EP3541964A1 - Procédé et dispositif de fonctionnement d'un réacteur de réduction directe pour la production de fer à réduction directe à partir de minerai de fer - Google Patents

Procédé et dispositif de fonctionnement d'un réacteur de réduction directe pour la production de fer à réduction directe à partir de minerai de fer

Info

Publication number
EP3541964A1
EP3541964A1 EP17801589.7A EP17801589A EP3541964A1 EP 3541964 A1 EP3541964 A1 EP 3541964A1 EP 17801589 A EP17801589 A EP 17801589A EP 3541964 A1 EP3541964 A1 EP 3541964A1
Authority
EP
European Patent Office
Prior art keywords
gas
reduction reactor
direct
direct reduction
electrolysis cell
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.)
Pending
Application number
EP17801589.7A
Other languages
German (de)
English (en)
Inventor
Alexander Redenius
Ralph Schaper
Simon Kroop
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.)
Salzgitter Flachstahl GmbH
Original Assignee
Salzgitter Flachstahl 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 Salzgitter Flachstahl GmbH filed Critical Salzgitter Flachstahl GmbH
Publication of EP3541964A1 publication Critical patent/EP3541964A1/fr
Pending legal-status Critical Current

Links

Classifications

    • 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
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing 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
    • C21B2100/40—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
    • C21B2100/62—Energy conversion other than by heat exchange, e.g. by use of exhaust gas in energy production
    • 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 present invention relates to a method and an apparatus for operating a direct reduction reactor for the production of direct-reduced iron from iron ore.
  • the inventive method is characterized in comparison to known methods for the production of direct-reduced iron in particular by an increased process economy, characterized in that conventionally required process steps can be saved, and by an environmentally friendly and resource-saving process management.
  • ENERGIRON ZR method (HYL-I Ii method) or obtained by the MIDREX method.
  • lumpy iron ores are reduced by the countercurrent principle of a reducing gas mixture.
  • the main difference between the ENERGIRON ZR process and the MIDREX process is that the reducing gas mixture in the ENERGIRON ZR process is produced by splitting natural gas directly in the ENERGIRON ZR process
  • Direct reduction reactor is generated, while the reduction gas generation in the MIDREX process in a direct reduction reactor upstream
  • the blast furnace gas resulting from the production of direct reduced iron in the direct reduction reactor is quenched and cooled down according to the ENERGIRON ZR method for separating the water contained therein. After a further purification step, the CO2 contained in the blast furnace gas is washed out with the aid of amines.
  • this process is an additional step for the Cleavage of the natural gas used and the recycled, CO2-containing process gas in a separate reformer required.
  • the object of the invention is to provide an alternative method for operating a direct reduction reactor for producing direct-reduced iron and an apparatus for carrying out the method, wherein the
  • resulting CO2 and H2O-containing blast furnace gas is removed from the direct reduction reactor and fed to a high-temperature electrolysis cell in which CO gas generated by co-electrolysis and H2 and oxygen are produced.
  • a device according to the invention is indicated by the features 8 to 9 and a use of the Sythesegases invention produced by claim 10.
  • iron ore as in conventional processes for the production of direct-reduced iron, is transformed from above into a Direct reduction reactor given and contacted in countercurrent with reducing gas, in particular natural gas and / or synthesis gas.
  • reducing gas in particular natural gas and / or synthesis gas.
  • the reducing gas itself is oxidized, essentially to CO2 and H2O, which are removed in the upper part of the reactor as blast furnace gas from this.
  • the CO2 and h O-containing top gas usually contains also still H2, CO, N2 and CH. 4 It has a temperature of about 450 ° C and a pressure of about 6-8 bar.
  • the CO2 and h o-containing top gas after leaving the direct reduction reactor according to the invention is not quenched for the purpose of water removal and not subjected to amine scrubbing for the purpose of CO 2 removal, but the blast furnace gas containing H 2 O and h is introduced in the Process according to the invention fed to a high-temperature electrolysis cell, in which from the CO2 and h O-containing gas by means of co-electrolysis synthesis gas, ie CO and H2, as well as oxygen are generated.
  • the high-temperature electrolysis cell is preferably a solid-oxide electrolysis cell which has an electrolyte which is ion-conductive at higher temperatures, in particular at temperatures above 800-900 ° C.
  • the electrolyte is conductive at the aforementioned temperatures for oxygen ions.
  • the CO2 and H2O-containing blast furnace gas before being fed to the
  • High-temperature electrolysis cell precleaned, e.g. in a facility for
  • Pre-cleaning In the pre-cleaning in particular dust particles are removed, which is why the device for pre-cleaning is preferably a dust filter.
  • the top gas containing CO 2 and H 2 O has a temperature of about 450 ° C. on leaving the direct reduction reactor, it is preferably heated, in particular on, before being fed to the high-temperature electrolysis cell
  • the heating of the CO2 and H2O-containing top gas can be carried out, for example, in a device for reheating, which is connected via a pipeline to the direct reduction reactor.
  • the pressure level of the coming from the direct reduction reactor CO2 and H2O-containing top gas is preferably up to its supply to
  • High-temperature electrolysis cell obtained. These are usually 6-8 bar.
  • the co-electrolysis of optionally prepurified and / or post-heated CO2 and H20-containing top gas preferably at temperatures between 850 and 950 ° C.
  • CO2 and H2O are converted into CO and H2 under the application of electric current.
  • the liberated during the reaction oxygen ions migrate through the
  • Electrolytes which in particular comprises or consists of a solid oxide, and are oxidized to oxygen at the anode.
  • the resulting in a process according to the invention in the high-temperature electrolysis by co-electrolysis of the CO2 and H2O-containing top gas products are thus CO, H2 and O2.
  • the synthesis gas formed in the high-temperature electrolysis cell can
  • the synthesis gas formed at the cathode of the high-temperature electrolysis cell is subsequently fed again as a reducing gas to the direct reduction reactor.
  • Reduction gas are passed into the direct reduction reactor, whereby natural resources are conserved.
  • High-temperature electrolysis cell is converted to CO.
  • the synthesis gas produced in the high-temperature electrolysis cell exhibits at
  • the electrolysis cell preferably at a temperature between 850 and 950 ° C.
  • the synthesis gas is preferably in a device for gas heating heated to about 1000 ° C and passed from there into the reactor.
  • the oxygen produced in the high-temperature electrolysis cell can be any oxygen produced in the high-temperature electrolysis cell.
  • the oxygen can also be used to heat the
  • Direct reduction reactor can be used.
  • the oxygen produced in the high-temperature electrolytic cell is used for heating the device for gas heating, in which the in the
  • Direct synthesis reactor to be introduced synthesis gas and / or natural gas is heated to about 1000 ° C.
  • the device for gas heating preferably one
  • the reducing gas is heated in particular by means of a pure oxygen operated oxyfuel burner, which not only brings the advantage that in this way higher temperatures can be achieved than when combusted with air, but also that no nitrogen in the System is introduced.
  • the exhaust gas produced in the device for gas heating therefore consists essentially of H 2 O and CO 2 in this embodiment and contains no nitrogen oxides. Therefore, the exhaust gas produced in the device for gas heating is preferably also returned to the high-temperature electrolysis cell, optionally after prior reheating.
  • the carbon which is introduced in the form of reducing gas into the direct reduction reactor is therefore preferably circulated in a process according to the invention.
  • the carbon contained in the natural gas and / or CO is converted to CO 2, which is then added again in the high-temperature electrolysis cell CO is reduced and so again together with the H2 also formed as a reducing gas for more
  • Direct reduction reactor is passed.
  • the method according to the invention is also distinguished by a high energy-saving potential.
  • several process steps required by conventional processes can be dispensed with, in particular the cooling of the CO 2 and H 2 O-containing top gas required in the ENERGIRON ZR process for H 2 O removal, the subsequent drying and the amine scrubbing required for the removal of CO 2 or those in the MIDREX Process required steam reforming tion in a separate reformer.
  • the waste heat generated in the process according to the invention is used very efficiently.
  • the CO2 and H20-containing blast furnace which leaves the direct reduction reactor with a temperature of about 450 ° C and a pressure of about 6-8 bar, is not cooled according to the invention, but heated to about 800-1000 ° C while maintaining the pressure level before it is fed to the high-temperature electrolysis cell.
  • the synthesis gas leaving the high-temperature electrolysis cell in the process according to the invention has a temperature of about 900-950 ° C. and only needs to be heated comparatively slightly until it can be returned to the direct reduction reactor at about 1000 ° C.
  • the invention also relates to the use of the synthesis gas generated in a process according to the invention as
  • Reducing agent for the reduction of iron ore in a direct reduction reactor Reducing agent for the reduction of iron ore in a direct reduction reactor.
  • the invention also relates to a device for operating a
  • Direct reduction reactor for the production of direct reduced iron from iron ore, comprising a direct reduction reactor and a high temperature electrolysis cell, wherein the direct reduction reactor is connected to the high temperature electrolysis cell via a pipeline for transporting the synthesis gas.
  • the direct reduction reactor that takes place in connection with the
  • High-temperature electrolysis cell is preferably prepurified and / or reheated, is in the pipeline between the direct reduction reactor and the
  • High-temperature electrolysis cell preferably also arranged a means for pre-cleaning and / or a means for reheating.
  • the optional device for pre-cleaning is in particular a dust filter and the optional device for reheating is preferably adapted to heat the CO2 and H2O-containing blast furnace gas to a temperature above 800 ° C, in particular to about 850-950 ° C.
  • the pipeline by means of which the direct reduction reactor with the
  • a high-temperature electrolysis cell is connected, can therefore in fact consist of several line pieces, e.g. from a line piece between the
  • Line piece between the device for pre-cleaning and the device for reheating and still another line piece between the device for reheating and the high-temperature electrolysis cell.
  • the synthesis gas produced in the high-temperature electrolysis cell is, as
  • the high-temperature electrolysis cell in the device according to the invention is preferably connected via a further pipeline to the direct reduction reactor through which synthesis gas is passed from the high-temperature electrolysis cell into the direct reduction reactor.
  • a device for gas heating is preferably interposed, which can heat the synthesis gas to about 950-1000 ° C.
  • the gas heating can in different ways by means of the following
  • the required heat energy can be provided by means of a heating coil, electric heating coil or other heat-converting apparatus, electric power without any carbon input or carbon emissions at the place of heat generation.
  • the electricity used is generated by means of renewable energy systems, so that no carbon emissions are released even at the place of power generation.
  • the heat energy required can be provided by burning carbon-containing gases supplied from external sources, such as natural gas, biogas or cogeneration gases from conventional steelmaking plants.
  • the required heat energy can be provided by combustion of the synthesis gas produced according to the invention in the high-temperature electrolysis cell.
  • the required heat energy can also be provided by burning coal or pulverized coal.
  • the combustion gas contains comparatively much carbon in the form of CO2, regardless of whether the combustion of the coal / pulverized coal takes place with ambient air or pure oxygen.
  • the gas heating means comprises an oxy-fuel burner which is advantageously operated with low-nitrogen fuels (such as synthesis gas, carbonaceous gases, coal, etc.) to heat the synthesis gas prior to introduction into the reactor.
  • low-nitrogen fuels such as synthesis gas, carbonaceous gases, coal, etc.
  • Oxygen is preferably the oxygen produced in the high-temperature electrolysis cell by co-electrolysis. Accordingly, the
  • High-temperature electrolysis cell connected in this embodiment via a pipe to the oxyfuel burner.
  • Gas heating is effected by means of an oxy-fuel burner, which consists in the device for gas heating exhaust gas consisting essentially of H2O and CO2, and contains no nitrogen in particular, the CO2 and h O-containing exhaust gas can again be supplied to the high-temperature electrolysis cell for the purpose of co-electrolysis.
  • the device for gas heating in this embodiment is connected via a further pipeline to the high-temperature electrolysis cell.
  • the device according to the invention also has a feed device, for example a pipeline or a conveyor belt, for the introduction of a
  • Carbon source in the system Even if the carbon present in the system is recovered according to the invention as CO and so is available for further reduction processes, but always a small proportion of carbon is bound in the direct reduced iron formed and must be replaced from an external source.
  • the feed device opens either directly into the direct reduction reactor or preferably into the device for gas heating.
  • the supply of the required carbon in the direct reduction reactor according to the invention can also be advantageous by the introduction of carbonaceous combustion products for heating the blast furnace gas behind the
  • Direct reduction reactor can be realized before entering the high-temperature electrolysis.
  • the heat required to heat the CO2 and H2O-containing top gas leaving the direct reduction reactor at a temperature of about 450 ° C and heated to about 800-1000 ° C may be provided from the heat sources described above and the
  • FIG. 1 is a process diagram for the production of direct-reduced
  • FIG. 2 shows a process diagram for the production of direct-reduced iron by means of a direct reduction reactor operated by a process according to the invention
  • FIG. 3 shows a process diagram for the production of direct-reduced iron by means of a direct reduction reactor operated according to a further inventive method.
  • FIG. 1 shows a process diagram for the production of direct-reduced iron by means of a conventionally operated direct reduction reactor
  • Direct reduction reactor 1 is given and for reduction in countercurrent with
  • Reduction gas 16 contacted, which previously in a device for
  • Direct reduction reactor 1 is formed by direct-reduced iron 2.
  • the CO 2 and H 2 O-containing head gas 4 formed during the reduction is removed from the reactor 1.
  • the top gas 4 In order to cool the top gas 4 to separate the water contained this is passed through a heat exchanger 17 and then through an air dryer 13.
  • the blast furnace gas After flowing through a process gas compressor 14, the blast furnace gas passes through a CO 2 scrubber 15.
  • the CO and H2-containing gas stream remaining after removal of the CO 2 is preheated in the apparatus for gas heating 9 and then returned to the direct reduction reactor 1.
  • Direct reduction reactor 1 essential process steps of the schematically illustrated in FIG. 1 conventional process for the preparation of
  • FIG. 2 shows the process diagram for carrying out an exemplary method according to the invention. As in the conventional
  • Piping existing pipe 11 is removed from the reactor 1 and, while maintaining the pressure and temperature levels optionally first a means for pre-cleaning 8 supplied, which is preferably a dust filter. Subsequently, the CO2- and h O-containing top gas 4 is further optionally a device for
  • Subsequent heating 12 is supplied, in which it is heated to about 850-950 ° C before it is the high-temperature electrolysis cell 5 is supplied. Instead of the separate one
  • Means for reheating 12, the CO2 and h O-containing top gas 4 can also be heated by the means for gas heating 9 to a temperature of about 850-950 ° C.
  • the device for gas heating 9 heating or fuel gas 18 is supplied.
  • synthesis gas 6 and oxygen 7 are produced by co-electrolysis of the CO 2 and H 2 O-containing top gas 4 at approximately 950 ° C.
  • the synthesis gas 6 is further heated as well as externally supplied reducing gas 16 by means of the gas heating device 9, in particular up to about 1000 ° C, before being passed as reductant for further reduction processes back into the direct reduction reactor 1.
  • FIG. 3 shows a process diagram of a particularly preferred embodiment of the method according to the invention. This differs from the method shown schematically in FIG. 2 essentially in that the oxygen 7 produced in the high-temperature electrolysis cell 5 for heating the synthesis gas 6 by means of an oxy-fuel burner in the device for
  • Gas heating 9 is used. Since the oxy-fuel burner is operated with pure oxygen, the exhaust gas formed in the device for gas heating 9 consists essentially of CO2 and H2O and in particular contains none
  • Nitrogen oxides so that the CO2 and H20-containing exhaust gas 10 from the device for gas heating 9 again for the purpose of new co-electrolysis of high-temperature electrolysis cell 5 can be supplied, optionally after heating in the
  • the CO2 and hO-containing exhaust gas 10 from the device for gas heating 9 can therefore first be combined with the CO2 and H2O-containing blast furnace gas 4 and then the means for reheating 12 are supplied in the gas again is heated to about 850-950 ° C and then the high temperature electrolysis cell 5 is supplied. Because the CO2 cycle is almost closed, significantly less CO2 is released into the atmosphere compared to the state of the art.
  • Embodiments be essential.

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

Abstract

L'invention concerne un procédé de fonctionnement d'un réacteur de réduction directe (1) pour la production de fer (2) à réduction directe à partir de minerai de fer (3), le gaz résiduaire contenant du CO2 et du H2O résultant de la production de fer à réduction directe (2) étant conduit dans une cellule d'électrolyse à haute température, dans laquelle un gaz de synthèse (6) contenant du CO et du H2 ainsi que de l'oxygène sont produits par co-électrolyse.
EP17801589.7A 2016-11-17 2017-10-18 Procédé et dispositif de fonctionnement d'un réacteur de réduction directe pour la production de fer à réduction directe à partir de minerai de fer Pending EP3541964A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016122083.3A DE102016122083A1 (de) 2016-11-17 2016-11-17 Verfahren und Vorrichtung zum Betreiben eines Direktreduktionsreaktors zur Herstellung von direkt reduziertem Eisen aus Eisenerz
PCT/DE2017/100897 WO2018091028A1 (fr) 2016-11-17 2017-10-18 Procédé et dispositif de fonctionnement d'un réacteur de réduction directe pour la production de fer à réduction directe à partir de minerai de fer

Publications (1)

Publication Number Publication Date
EP3541964A1 true EP3541964A1 (fr) 2019-09-25

Family

ID=60421538

Family Applications (1)

Application Number Title Priority Date Filing Date
EP17801589.7A Pending EP3541964A1 (fr) 2016-11-17 2017-10-18 Procédé et dispositif de fonctionnement d'un réacteur de réduction directe pour la production de fer à réduction directe à partir de minerai de fer

Country Status (3)

Country Link
EP (1) EP3541964A1 (fr)
DE (1) DE102016122083A1 (fr)
WO (1) WO2018091028A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102018202594B4 (de) * 2018-02-21 2021-05-06 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur Herstellung von Eisenschwamm insbesondere in einem Direktreduktionsprozess

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7045238B2 (en) * 2003-03-24 2006-05-16 Ion America Corporation SORFC power and oxygen generation method and system
JP5482802B2 (ja) * 2010-01-14 2014-05-07 新日鐵住金株式会社 製鉄方法
EP2973817B1 (fr) * 2013-03-15 2019-01-02 ExxonMobil Research and Engineering Company Intégration de piles à combustible à carbonate fondu dans un traitement de fer et d'acier
DE102013113913A1 (de) * 2013-12-12 2015-06-18 Thyssenkrupp Ag Anlagenverbund zur Stahlerzeugung und Verfahren zum Betreiben des Anlagenverbundes

Also Published As

Publication number Publication date
DE102016122083A1 (de) 2018-05-17
WO2018091028A1 (fr) 2018-05-24

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