melter gasifier), a compressor, preferably with aftercooler, for the reducing gas recycled in the reduction reactor reducing gas, a device for CO 2 removal, according to the prior art usually by pressure swing Adsorption and optionally provided a heater for the reducing gas and / or a combustion chamber for partial combustion with oxygen.
    The COREX® process is a two-stage process
    Smelting reduction. The smelting reduction combines the process of direct reduction (prereduction of iron into sponge iron) with a melting process (main reduction). 4
    2010P21665AT
    The well-known FINEX® process essentially corresponds to the COREX® process, but iron ore is introduced as fine ore.
    The invention can be applied not only to pig iron production but also to synthesis gas plants. Synthesis gases are all hydrogen-containing and usually also CO-containing gas mixtures which are to be used in a synthesis reaction. Synthesis gases can be made from solid, liquid or gaseous substances. In particular, this includes coal gasification (coal is converted with water vapor and / or oxygen to hydrogen and CO) and the production of synthesis gas from natural gas (conversion of methane with water vapor and / or oxygen to hydrogen and CO). In the case of coal gasification expediently eliminates the export gas storage, as provided for plants for pig iron production, because the high synthesis gas pressure from the carburetor (usually> 20 barg, preferably about 40 barg) can also be used in the gas turbine, where in the Usually a gas pressure of about 20-25 barg is needed. However, the CO 2 -rich residual gas from the CO 2 removal plant must be compressed by means of a compressor to the pressure of the synthesis gas stream.
    If the CO 2 emission into the atmosphere in the production of pig iron or in the synthesis gas production is to be reduced, this must from the exhaust gases from the pig iron or. Synthesis gas generation deposited and stored in bound form (English: C02 Capture and Sequestration (CCS)).
    For the deposition of CO 2 mainly the pressure swing adsorption (English: PSA - Pressure Swing Adsorption), in particular also the vacuum pressure swing adsorption (English: VPSA - Vacuum Pressure Swing Adsorption) is used. Pressure swing adsorption is a physical process for the selective decomposition of gas mixtures under pressure. Special porous materials (eg zeolites,
    2010P21665AT 5
    Activated carbon, activated silica (SiO 2), activated alumina (Al 2 O 3) or the combined use of these materials) are used as a molecular sieve to adsorb molecules according to their adsorption forces and / or their kinetic diameters. The PSA exploits the fact that gases adsorb to surfaces to different extents. The gas mixture is introduced into a column under a precisely defined pressure. The unwanted components (in this case CO 2 and H 2 O) and the valuable material (in this case CO, H 2, CH 4) adsorb largely freely through the column Once the adsorbent has been completely charged, the pressure is reduced and the column is backwashed ) PSA plant requires electrical current for the prior compression of C02 rich recycle gas.
    The product gas stream after the pressure swing adsorption, which contains the valuable substances, still contains about 2-6 vol% CO2 in exhaust gases from pig iron production. However, the residual gas flow (tail gas) from the (V) PSA plant still contains relatively high reducing gas constituents (such as CO, Η2), which are lost for pig iron production.
    The residual gas stream after pressure swing adsorption, which contains the undesirable components, is typically composed of exhaust gases from pig iron production as follows:
    Compound% vol at VPSA vol% at PSA h2 2.2 5.5 n2 1.5 2.4 CO 10, 9 16, 8 co2 82.1 72.2 ch4 0.7 0.9 h2o 2, 6 2, 2
    The residual gas can not simply be thermally recycled because it - due to the low and / or fluctuating
    2010P21665AT 6
    Calorific value of about ± 50% - would have to be enriched with other fuels. For example, it can be mixed entirely with so-called export gas, which is the part of the process gas that is withdrawn from the pig iron or syngas production process and used for other purposes, such as fuel in a combined gas and steam power plant Combined cycle power plant (English: combined cycle power plant, short CCPP) is called. Components of the export gas in the pig iron production can be: Topgas and / or generator gas from a blast furnace, a reduction reactor (fluidized bed reactor) or a reduction shaft (fixed bed reactor) so-called offgas from a reduction reactor (fluidized bed reactor) so-called excess gas (English, excess gas) from a gasifier
    The admixing of residual gas from the CO 2 separation to the export gas is only meaningful if the calorific value of the export gas is so high that it does not sink after admixing the residual gas below a value that is too low for the subsequent use of the export gas.
    A reduced calorific value of the export gas subsequently reduces the efficiency of a power plant supplied with the export gas, such as in a combined cycle power plant due to the high combustion gas compression and the lower efficiency of the gas turbine. In a steam power plant or boiler, the flame temperature would be reduced during combustion.
    If an admixing of the residual gas from the CO 2 separation to export gas does not make sense, this has been completely burned on a hot torch. This not only has the disadvantage that the heat generated during flaring is lost, but also that by incomplete combustion of the
    2010P21665AT 7 • * «·· * · · · · * * * * * * ♦ * ♦ ♦ • · · · · · · · · · · · · · · · * * * * ♦ * ·»
    Residual gases on the hot flare considerable gas emissions in the form of carbon monoxide CO, hydrogen sulfide H2S, etc., could arise.
    Another problem with the use of export gas from pig iron or syngas production plants is that the calorific value of the export gas varies. Therefore, the export gas, before being supplied to a consumer such as a power plant, is stored in a high volume export gas container, e.g. in the order of 100,000 m3, to make the gas composition uniform. In order to achieve a constant calorific value with a fluctuation range of +/- 1-2%, waste nitrogen from an air separation plant has so far been admixed with deviations of the calorific value from the desired constant value upward. In the case of deviations in the calorific value, coke oven gas (for example from the pyrolysis of hard coal to coke for the blast furnace) was admixed.
    A corresponding method for calorific value compensation is shown in AT 507 525 Bl. According to this publication, the export gas is supplied to a buffer device, where the control of the heating value is carried out, according to which the calorific value is raised by the addition of metallurgical gas or natural gas or lowered by the addition of nitrogen or water vapor.
    The accumulating residual gas (tail gas) from a CO 2 separation device is collected in the AT 507 525 Bl in a separate storage device, wherein there is a calorific value compensation in the stored residual gas. The pre-stored residual gas is supplied to a waste heat steam generator, where steam is generated by combustion of the residual gas, which drives a steam turbine and a generator. The residual gas can be fed into the storage device, a part of the export gas that has passed an expansion turbine.
    Although in the embodiment according to AT 507 525 Bl the burning of the residual gas in a heating torch is avoided,
    2010P21665AT 8 * «· · · · · · · · · · * * * *« «- * * • ·« * * · · · · ··································· Control of the calorific value of the export gas High-quality fuel gas, such as metallurgical gas available in the plant or natural gas to be procured specifically, which is not available in the plant.
    It is therefore an object of the invention to provide a method for heating value control for the export gas, which manages with a lower addition of high quality fuel gases.
    PRESENTATION OF THE INVENTION
    The object is achieved by a method according to claim 1, by the export gas before the gas turbine, in particular optionally before the export gas container, depending on the calorific value of the export gas after the residual gas addition, in particular after the export gas container, at least a portion of the residual gas from the C02-Abscheideanlage admixed is, wherein the residual gas content is increased when the calorific value of the export gas over a predefined maximum calorific value increases, and the residual gas content is reduced, when the calorific value of the export gas falls below a predefined minimum calorific value.
    As a rule, a desired heating value of the export gas, which depends on the gas turbine used, is determined, as well as a fluctuation range by which the actual calorific value may deviate from the desired calorific value during operation. The upper end of the fluctuation range represents the predefined maximum calorific value, the lower end represents the predefined minimum calorific value. If no fluctuation range is specified, then the minimum coincides with the maximum calorific value. For most of the operation, the heating value control will be possible due to the added amount of residual gas. But it can also be provided that with residual gas
    2010P21665AT 9 »· ·· * * * * * f« * * »* · * ι • ι · < ······················································································································ mixed gas passes through a buffer tank in front of the gas turbine. In this buffer container further, supplied before the buffer tank gas can be mixed with the mixture of export gas and residual gas.
    For example, provision may be made for fuel gas to be added in addition to the predefined minimum calorific value in front of the gas turbine, for example before and / or after the buffer vessel. As fuel gas is called gas that contains combustible gases for the most part. Typical fuel gases are natural gas, liquefied natural gas (LNG), coke oven gas.
    If the calorific value increases, it can be provided that, in addition to the residual gas, non-combustible gas is added when the predefined maximum calorific value in front of the gas turbine is exceeded, for example before and / or after the buffer vessel. Non-flammable gas is gas that contains predominantly non-flammable gases. Typical non-combustible gases are nitrogen or water vapor.
    The part of the residual gas that is not mixed with the export gas can be supplied to the metallurgical gas network in the case of pig iron production. The metallurgical gas network includes all the pipelines for gases produced in a smelting plant or produced for smelting, such as gas for drying raw material (iron ore, coal) or gas supplied from the smelter to a conventional power plant with boiler as fuel. Of course, the gas network for the top gas, the top gas or generator gas, the offgas and the excess gas is part of the metallurgical gas network, ideally, the residual gas is added to the blast furnace, since the calorific value is in the same range (the average calorific value is in the range of 2,000 to 4,000 kJ / Nm3). The part of the residual gas, which is not added to the export gas, can also be fed to a hot torch. 10
    2Q1QP21665AT
    Bel a fault or lack of decrease in the residual gas through the steelworks gas network, the residual gas can be passed through a control valve to the hot flare.
    In the present invention, the export gas can contain at least one of the following exhaust gases: Top gas from a blast furnace, in particular from an oxygen blast furnace with top gas recirculation, Exhaust gas from a melter gasifier of a smelting reduction plant, which is also referred to as excess gas, Exhaust gas from at least one reduction reactor of a smelting reduction plant, which is also referred to as offgas, or from a reduction shaft - exhaust gas from at least one fixed bed reactor for preheating and / or reduction of iron oxides and / or iron briquettes of a smelting reduction plant, which is also referred to as top gas - synthesis gas from a plant for syngas production.
    The plant according to the invention for carrying out the process comprises at least: - a plant for pig iron production with integrated CO 2 separation plant or a plant for syngas production with integrated CO 2 separation plant, an export gas line, with which a part of the exhaust gas or synthesis gas as export gas from the plant for pig iron production or for synthesis gas production can be removed, - optionally an export gas container in which the export gas can be collected, and - a gas turbine in which the export gas can be thermally recycled, - a waste heat steam generator, in which the exhaust gas from
    The gas turbine of the gas turbine can be used to generate steam.
    It is characterized in that the CO 2 separation plant is connected to the export gas line that the export gas before the gas turbine, in particular optionally before the export gas container at least a portion of the residual gas from the C02-Abscheideanlage can be added, and that after the addition of residual gas, in particular after the export gas container a meter for calorific value measurement of the export gas is provided.
    According to the method variants described above, it can be provided that-if appropriate after the export gas container and - a buffer container is provided in front of the gas turbine.
    Before and / or after the buffer tank can be provided at least one supply line for fuel gas, as well as at least one supply line for non-combustible gas. For that part of the residual gas that is not added to the export gas, in the case of pig iron production, a line may be provided which opens into the metallurgical gas network, preferably into the blast furnace network, or into a hot flare.
    In the export gas line usually opens at least one line, with which - top gas from a blast furnace, in particular from a Sauerstoffhochofen with Topgasrückführung, - exhaust gas from a melter gasifier smelting reduction plant, - exhaust gas from at least one reduction reactor or reduction shaft of a smelting reduction plant, - exhaust from at least one Fixed bed reactor for preheating and / or reducing iron oxides and / or iron briquettes of a smelting reduction plant,
    2010P21665AT * 12 4 • * • · - Synthesis gas from a synthesis gas plant can be fed into the export gas pipeline.
    With the method according to the invention or the device according to the invention, higher-grade fuel gas, such as natural gas, liquefied petroleum gas or coke oven gas, can be saved; at the same time, the calorific value of the export gas can be adapted to the gas turbine, thus achieving a high degree of efficiency of the gas turbine. By mixing the residual gas from the CO 2 separation plant to the export gas less or no residual gas is flared off. The energy of the residual gas can therefore be largely converted into electrical energy, the gas emissions of the heating torch sink by unburned residual gas or are completely avoided in the best case.
    BRIEF DESCRIPTION OF THE FIGURES
    The invention is explained in more detail below with reference to the exemplary and schematic figures.
    1 shows a system according to the invention with a blast furnace FIG. 2 shows an installation according to the invention with a FINEX® system FIG. 3 shows an installation according to the invention with a COREX® system
    WAYS FOR CARRYING OUT THE INVENTION
    In Fig. 1, an oxygen blast furnace is shown with top gas recirculation 1, in which iron ore from a sinter plant 2 and coke (not shown) is supplied.
    Oxygenated gas 3 having an oxygen content > 90% by volume is introduced into the ring line 4, as well as heated reducing gas 5 is introduced into the blast furnace 1 together with cold or preheated oxygen 02 in the reduction gas furnace 6. Slag 7 and Cast Iron 8 are subtracted below 13 2010P21665AT. At the top of the blast furnace 1, the top or top gas 9 is removed and prepurified in a dust separator or cyclone 10 and a wet scrubber 11 (or a bag filter or hot gas filter system) cleaned again. The top or top gas purified in this way can be taken directly from the blast furnace system as export gas 12 and fed to an export gas container 13, on the other hand it can be fed to a CO 2 separation plant, here as a plant for pressure swing absorption of CO 2, in short as a PSA plant 14, is executed, wherein the purified top or top gas is previously compressed in a compressor 15 to about 2-6 barg and cooled in an aftercooler 16 to about 30-60 ° C.
    The PSA system 14 is known from the prior art and therefore need not be further explained here.
    The residual gas 20 is here according to the invention at least partially supplied to the export gas 12 before the export gas tank 13 and mixed with this. It could also be in the case of an absorption system for CC> 2 removal - all or part - either after an H2S purification again released into the atmosphere and / or another compressor for the liquefaction of CO2 are fed to then forward it and about to store underground or to use it as a substitute for nitrogen in iron production. In the case of a (V) PSA for CO 2 removal and sequestration, a further treatment plant is usually required to concentrate the CO 2 stream.
    The pressure energy content of the export gas 12 can also be utilized in an expansion turbine 35 (top gas pressure recovery turbine), which in this example is arranged in front of the export gas container 13 and the supply line for residual gas 20. A corresponding diversion for the export gas 12 to the expansion turbine 35 is provided if the export gas 12 - in the case of a
    Maintenance outage of the expansion turbine - not by the
    14 2010P21665AT 4 * • Λ * *
    Expansion turbine 35 is to be performed. The pressure of the export gas 12 after the expansion turbine 35 and before the supply of residual gas 20 is measured with a pressure gauge 17 and actuated depending on the measured pressure or the level in Exportgasbehälter a valve 18 in the line 21 for export gas to the hot torch 19: exceeds the pressure the export gas 12 or the level in the export gas container a predefined value, then at least part of it is passed to the hot flare 19 and burned there, the rest goes on in the export gas container 13th
    The export gas from the export gas container 13 is fed to a combined cycle power plant 24 as fuel, optionally via a buffer tank 25 and optionally a filter 26. The export gas is supplied to a fuel gas compressor 27 and then to the gas turbine 28. The waste heat from the gas turbine is used in the waste heat boiler 29 for a steam cycle with a steam turbine 30. For the combined cycle power plant 24 not required export gas 22 can be withdrawn after the export gas tank 13 and the metallurgical gas network can be used where it can be used for other purposes, such as drying raw materials (coal, fine coal or Erztrocknung) or it can be used as fuel for conventional thermal utilization (eg steam power plants, steam boilers, etc.) are used. The derivation of unneeded export gas 22 can be done via a control valve, not shown here in the line for the export gas 22 is not needed.
    After the export gas container 13 and after the discharge of unneeded export gas 22, a first measuring device 23 is provided for calorific value measurement. Depending on its measured value, a fan 31 is regulated, which is arranged in a line 32 for residual gas. This line 32 branches off from the line for residual gas 20 before its mouth in the line for export gas 12 and leads to the line for unneeded export gas 22. If the calorific value of the export gas over a predefined
    2010P21665AT 15 »*» »» »..... · · · · · · · · · · · Maximalen maximalen maximalen maximalen maximalen maximalen maximalen maximalen Reduced power of the fan 31, so that less residual gas sucked into the line 32 and thus less residual gas to unneeded export gas 22 passes. Thus, more residual gas enters the export gas container 13 and the calorific value of the export gas decreases.
    Instead of the blower 31, a control valve can also be used which is regulated on the basis of the measured value of the first measuring device 23 for calorific value measurement and which increases the supply of residual gas 20 to the export gas 12 and thus into the export gas container 13.
    However, if the calorific value of the export gas falls below a predefined minimum calorific value, then the power of the fan 31 is increased (or a corresponding control valve fully or partially open), so that more residual gas is sucked or led into the conduit 32 and thus more residual gas to not needed export gas 22 passes. Thus, less residual gas enters the export gas container 13 and the calorific value of the export gas increases. For emergencies, a control valve, not shown here can be opened, which initiates the residual gas into the hot flare 19 for combustion.
    The pressure in the foot of the hot torch 19 is less than about 5 kPag. This pressure in turn is less than the pressure of the export gas 12, which is usually between 8 and 12 kPag, with the pressure of the export gas 12 due to pipeline pressure losses in the amount of about 1-3 kPag to a pressure of 7-9 kPag im Export gas tank 13 lowers.
    Since the line system, including that for the residual gas 20 and the line 32, remains connected to the export gas line system 12 throughout operation, the desorption pressure for the PSA system 14 also does not change.
    Thus, the solution according to the invention does not lead to any deterioration in the operation of the PSA system 14.
    2010P21665AT
    Since the regulation of the calorific value by means of blower 31 or control valve for the residual gas does not always have to be sufficient, after the export gas container 13 and after the first measuring device 23 for calorific value measurement optionally additionally a buffer tank 25 is arranged, in which the export gas 12, which may already mixed with residual gas 20 can be mixed with other gases. For this purpose, a fuel gas supply line 33 (e.g., natural gas, LPG, coke oven gas) and a non-combustible gas supply 34 (e.g., nitrogen such as waste nitrogen from an air separation plant or steam) are disposed between the first measuring device 23 for calorific value measurement and the buffer tank 25. Fuel gas can now be added with these feed lines if, even without the addition of residual gas, the calorific value can not be raised above the predefined minimum calorific value. Similarly, non-flammable gas can be added if, even with the addition of all the residual gas, the calorific value can not be lowered below the predefined maximum calorific value.
    After these two supply lines, but before the buffer tank 25, a second measuring device 36 is provided for calorific value measurement. This checks whether the calorific value between predefined minimum and maximum calorific value could be adjusted by the leads 33, 34 in front of it. If not, fuel gas or incombustible gas can be added again by means of supply lines 33, 34 arranged after the buffer container 25. The calorific value thus obtained is determined with a third measuring device 56 for calorific value measurement. This measuring device 56 is provided after the supply lines 33, 34, which are arranged after the buffer tank 25, and in front of the gas compressor 27, here also before the filter 26th
    The typical calorific value of the residual gas from a PSA plant 14 is 700-900 kcal / Nm3, the calorific value of the offgas from 17
    2010P21665AT of a FINEX © plant, which is withdrawn as export gas 12, is 1300-1800 kcal / Nm3. The calorific value required for the gas turbine 28 is in the range of the calorific value of the export gas, the typical permissible fluctuation range of the calorific value for 1300 kcal / Nm3 is +/- 20 kcal / Nm3. In this case, the predefined minimum calorific value would be 1280 kcal / Nm3 and the predefined maximum calorific value would be 1320 kcal / Nm3. The calorific value required for the gas turbine 28 depends on the type of gas turbine. 10
    The mixed with residual gas export gas is cleaned as a precaution before the gas turbine 27 and optionally after the buffer tank 25 in a separator 26 for solids. Fig. 2 shows the connection according to the invention between a FINEX © system on the one hand and a combined cycle power plant 24 together with an upstream export gas container 13 on the other hand, the latter being constructed exactly the same as those in FIG. 20 The power plant 24 is supplied by a FINEX® plant with export gas 12, which can be cached in an export gas container 13. Not required for the power plant 24 export gas 22 may be the metallurgical gas network, such as a raw material drying, fed again. 25
    The FINEX® plant has in this example four reduction reactors 37-40, which are designed as fluidized bed reactors and are charged with fine ore. Fine ore and additives 41 are fed to the ore drying 42 and from there first to the fourth
    Reactor 37, they then enter the third 38, the second 39 and finally the first reduction reactor 40. Instead of four fluidized bed reactors 37-40 but only three may be present.
    In countercurrent to the fine ore, the reducing gas 43 is guided. It is introduced at the bottom of the first reduction reactor 40 and exits at its top. Before it enters the second reduction reactor 39 from below, it can still be heated with oxygen 02, as well as between the second 39 and third 38 reduction reactor.
    The exhaust gas 44 from the reduction reactors is purified in a wet scrubber 47 and used as export gas 12 as described above in the downstream combined cycle power plant 24 on.
    The reducing gas 43 is prepared in a melter gasifier 48, in the one hand coal in the form of lumpy coal 49 and coal in powder form 50 - this is supplied together with oxygen 02, in the other hand, the vorreduzierte in the reduction reactors 37-40 and in the Iron briquetting 51 is added in hot condition to briquettes (English: HCl for Hot Compacted Iron) shaped iron ore. The iron briquettes arrive via a conveyor 52 in a storage tank 53, which is designed as a fixed bed reactor, where the iron briquettes with coarse purified gas generator 54 from the melter gasifier 48 optionally preheated and reduced. Cold iron briquettes 65 can also be added here. Subsequently, the iron briquettes or oxides are charged from above into the melter gasifier 48. Low reduced iron (LRI) may also be withdrawn from iron briquetting 51.
    The coal in the melter gasifier 48 is gasified, resulting in a gas mixture consisting mainly of CO and H2, and withdrawn as a reducing gas (generator gas) 54 and a partial flow as reducing gas 43 is fed to the reduction reactors 37-40. The hot metal melted in the melter gasifier 48 and the slag are withdrawn, see arrow 58.
    The withdrawn from the meltdown gasifier 48 generator gas 54 is first passed into a separator 59 to deposit with discharged dust and the dust over
    2010P21665AT 19
    Dust burner in the melter gasifier 48 due. Part of the purified from the coarse dust generator gas is further purified by wet scrubber 60 and removed as excess gas 61 from the FINEX © system, a part of the 5 PSA system 14 can be supplied.
    Another part of the purified gas generator 54 is also further purified in a wet scrubber 62, fed to a gas compressor 63 for cooling and then after 10 mixing with the removed from the PSA system 14, C02-freed product gas 64 back to the generator gas 54 after the melter gasifier 48th supplied for cooling. As a result of this recycling of the C02-freed gas 64, the reducing proportions contained therein can still be exploited for the FINEXO-15 process and, on the other hand, the required cooling of the hot generator gas 54 from approximately 1050 ° C. to 700-870 ° C. can be ensured.
    The top gas 55 leaving the storage system 53, where the iron briquettes or 20 iron oxides are heated and reduced with dedusted and cooled generator gas 54 from the melter gasifier 48, is cleaned in a wet scrubber 66 and then likewise at least partially removed from the PSA unit 14 for removal of C02 supplied, at least partially the exhaust gas 25 44 are admixed from the reduction reactors 37-40. The
    Gas supply to the storage facility 53 may also be omitted.
    Part of the exhaust gas 44 from the reduction reactors 37-40 can also be mixed directly into the PSA system 14. The 30 PSA system 14 to be supplied gases are previously compressed in a compressor 15.
    According to the invention, the residual gas 20 from the PSA plant 14 can be wholly or partly admixed with the export gas 12 or added via the unneeded export gas 22 to the metallurgical gas network or fed to the hot flare 19 for combustion, as has already been described with reference to FIG , As well
    2010P21665AT 20 «« * Μ * «** Φ * * Φ · ** Φ · * Φ Φ« · «* I« Φ Φ Φ fl * · · Φ »Μ * * Φ · Φ Φ · * ·» Structure and function of the plant coincide with that of the export gas container 13 with that of FIG. 1.
    Fig. 3 shows the connection according to the invention between a plant for smelting reduction on the one hand and a
    Export gas container 13 with combined cycle power plant 24 on the other hand, the latter being constructed exactly the same as those in Fig. 1. 10 The power plant 24 is supplied by a COREX © plant with export gas 12, which can be temporarily stored in an export gas container 13. Not required for the power plant 24 export gas 22 may be the metallurgical gas network, such as a raw material drying, fed again. 15
    In this example, the COREX® plant has a reduction shaft 45, which is designed as a fixed bed reactor and is charged with lump, pellets, sinter and additives, see reference number 46. 20 In countercurrent to the lump etc., the reducing gas 43 is conducted. It is introduced at the bottom of the reduction shaft 45 and exits at the top as top gas 57 from. The top gas 57 from the reduction shaft 45 is further purified in a wet scrubber 67 and a portion removed as export gas 12 25 from the COREX® plant and freed a part of the C02 in the COREX® plant PSA plant 14 and again the Reduction shaft 45 supplied.
    The reducing gas 43 for the reduction shaft 45 is produced in a melter gasifier 48, into which coal in the form of lumped coal 49 and coal in powder form 50 - this together with oxygen 02 - is fed, in the other hand, in the reduction shaft 45 prereduced iron ore is added. The coal in the melter gasifier 48 is gasified, resulting in a gas mixture consisting mainly of CO and H2, and withdrawn as top gas (generator gas) 54 and a partial flow as reducing gas 43 is fed to the reduction shaft 45. 21
    2010P21665AT
    The hot metal melted in the melter gasifier 48 and the slag are withdrawn, see arrow 58.
    The withdrawn from the melter gasifier 48 generator gas 54 5 is passed into a separator 59 to deposit with discharged dust and return the dust dust burner in the melter gasifier 48.
    Part of the top dust 54 purified by the coarse dust is further purified by means of wet scrubber 68 and removed as excess gas 10 69 from the COREX® plant and the top gas 57 or the
    Export gas 12 added.
    A portion of the purified top or generator gas 54 after wet scrubber 68 is fed to a gas compressor 70 15 for cooling and then fed back to the top or generator gas 54 after the melter gasifier 48 for cooling. As a result of this recirculation, the reducing proportions contained therein can still be utilized for the COREX® process and, on the other hand, the required cooling of the hot top-20 or generator gas 54 from approximately 1050 ° C. to 700-900 ° C. can be ensured.
    A portion of the top gas 57, which may also contain excess gas 69, is compressed by means of compressor 15 and cooled in the aftercooler 25 16 before it is fed to the PSA system 14. The product gas freed from CO2 from the PSA plant 14 is at least partially supplied to the cooled gas after the wet scrubber 68 and thus back to the generator gas 54. The product gas freed from C02 from the PSA plant 14 may also be partially heated in a heating unit 71 and admixing the reducing gas 43 after adding the generator gas 54. However, part of the top gas 57 may also be heated in the heating unit 71 and then mixed with the reducing gas 43.
    According to the invention, the residual gas 20 is at least partially replaced by the export gas 12 in front of the export gas container 13 22 22.
    2010P21665AT and mixed with this. It could also, in whole or in part, either be released back into the atmosphere after H2S purification and / or fed to another compressor for liquefying CO 2, to be sent away and stored underground, or as a substitute for it To use nitrogen in iron production.
    The pressure of the export gas 12 after the supply of residual gas 10 20 is measured with a pressure gauge 17 and actuated depending on the measured pressure or the level of Exportgasspeichers a valve 18 in the line 21 for export gas to the hot flare 19: exceeds the pressure of the export gas 12 a predefined pressure or a predefined level in the export gas storage, then at least part of it is passed to the hot flare 19 and burned there, the rest goes into the export gas container 13th
    The export gas from the export gas container 13 is fed to a combined cycle power plant 24 as fuel, optionally via a buffer tank 25 and optionally a filter 26. The export gas is supplied to a fuel gas compressor 27 and then to the gas turbine 28. The waste heat from the gas turbine is used in the waste heat boiler 29 for a steam cycle 25 with a steam turbine 30.
    The installation and the function of the system according to FIG. 3 after the withdrawal of the export gas from the COREX system are identical to those of FIG. 1. 30
    In Fig. 3, a control valve 72 is additionally provided for export gas 12, with which the amount of export gas 12 can be controlled, which is taken from the COREX © system.
    If the invention is applied to the synthesis gas of a synthesis gas production plant, this takes the place of the plant for the 35th invention in the above embodiments
    23 2010P21665AT • * • · * * · • fr
    Pig iron production. At least part of the synthesis gas then forms the export gas, for which no export gas container 13 is provided, and whose calorific value is regulated by admixing residual gas from a CO 2 separation plant located in the synthesis gas production plant 5. The corresponding system with supply lines 33, 34 for fuel gas and non-combustible gas and power plant 24, then similar for the synthesis gas that of Fig. 1-3 The CO 2 -rich residual gas from the C02-Abscheideanlage means for mixing to 10 export gas means Compressor to the export gas pressure (= synthesis gas pressure) are compressed.
    List of Reference Numerals: 15 1 Blast furnace 2 Sintering plant 3 Oxygen-containing gas 4 Ring line 5 Hot blast 20 6 Reduction gas furnace 7 Slag 8 Pig iron 9 Top or top gas 10 Dust separator or cyclone 25 11 Wet scrubber 12 Export gas 13 Export gas tank 14 PSA plant 15 Compressor 30 16 Aftercooler 17 Pressure gauge 18 Valve 19 Hot torch 20 Residual gas 35 21 Conduit for export gas to hot flare 19 22 Export gas not needed 23 First meter for calorific value measurement 24 Combined cycle power plant
    2010P21665AT 24 · 9 9 • · • #
    * Ft ft ft ft
    25 26 27 28 5 29 30 31 32 10 33 34 35 36 37 15 38 39 40 41 42 20 43 44 45 46 47 25 48 49 50 51 52 30 53 54 55 35 56 57 58 59
    buffer tank
    filter
    Fuel gas compressor
    gas turbine
    waste heat boiler
    steam turbine
    fan
    Line for residual gas to the metallurgical gas network or to
    Hot Torch 19
    Supply line for fuel gas
    Supply line for non-flammable gas
    Expansion turbine second measuring device 36 for calorific value measurement
    Fourth reduction reactor
    Third reduction reactor
    Second reduction reactor
    First reduction reactor
    Fine ore and additives
    Erztrocknung
    reducing gas
    Exhaust gas from reduction reactors 37-40 reduction shaft
    Lump ore, pellets, sinter and additives
    Wet scrubber for exhaust gas 44
    A melting carbine lumpy coal
    Coal in powder form
    Iron briquetting conveyor system designed as a fixed bed reactor storage tank for preheating and reduction of iron oxides and / or iron briquette s
    Generator gas from melter gasifier 48 top gas from wet scrubber 66 third meter for calorific value measurement Topgas from reduction shaft 45 hot metal and slag separators for fine ore
    2010P21665AT 25 ft »« i «ft * ·» «· ί · · * · * · · * *» • * * I I · I · * ftft ♦ * · * < · · · Ft ft · ft · ft · ft ft * ft 60 Wet Scrubber 61 Excess Gas 62 Wet Scrubber 63 Gas Compressor 5 64 gas freed of CO2 (product gas) from PSA plant 14 65 cold iron briquettes 66 Wet scrubber 67 Wet scrubber after reduction shaft 45 68 Wet scrubber after separator for fine ore 59 10 69 Excess gas from COREX® plant 70 Gas compressor after wet scrubber 68 71 Heating unit 72 Control valve for export gas 12 15
    权利要求:
    Claims (10)
    [1]
    26 26 2010P21665AT 1. A method for heating value control of waste gases from pig iron production plants with integrated CO 2 separation plants or for synthesis gas from synthesis gas production plants with integrated 002 -Abscheideanlagen, wherein at least a portion of the exhaust gas or synthesis gas as export gas (12) removed from the plant for pig iron production or synthesis gas production, optionally collected in an export gas container (13) and subsequently thermally utilized in a gas turbine (28), wherein the Exhaust gas from the gas turbine is fed to a waste heat steam generator (29) for generating steam, characterized in that the export gas (12) before the gas turbine (28), in particular optionally before the export gas container (13), depending on the calorific value of the export gas after the residual gas , in particular after the export gas container, at least part of the residual gas (20) from the CO 2 -Abscheideanlage (14) is added, wherein the residual gas content is increased when the calorific value of the export gas (12) rises above a predefined maximum calorific value, and the residual gas content is reduced when the calorific value of the export gas 27 1 2010P21665AT (12) below a predefined minimum Calorific value drops.
    [2]
    2. The method according to claim 1, characterized in that the mixed with residual gas (20) export gas (12) before 5 of the gas turbine (28) passes through a buffer tank (25).
    [3]
    3. The method of claim 1 or 2, characterized in that when falling below the predefined minimum heating value in front of the gas turbine 10 (28) in addition, for example, before and / or after the buffer tank (25), fuel gas (33) is added.
    [4]
    4. The method according to any one of claims 1 to 3, characterized in that when the predefined maximum heating value in front of the gas turbine 15 (28) is additionally added, for example before and / or after the buffer tank (25), non-combustible gas (34) is added ,
    [5]
    5. The method of any of claims 1 to 4, characterized in that in the case of pig iron production 20 that part of the residual gas (20) which is not the export gas (12) is added, the metallurgical gas network, preferably the top gas network, or, a hot flare ( 19) is supplied. 1665AT 28 • «



    Method according to one of claims 1 to 5, characterized in that the export gas (12) contains at least one of the following exhaust gases: - top gas (9) from a blast furnace, in particular from an oxygen blast furnace (1) with Topgasrückführung, - exhaust (61) a melter gasifier (48) of a smelting reduction plant, - exhaust gas (44, 57) from at least one reduction reactor (37-40) or reduction shaft (45) of a smelting reduction plant, - exhaust gas (55) from at least one fixed bed reactor (53) for preheating and / or reduction of iron oxides and / or iron briquettes of a smelting reduction plant, synthesis gas from a synthesis gas production plant, plant for carrying out the process according to one of claims 1 to 6, comprising at least one plant for the production of pig iron with integrated CO 2 separation plant (14) or a plant for syngas production with integrated CO 2 separation plant, - an export gas line, with which a part of the exhaust gas or Synthesega ses as export gas (12) can be removed from the plant for pig iron production or syngas production, 2010P21665AT 29 • ι · • t # * * * * * * * · - optionally an export gas container (13) in which the export gas (12) can be collected, and - a gas turbine (28) in which the export gas (12) can be thermally utilized - a waste heat steam generator (29), in which the exhaust gas from the gas turbine (28) can be used to generate steam, characterized characterized in that the CCk separation plant (14) is connected to the export gas line such that at least part of the residual gas (20) from the CO 2 separation plant (20) in front of the gas turbine (28), in particular optionally before the export gas container (13), is provided to the export gas (12). 14) can be admixed, and that after the addition of residual gas, in particular after the export gas container (13), a measuring device (23) is provided for calorific value measurement of the export gas.
    [6]
    8. Plant according to claim 7, characterized in that optionally after the export gas container (13) and in front of the gas turbine (28), a buffer container (25) is provided.
    [7]
    9. Plant according to claim 7 or 8, characterized in that before and / or after the buffer tank (25) 30 at least one supply line (33) is provided for fuel gas.
    [8]
    10. Installation according to one of claims 7 to 9, characterized in that before and / or after the 5 buffer container (25) at least one supply line (34) is provided for non-combustible gas.
    [9]
    11. Plant according to one of claims 7 to 10, characterized in that in the case of pig iron production, a line (32) for that part of the residual gas, which is not 10 the export gas (12) is added, which in the metallurgical gas network, more preferably Way in the blast furnace network, or in a hot flare (19) opens.
    [10]
    12. Plant according to one of claims 7 to 11, characterized in that at least one conduit is provided, with which - top gas (9) from a blast furnace, in particular from a Sauerstoffhochofen (1) with Topgasrückführung, - exhaust (61) from a Meltdown gasifier (48) of a smelting reduction plant, - waste gas (44, 57) from at least one reduction reactor (37-40) or reduction shaft (45) of a smelting reduction plant, - offgas (55) from at least one fixed bed reactor (53) 2010P21665AT 31 I · · * For the preheating and / or reduction of iron oxides and / or iron briquettes of a smelting reduction plant, synthesis gas from a plant for Synthesis gas production in the export gas line 5 can be passed.
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    同族专利:
    公开号 | 公开日
    CN103415628B|2016-09-14|
    ZA201306721B|2014-12-23|
    AU2012228450C1|2017-01-05|
    CA2830212A1|2012-09-20|
    RU2598062C2|2016-09-20|
    US9222042B2|2015-12-29|
    AU2012228450A1|2013-09-19|
    KR20140012737A|2014-02-03|
    BR112013023800A2|2017-03-01|
    CN103415628A|2013-11-27|
    KR101866929B1|2018-06-14|
    UA110960C2|2016-03-10|
    RU2013146330A|2015-04-27|
    US20140007504A1|2014-01-09|
    WO2012123322A1|2012-09-20|
    AT510273B1|2012-03-15|
    EP2686455B1|2015-03-04|
    EP2686455A1|2014-01-22|
    AU2012228450B2|2016-10-13|
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    法律状态:
    2016-06-15| PC| Change of the owner|Owner name: PRIMETALS TECHNOLOGIES AUSTRIA GMBH, AT Effective date: 20160415 |
    2018-11-15| MM01| Lapse because of not paying annual fees|Effective date: 20180317 |
    优先权:
    申请号 | 申请日 | 专利标题
    AT0036911A|AT510273B1|2011-03-17|2011-03-17|METHOD FOR HEATING CONTROL FOR EXHAUST GASES FROM REPRODUCTION OR SYNTHESEGAS PLANTS|AT0036911A| AT510273B1|2011-03-17|2011-03-17|METHOD FOR HEATING CONTROL FOR EXHAUST GASES FROM REPRODUCTION OR SYNTHESEGAS PLANTS|
    KR1020137027424A| KR101866929B1|2011-03-17|2012-03-08|Process for regulating the joule value of offgases from plants for pig iron production or of synthesis gas|
    AU2012228450A| AU2012228450C1|2011-03-17|2012-03-08|Process for regulating the joule value of offgases from plants for pig iron production or of synthesis gas|
    CN201280013781.7A| CN103415628B|2011-03-17|2012-03-08|For the equipment from pig iron manufacture aerofluxus or the method for adjustment heat value for synthesis gas|
    RU2013146330/02A| RU2598062C2|2011-03-17|2012-03-08|Method of controlling combustion heat of exhaust gases from plants for production of cast iron or for synthetic gas|
    UAA201311034A| UA110960C2|2011-03-17|2012-03-08|process for regulating the joule value of offgases from plants for pig iron or synthesis gas production|
    EP12709054.6A| EP2686455B1|2011-03-17|2012-03-08|Process for regulating the joule value of offgases from plants for pig iron production or of synthesis gas|
    PCT/EP2012/053979| WO2012123322A1|2011-03-17|2012-03-08|Process for regulating the joule value of offgases from plants for pig iron production or of synthesis gas|
    BR112013023800A| BR112013023800A2|2011-03-17|2012-03-08|process for regulating joule value of outgoing gases from pig iron or synthesis gas plants and|
    CA2830212A| CA2830212A1|2011-03-17|2012-03-08|Process for regulating the joule value of offgases from plants for pig iron production or of synthesis gas|
    US14/005,766| US9222042B2|2011-03-17|2012-08-03|Process for regulating joule value of offgases from plants for pig iron production or of synthesis gas|
    ZA2013/06721A| ZA201306721B|2011-03-17|2013-09-06|Process for regulating the joule value of offgases from plants for pig iron production or of synthesis gas|
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