WO2011144401A1 - Procédé et dispositif pour le réglage de la température de gaz de procédé provenant d'installations de production de fonte en vue de l'exploitation d'une turbine à cycle d'expansion - Google Patents

Procédé et dispositif pour le réglage de la température de gaz de procédé provenant d'installations de production de fonte en vue de l'exploitation d'une turbine à cycle d'expansion Download PDF

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Publication number
WO2011144401A1
WO2011144401A1 PCT/EP2011/056105 EP2011056105W WO2011144401A1 WO 2011144401 A1 WO2011144401 A1 WO 2011144401A1 EP 2011056105 W EP2011056105 W EP 2011056105W WO 2011144401 A1 WO2011144401 A1 WO 2011144401A1
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WIPO (PCT)
Prior art keywords
gas
process gas
expansion turbine
plant
line
Prior art date
Application number
PCT/EP2011/056105
Other languages
German (de)
English (en)
Inventor
Robert Millner
Kurt Wieder
Original Assignee
Siemens Vai Metals Technologies Gmbh
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 filed Critical Siemens Vai Metals Technologies Gmbh
Priority to CN201180035354.4A priority Critical patent/CN102985567B/zh
Priority to KR1020127033309A priority patent/KR101792486B1/ko
Publication of WO2011144401A1 publication Critical patent/WO2011144401A1/fr

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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
    • 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
    • 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
    • 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
    • C21B5/00—Making pig-iron in the blast furnace
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/06—Making pig-iron in the blast furnace using top gas in the blast furnace process
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B7/00—Blast furnaces
    • C21B7/002—Evacuating and treating of exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
    • 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
    • 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
    • C21B2100/62—Energy conversion other than by heat exchange, e.g. by use of exhaust gas in energy production
    • 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
    • C21B2100/64—Controlling the physical properties of the gas, e.g. pressure or temperature
    • 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
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • 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
    • 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
    • Y02P10/25—Process efficiency

Definitions

  • the blast furnace process first produces pig iron from iron ore using coke.
  • scrap can also be used.
  • steel is produced by further processes from pig iron.
  • the iron ore is used as lump, pellets or sinter together with the reducing agents (usually coke, or coal, for example in the form of a
  • Fine coal indisposition plant Fine coal indisposition plant
  • other constituents limestone, slag formers, etc.
  • the blast furnace is a metallurgical reactor in which the Möllerklax reacts in countercurrent with hot air, the so-called hot blast.
  • 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 Möllerklale and reduces the iron ore.
  • the result is pig iron and slag, which are tapped periodically.
  • oxygen blast furnace which is also referred to as blast furnace with top or top gas recirculation, in the gasification of coke or coal oxygen-containing gas with more than 80% oxygen content (0 2 ) in the blast furnace
  • Top ⁇ or blast furnace gas purification For the emerging from the blast furnace gas, the so-called Top ⁇ or blast furnace gas purification must be provided (eg Dust collectors and / or cyclones in combination with
  • the oxygen blast furnace usually a compressor, preferably with aftercooler, for in the blast furnace
  • Blast furnace methods are a heater for the reducing gas and / or a combustion chamber for 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, so that sufficient cavities remain in the Möllerklale, which ensure the flow through the blown wind.
  • the C0 2 output represents a strong
  • Natural gas sponge iron production (MIDREX, HYL, FINMET) and smelting reduction processes (COREX® and FINEX® processes).
  • a melter gasifier 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) with
  • Reduction gas is reduced, the reducing gas in the melter gasifier by gasification of coal (and
  • a compressor preferably with an aftercooler, for the reducing gas recycled to the reduction reactor
  • the COREX® process is a two-stage process
  • the smelting reduction combines the process of direct reduction (prereduction of iron to sponge iron) with one
  • the process gas which is withdrawn from the process of pig iron production or synthesis gas production, because it can no longer be used there, is often referred to as "export gas.” It is used in particular as a name for that part of the top gas, which deducted from the process of pig iron production , usually cooled, such as in a waste heat boiler, and usually also dedusted, especially dry
  • the gas After dry dedusting and heat extraction from the top gas of a COREX® plant, the gas has a temperature from about 150-250 ° C and a pressure of typically 3 bar g .
  • Dry dedusting and heat extraction in approximately the following composition:
  • the export gas can be compressed, such as by means of one or two-stage centrifugal compressors, and then cooled to produce e.g. be used as fuel gas continue to be used or stored.
  • the export gas after the expansion turbine has a lower pressure and a lower temperature than before the expansion turbine.
  • Expansion turbine with an efficiency of 85 "6 and an associated generator with an efficiency of 97% result - with an export gas composition as above - at the inlet temperatures and pressures given below when entering the expansion turbine, the following
  • Inlet temperature are determined at which just does not take place condensation in the expansion turbine. If the export gas, when entering the expansion turbine, has a lower temperature than this minimum inlet temperature, condensation will occur.
  • the temperature of the export gas before entering into the low-pressure gas storage must be introduced equalization of its amount and its calorific value
  • Low-pressure gas storage can be reduced by direct or indirect cooling. If you join one
  • the export gas should therefore not exceed a maximum export gas temperature.
  • the object is achieved by a method according to claim 1, in that the inlet temperature of the process gas is set on entering the expansion turbine so that it does not fall below a minimum inlet temperature at which condensation occurs in the expansion turbine, and / or that the process gas is cooled such that the process gas leaving the expansion turbine does not exceed a maximum inlet temperature permissible for it when entering a low-pressure gas storage, by at least one of the following measures:
  • Heat recovery steam generator which flows through the process gas before entering the expansion turbine
  • Waste heat recovery system only cooled so far that no components of the process gas condense in the expansion turbine.
  • the waste heat recovery system as part of the plant for pig iron production anyway available to the heat of the hot process gas (about 350-450 ° C) for the
  • Expansion turbine exiting process gas when entering a low-pressure gas storage does not exceed a permissible maximum export gas temperature for this. If necessary, condensation is accepted in the expansion turbine.
  • the process gas is either already before
  • Relaxation turbine cooled, for example by cooling the gas in the waste heat recovery system and / or by admixing cooled further process gas before the expansion turbine and / or by injecting water before the
  • Expansion turbine and / or by injecting water after the expansion turbine and / or by mixing cold residual gas from a plant for C02 ⁇ removal after the expansion turbine. When cooling before the Expansion turbine can then come to condensation in the expansion turbine.
  • this measure means that the inlet temperature of the process gas in the expansion turbine is only controlled to below 175 ° C. Or that the inlet temperature of the process gas is not regulated in the expansion turbine, but the emerging from the expansion turbine process gas is cooled to below 75 ° C.
  • Process gas In addition, however, cooled further process gas can be introduced or water can be injected.
  • this can be realized in such a way that the inlet temperature of the process gas in the expansion turbine is controlled to a value in the range between about 150 ° C to 175 ° C.
  • the waste heat recovery system does not have to be as
  • Heat recovery steam generator be formed. Instead, other heat exchangers can be used. For example, one or more gas-gas heat exchangers
  • Nitrogen or thermal oil to be used indirectly for heating other media Nitrogen or thermal oil to be used indirectly for heating other media.
  • combinations of different waste heat recovery systems are possible.
  • Pig iron production is finally deducted.
  • the plant for the production of pig iron includes here next blast furnace or
  • Exhaust gas from at least one fixed bed reactor in particular for preheating and / or reduction of iron oxides and / or
  • melter gasifier and at least one fixed bed reactor are used to reduce
  • Meltdown gasifier and a plurality of successively connected, designed as fluidized bed reactors reduction reactors.
  • the process or export gas from a smelting reduction plant used for the invention can, of course, be fed from several sources of the smelting reduction plant.
  • Plant parts (melter gasifier, reduction reactor,
  • Pig iron production (blast furnace or smelting reduction plant) can also be removed in other ways from the plant and cooled and mixed as cooled, under pressure further process gas the so-called export gas before the expansion turbine for the purpose of cooling, which are also mixed for the purpose of heating could, for example, if the export or process gas was cooled down too much by the waste heat recovery system and these gas streams were previously cleaned while hot. It makes sense to use that cooled process gas that is obtained in the plant for pig iron anyway in the production of pig iron, such as the purified and cooled reducing gas from a melter gasifier, which has not been passed to the reduction reactor (excess gas).
  • the inlet temperature of the process gas is not below the minimum inlet temperature of about 145 ° C when entering the expansion turbine.
  • the inlet temperature of the process gas is set to a value in the range of 150-175 ° C when entering the expansion turbine. This results in an outlet temperature of the process gas from the
  • the export or process gas can also or additionally
  • the process gas is dry-dedusted in front of the expansion turbine.
  • the dry dedusting takes place anyway in the plant for pig iron production, it must then be installed no own dry dedusting for the expansion turbine.
  • the dry dedusting is typically done by means of bag filter, the waste heat recovery system downstream or by means of ceramic hot gas filters, which are connected upstream of the waste heat recovery system.
  • Fine dedusting bag filter, hot gas filter
  • Dry dust removal has the advantage over wet processes that much less energy is extracted from the process gas, which is to be used in the expansion turbine.
  • the method according to the invention can be embodied such that the plant for producing pig iron with at least one first process gas line for introducing process gas into a
  • Relaxation turbine is connected by a second process gas line with a low-pressure gas storage for process gas, wherein additionally at least one of the following
  • Pig iron production arranged waste heat recovery plant, in particular a heat recovery steam generator plant, wherein the first control device for the waste heat recovery plant is used to control the process gas temperature,
  • the second control device for regulating the amount of process gas, which is passed to the waste heat recovery system, in particular the heat recovery steam generator system, bypassed by means of a bypass line, serves,
  • a third control device with which the amount of cooled, pressurized further process gas from the plant for the production of pig iron, which in the first Process gas line is conducted, regulated,
  • a fourth control device with which the amount of water which can be injected into the first or second process gas line by means of an injection device is regulated
  • a fifth control device with which the amount of cold residual gas from a plant for C02 ⁇ removal is mixed by means of a residual gas line in the second process gas line to the process gas, is regulated.
  • control devices are linked to a central control or one of the control devices, such as the first, takes over the calculation of the setpoints and control values and control of the other control devices.
  • Relaxation turbine are passed, at least one line is provided with which top gas from a blast furnace, in particular from an oxygen blast furnace with
  • Topgas return, in the first process gas line can be passed.
  • At least one line is provided, with which exhaust gas from a
  • Smelting reduction plant can be directed into the first process gas line. It is then provided that
  • At least one of these lines is connected to at least one of the following devices:
  • Fig. 1 shows a COREX® system with bag filters for
  • Fig. 2 shows a COREX® system with ceramic filters for
  • Fig. 3 shows a FINEX® system with bag filters for
  • Fig. 4 shows a FINEX® plant with ceramic filters for
  • Fig. 5 shows an oxygen blast furnace with bag filters for dedusting and downstream expansion turbine.
  • FIG 6 shows an oxygen blast furnace with ceramic filters for dedusting and downstream expansion turbine.
  • a COREX® system is shown. It has, in this example, a reduction shaft 17, which is designed as a fixed bed reactor and is charged with lump, pellets, sinter and additives, see reference number 18.
  • the reducing gas 19 is guided. It is introduced in the lower region of the reduction shaft 17 and exits at its upper side as a top gas 22.
  • the heat of the top gas 22 from the reduction shaft 17 is used in a waste heat boiler 21 for generating steam, the resulting low-pressure steam can a stripper a - not shown here - Appendix 14 for chemical Absorption of CO 2 are supplied.
  • the top gas 22 Before entering the waste heat boiler 21, the top gas 22 can be freed of coarse dust in a dust separator or cyclone 23.
  • the emerging from the waste heat boiler 21 top gas is further purified in a bag filter 30 and fed as export gas 12 of the expansion turbine 34.
  • the reducing gas 19 for the reduction shaft 17 is produced in a melter gasifier 48 into which coal in the form of lumpy coal 49 and optionally coal in powder form is fed, into which the iron ore prereduced in the reduction shaft 17 is added. With the lumpy coal 49 can also fine ore 47, which is too fine for the reduction shaft 17, are introduced.
  • the coal in the melter gasifier 48 is gasified, it produces a gas mixture consisting mainly of CO and H 2 , and withdrawn as a top gas (generator gas) 54 and a partial flow as reducing gas 19 is fed to the reduction shaft 17, after it in a separator 59, the Here is designed as a hot gas cyclone, was cleaned of dust and fine ore.
  • the dust deposited here and the deposited fine ore 25 are returned to the melter gasifier 48.
  • the top gas 54 withdrawn from the melter gasifier 48 is first passed into a separator 59 to separate with discharged dust and the dust 25 - possibly via dust burner - returned to the melter gasifier 48.
  • Part of the top dust 54 cleaned by the coarse dust is further purified by means of wet scrubber 26 and as excess gas 27 taken from the COREX® plant and - according to the invention - the export gas 12 fed to the expansion turbine 34.
  • Expansion turbine 34 are mixed.
  • a portion of the purified top or generator gas 54 after the wet scrubber 26 is supplied to a gas compressor 63 for cooling and then as the cooling gas 28 back to the top or
  • the top gas 22 is injected into the top gas 22 with a first injection device 29 in order to cool it.
  • the top gas 22 enters the bag filter, where the fine dust is separated.
  • the bag filter begins the first process gas line 31 for the export gas 12, which in the
  • Expansion turbine 34 ends.
  • the second process gas line 32 starts at the expansion turbine 34 and ends at
  • Injector 33 is provided to further cool the export gas 12.
  • Topgas 22 can be passed uncooled to the waste heat boiler 21 over.
  • a first control device 45 the processes are controlled in the waste heat boiler 21, but it is also with the connected to other control devices according to the invention, as the dashed lines show:
  • a second control device here in the form of a controllable valve 46, with which the bypass line 36 can be opened or closed completely or partially,
  • the first control device 45 is connected to a first temperature sensor 67, the temperature of the export gas 12 directly before entering the
  • Relaxation turbine 34 measures, with a second
  • Temperature sensor 68 which measures the temperature of the export gas 12 immediately after exiting the expansion turbine 34, and a third temperature sensor 69, the
  • Temperature sensor measures.
  • the setpoint values are then determined and with the aid of the abovementioned
  • Control devices set.
  • Excess export gas can be conveyed before the expansion turbine 34 through a first line 70 and after the expansion turbine 34 through a second line 71 to a flare system 72 and flared there.
  • a portion of the export gas 12 can be passed past a pressure measurement with a pressure sensor 73 by means of a bypass line 74 for the expansion turbine 34 at this. This is in particular for startup and shutdown of the
  • an export gas cooler 75 can still be arranged after the expansion turbine 34, by which the gas mixture of export gas 12 after the expansion turbine 34 and excess gas 27, which was introduced after the expansion turbine 34, is completely or partially cooled.
  • the part to be cooled is removed from the second process gas line 32, passed through the export gas cooler 75 and returned to the second process gas line 32.
  • cold water 76 is used for cooling. If the regulation according to the invention fills in, it can be ensured by means of the export gas cooler 75 that the export gas 12 is not too high
  • Hot gas filter 11 used with ceramic filter elements.
  • hot gas filter elements predominantly in the form of porous candles made of ceramic, fiber ceramics or
  • accumulated dust can be cleaned from the filter cartridges through a backwashing device, which is typically operated with nitrogen 2.
  • the separated in the hot gas filter 11 dust may alternatively be fed back to the melter gasifier 48.
  • a further embodiment variant is that in front of the hot gas filter 11, a cyclone 23, more precisely, a
  • Hot gas cyclone is arranged. As a result, the dust content of the top gas 22 can be further reduced.
  • a FINEX® system instead of the COREX® system of FIGS. 1 and 2, a FINEX® system is used.
  • the export gas 12 is fed to an expansion turbine 34 and then cached again in a formed as a low-pressure gas storage export gas container 13. It can then be a raw material drying or a
  • Power plant can be supplied as fuel, see
  • the FINEX® system has four in this example
  • Fine ore and additives 41 are the
  • Erztrocknung 42 supplied and from there first to the fourth reactor 37, they then get into the third 38, the second 39 and finally the first reduction reactor 40.
  • the fourth reactor 37 instead of four fluidized bed reactors 37-40 but only three may be present.
  • 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 from below into the second reduction reactor 39, it can still with
  • Oxygen O 2 are heated, as well between the second 39 and third 38 reduction reactor.
  • the heat of the exhaust gas 44 from the reduction reactors 37-40 is used in a waste heat boiler 21 for generating steam, the resulting
  • the exiting from the fourth reduction reactor 37 exhaust 44 is cleaned after the waste heat boiler 21 in a bag filter 30.
  • a partial flow of exiting from the bag filter 30 exhaust gas is 12 as the export gas Expansion turbine 34 supplied, another partial flow is to be used as recirculation gas 79 again in the FINEX® method. For this purpose, it is cooled in a gas cooler 77 by means of cold water 78, compressed in the recirculating gas compressor 80, cooled again in a subsequent cooler 81 and then one
  • Vacuum pressure exchange system or chemical absorption.
  • CCS CO 2 Capture and Sequestration
  • the residual gas stream 82 after the chemical absorption 14 mainly contains CO 2 , a portion of the residual gas 82 can through a residual gas line 84, which opens into the second process gas line 32, the export gas 12 before entering the
  • FIG. 3 corresponding fifth control device 20 for this purpose is shown in Fig. 3.
  • the reducing gas 43 is in Fig. 3 in a
  • Melt gasifier 48 produced in the one hand coal in the form of lumpy coal 49 and coal in powder form 50 - this is supplied together with oxygen O 2 - in the other hand, in the reduction reactors 37-40
  • prereduced iron ore formed into hot briquetting 51 into hot briquettes (English: HCl Hot Compacted Iron).
  • 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 may also be added.
  • the coal in the melter gasifier 48 is gasified, it produces a gas mixture consisting mainly of CO and H 2 , and withdrawn as a reducing gas (generator gas) 54 and a
  • the top gas 54 withdrawn from the melter gasifier 48 is first passed into a separator 59 to separate with discharged dust and return the dust via dust burner in the melter gasifier 48.
  • a portion of the top dust purified by the coarse dust is further purified by wet scrubber 60 and supplied as excess gas 61 of the CO 2 chemical absorption unit 14, before the recycle gas compressor 80.
  • Another portion of the purified gas generator 54 is also in a wet scrubber 62 for cooling gas on
  • Iron oxides with dedusted and cooled generator gas 54 are heated and reduced from the melter gasifier 48, emerging top gas 55 is cleaned in a wet scrubber 66 and can then also the system 14 for the removal of CO 2 are supplied.
  • the stripper of the plant 14 can be any suitable material.
  • the stripper of the plant 14 can be any suitable material.
  • Low pressure steam from the waste heat boiler 21 are supplied.
  • the waste heat from the iron production process should be used because of the short distances between waste heat boiler and Appendix 14 to
  • the condensate of the stripper can in this example the
  • the export gas 12 consists only of the exhaust gas 44 of the
  • Control devices (first 45, second 46, fourth 56 and fifth 20) are connected to each other and their manipulated variables are specified centrally.
  • Fig. 4 corresponds substantially to that in Fig. 3, but in Fig. 4 that from the fourth
  • Reduction reactor 37 exiting exhaust 44 before the
  • Waste heat boiler 21 cleaned in a hot gas filter 11 A partial flow of exiting the waste heat boiler 21 exhaust gas is then as export gas 12 of the expansion turbine 34th fed, another partial flow is to be used as recirculation gas 79 again in the FINEX® method.
  • Fig. 5 the invention is illustrated by means of an oxygen blast furnace.
  • iron ore from a sinter plant 2 and coke (not shown) via a charging device from above into the blast furnace 1 is fed.
  • Oxygen-containing gas 3 with an oxygen content> 80% is introduced into the loop 4, as well as coal in powder form 50.
  • Reduction gas furnace 6 reducing gas 5 is heated, wherein for the combustion of oxygen O 2 and combustion air are supplied. Together with cold or preheated oxygen O 2 , the heated reducing gas 5 in the blast furnace 1
  • top or top gas 9 is removed and pre-cleaned in a dust separator or cyclone 10.
  • the purified top or top gas 9 is still so hot that its energy is meaningfully used in a waste heat boiler 21 for steam generation.
  • the left circuit represents the steam cycle
  • the right circuit is used for heating and evaporation of condensate.
  • a first injection device 29 for water is again provided for cooling the top gas 9 in front of the waste heat boiler.
  • top gas 9 can again be passed uncooled around the waste heat boiler 21.
  • the top gas 9 enters after the waste heat boiler 21 in a bag filter 30 (it could be arranged instead of a wet scrubber at this point) and is further cleaned, so that the fine dust is deposited and can be removed, see arrow at the bottom of the Bag filter 30.
  • the purified and optionally cooled top gas 9 can on the one hand taken directly as export gas 12 from the blast furnace system and the expansion turbine 34 and then the
  • Export gas container 13 are supplied. On the other hand, it may be fed to a C02 removal unit 14, wherein the purified and recirculating top or top gas 9 is previously cooled in a gas cooler 77 cooled with cold water 78, followed by a compressor 15 to about 2-6 bar g is compressed and cooled in an aftercooler 16 to about 30- 60 ° C. Only then is the top gas 9 to be recycled introduced into the plant 14 for CO 2 removal.
  • a C02 removal unit 14 wherein the purified and recirculating top or top gas 9 is previously cooled in a gas cooler 77 cooled with cold water 78, followed by a compressor 15 to about 2-6 bar g is compressed and cooled in an aftercooler 16 to about 30- 60 ° C. Only then is the top gas 9 to be recycled introduced into the plant 14 for CO 2 removal.
  • the CO2 purified product gas is used as reducing gas 5 either directly and / or after heating in the
  • the CO2 rich residual gas 82 can discharge as in Fig. 3 directly into the atmosphere and / or just a C02 compression with
  • the residual gas stream consists mainly of CO2 and can therefore be used for
  • part of the residual gas 82 can also be supplied to the reduction gas furnace 6 as fuel gas.
  • a corresponding fifth control device 20 for this purpose is shown in Fig. 4.
  • Control devices (first 45, second 46, fourth 56 and fifth 20) are connected to each other and their manipulated variables are specified centrally.
  • Fig. 6 differs from that in Fig. 5 only by the nature of the cleaning of the top gas 9.
  • Fig. 6 namely the top gas 9 after the dust or
  • Cyclone 10 further purified in a hot gas filter 11, so that the fine dust is separated and can be removed, see arrow at the bottom of the hot gas filter 11.
  • the purified top or top gas 9 is then passed into the waste heat boiler 21.
  • the export gas 12 from the export gas container 13 can - regardless of the embodiment of the invention - a combined cycle power plant or a steam power plant are fed as fuel.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)

Abstract

L'invention présente un procédé et un dispositif pour le réglage de la température de gaz de procédé (12) provenant d'installations de production de fonte en vue de l'exploitation dans une turbine à cycle d'expansion (34), caractérisée en ce que la température d'entrée du gaz de procédé (12) lors de son entrée dans la turbine à cycle d'expansion (34) est réglée de manière telle qu'elle ne passe pas sous une température d'entrée minimale, à laquelle une condensation se produit dans la turbine à cycle d'expansion, et/ou en ce que le gaz de procédé, lors de l'entrée dans un accumulateur de gaz basse pression (13), ne passe pas au-dessus d'une température d'entrée maximale autorisée pour celui-ci. Ainsi, soit le refroidissement du gaz exporté lors de la sortie de la turbine à cycle d'expansion à la température de condensation ou sous celle-ci peut être empêché, soit l'utilisation de refroidisseurs de gaz exporté pour l'introduction du gaz exporté dans un accumulateur de gaz basse pression est évitée.
PCT/EP2011/056105 2010-05-20 2011-04-18 Procédé et dispositif pour le réglage de la température de gaz de procédé provenant d'installations de production de fonte en vue de l'exploitation d'une turbine à cycle d'expansion WO2011144401A1 (fr)

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CN201180035354.4A CN102985567B (zh) 2010-05-20 2011-04-18 调节来自生铁制造设备的用于在膨胀涡轮中使用的工艺气体的温度的方法和装置
KR1020127033309A KR101792486B1 (ko) 2010-05-20 2011-04-18 팽창 터빈에 사용하기 위한 선철 제조용 플랜트로부터 프로세스 가스의 온도를 조절하기 위한 방법 및 장치

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AT0083210A AT509224B1 (de) 2010-05-20 2010-05-20 Verfahren und vorrichtung zur regelung der temperatur von prozessgasen aus anlagen zur roheisenherstellung für die nutzung einer entspannungsturbine
ATA832/2010 2010-05-20

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JP2016505800A (ja) * 2012-12-21 2016-02-25 プライメタルズ テクノロジーズ オーストリア ゲー・エム・ベー・ハーＰｒｉｍｅｔａｌｓ Ｔｅｃｈｎｏｌｏｇｉｅｓ Ａｕｓｔｒｉａ ＧｍｂＨ 還元プロセスにおいて使用される送出ガスを過熱して量変動を補償する方法及び装置
CN109489438A (zh) * 2018-11-30 2019-03-19 中冶南方工程技术有限公司 一种转炉烟气二氧化碳捕集系统及方法

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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
CN105316446B (zh) * 2014-07-30 2017-10-31 宝山钢铁股份有限公司 一种部分替代纯氧的熔融还原炼铁方法
KR101797133B1 (ko) * 2016-08-05 2017-11-13 주식회사 포스코 용철 제조장치 및 용철 제조방법
CN109852424B (zh) * 2019-01-02 2021-04-27 新奥科技发展有限公司 一种煤气化炼铁方法和煤气化炼铁气化炉
CN112921142B (zh) * 2021-01-25 2022-04-12 王文超 一种氢能炼铁式综合回收装置
CN115232897B (zh) * 2022-06-28 2023-05-23 武汉钢铁有限公司 一种高炉软水密闭循环冷却系统调节水量的方法

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US4400184A (en) * 1979-05-18 1983-08-23 Hitachi Shipbuilding And Engineering Company Limited System for recovering pressure and sensible heat from blast furnace gas with use of dry-type dust collector
US4642127A (en) * 1980-08-28 1987-02-10 Sumitomo Metal Industries, Ltd. Method for cooling blast furnace gas in an heat recovery system
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WO2009115365A1 (fr) * 2008-03-17 2009-09-24 Siemens Vai Metals Technologies Gmbh & Co. Procédé et dispositif pour fabriquer des fontes brutes liquides ou des demi-produits liquides en acier
WO2010034791A1 (fr) * 2008-09-26 2010-04-01 Siemens Vai Metals Technologies Gmbh & Co Procédé et dispositif de dépoussiérage et d'épuration à sec d'un gaz produit lors de la fabrication de fonte ou de gazéification de charbon
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JP2016505800A (ja) * 2012-12-21 2016-02-25 プライメタルズ テクノロジーズ オーストリア ゲー・エム・ベー・ハーＰｒｉｍｅｔａｌｓ Ｔｅｃｈｎｏｌｏｇｉｅｓ Ａｕｓｔｒｉａ ＧｍｂＨ 還元プロセスにおいて使用される送出ガスを過熱して量変動を補償する方法及び装置
CN109489438A (zh) * 2018-11-30 2019-03-19 中冶南方工程技术有限公司 一种转炉烟气二氧化碳捕集系统及方法

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AT509224A4 (de) 2011-07-15
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AT509224B1 (de) 2011-07-15
CN102985567B (zh) 2015-01-07
KR101792486B1 (ko) 2017-11-02

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