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EP2895629A1 - Method for heating process gases for direct reduction plants - Google Patents

Method for heating process gases for direct reduction plants

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Publication number
EP2895629A1
EP2895629A1 EP13762102.5A EP13762102A EP2895629A1 EP 2895629 A1 EP2895629 A1 EP 2895629A1 EP 13762102 A EP13762102 A EP 13762102A EP 2895629 A1 EP2895629 A1 EP 2895629A1
Authority
EP
European Patent Office
Prior art keywords
gas
reduction
unit
enriched
reducing
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP13762102.5A
Other languages
German (de)
French (fr)
Inventor
Hermann WOLFMEIR
Thomas BÜRGLER
Peter Schwab
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.)
Voestalpine Stahl GmbH
Original Assignee
Voestalpine Stahl 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
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First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=50277660&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP2895629(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority claimed from DE201210109284 external-priority patent/DE102012109284A1/en
Priority claimed from DE102013104002.0A external-priority patent/DE102013104002A1/en
Application filed by Voestalpine Stahl GmbH filed Critical Voestalpine Stahl GmbH
Publication of EP2895629A1 publication Critical patent/EP2895629A1/en
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/004—Making spongy iron or liquid steel, by direct processes in a continuous way by reduction from ores
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C37/00—Cast-iron alloys
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22C—ALLOYS
    • C22C38/00—Ferrous alloys, e.g. steel alloys
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0086—Conditioning, transformation of reduced iron ores
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight

Definitions

  • the invention relates to a method for heating process gases for direct reduction plants
  • smelting reduction processes in which the melting process, the reduction gas production and the direct reduction are combined with one another, for example processes of the brands COREX, FINEX, HiSmelt or HiSarna.
  • Iron sponge in the form of HDRI, CDRI or HBI are usually further processed in electric furnace, which is extremely energy-intensive.
  • the direct reduction is carried out by means of hydrogen and carbon monoxide from natural gas (methane) and possibly synthesis gas and coke oven gas.
  • methane is first reacted according to the following reaction:
  • This process thus also emits CO 2 .
  • WO 2011/018124 discloses methods and systems for providing storable and transportable carbon-based energy carriers using carbon dioxide and using regenerative electrical energy and fossil fuels. In this case, a share of regenerative methanol and a proportion of methanol produced by means of non-regenerative electrical energy and / or direct reduction and / or partial oxidation and / or reforming.
  • the reduction process can be represented by the following equation:
  • the object of the invention is to provide a method for heating the process gases in direct reduction plants, with which the heating of the process gases is adapted and optimized better and more flexibly to ei ⁇ nen the energy requirement and the energy provided overall process.
  • the flexibility of the heating process according to the invention is converted to electric heating of the reduction gas or the Re ⁇ formers
  • the electrical energy can be generated from renewable sources and thus be substituted fossil fuels.
  • FIG. 1 shows by way of example the HYL-Energiron method according to FIG.
  • FIG. 2 shows the HYL-Energiron method according to the invention with an electrical heating of the process gas heating
  • FIG. 3 is a highly schematic representation of the MIDREX method
  • FIG. 4 is a highly schematic diagram of an expensive and complex CO 2 -improved MIDREX process according to the state of the art with a CC 2 removal unit (eg VPSA-Vacuum-Pressure Swing Adsorption).
  • the HYL process is in Figure 2 by way of example using a Ka ⁇ capacity of two million tonnes of Direct Reduced Iron (DRI) per year, including an electric arc furnace (EAF, Electro Are Furnace) shown.
  • the process gas from the shaft, in which the iron ore is reduced is first passed through a Wasserab ⁇ separation and then a CC> 2 separation.
  • the circulating gas volume flow here is about 500,000 m 3 per hour ⁇ de.
  • FIG. 3 shows the MIDREX method, in which the exhaust gas in the reduction shaft is likewise removed and divided into a process gas stream and a heating gas stream.
  • the process gas stream is passed through a process gas compressor until natural gas is supplied to it, in particular at a plant which is optionally designed for 2 million tonnes of reduced iron per year, an amount of about 63,000 m 3 natural gas per hour.
  • This process gas passes through a heat exchanger, it is preheated to 600 ° C with the exhaust gases from the reformer and then passes through the reformer and is heated to 980 ° C and is fed as a process gas with the addition of wei ⁇ terem natural gas and oxygen to the shaft again.
  • the heating gas is also removed from the shaft furnace, enriched with natural gas and added to the reformer together with preheated combustion air.
  • the total required Men ⁇ ge of natural gas is about 68,200 m 3 per hour, with about 5.100 m 3 per stun ⁇ de exhaust gas by 52 megawatts of electric power can be compensated for by an electric heater of the reformer. This can save on the one hand 7.5% CO 2 per ton of reduced iron ore.
  • the process is flexible and ser ⁇ ge ⁇ more precisely controlled by the electrical heating.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
  • Materials Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Mechanical Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Manufacture Of Iron (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Environmental & Geological Engineering (AREA)
  • Geology (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Geochemistry & Mineralogy (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Furnace Details (AREA)

Abstract

The invention relates to a method for reducing iron ore using the direct reduction method, wherein the iron ore to be reduced is conducted through a reduction unit such as a shaft furnace and brought into contact with a reduction gas, wherein the reduction gas is introduced into the reduction unit and flows through the unit and is extracted from the unit after flowing through the unit, wherein after exiting the unit the gas is refined and where necessary enriched with new reduction gas fractions and fed back, wherein the reduction gas is heated before entering the reduction unit, characterised in that the heating of the reduction gas before entering the unit takes place electrically.

Description

Verfahren zum Aufheizen von Prozessgasen für Direktreduktions- anlagen  Process for heating process gases for direct reduction plants
Die Erfindung betrifft ein Verfahren zum Beheizen von Prozessgasen für Direktreduktionsanlagen The invention relates to a method for heating process gases for direct reduction plants
Die Stahlerzeugung wird zur Zeit auf unterschiedliche Arten vorgenommen. Die klassische Stahlerzeugung erfolgt über die Erzeugung von Roheisen im Hochofenprozess aus vorwiegend oxi¬ dischen Eisenträgern. Bei diesem Verfahren werden ca. 450 bis 600 kg Reduktionsmittel, zumeist Koks, pro Tonne Roheisen ver¬ braucht, wobei dieses Verfahren sowohl bei der Erzeugung von Koks aus Kohle als auch bei der Erzeugung des Roheisens ganz erhebliche Mengen CO2 freisetzt. Zudem sind sogenannte "Direkt- reduktionsverfahren" bekannt (Verfahren entsprechend der Marken, MIDREX, FINMET, ENERGIRON/HYL , etc.), bei denen aus vorwiegend oxidischen Eisenträgern der Eisenschwamm in der Form von HDRI (Hot Direct Reduced Iron) , CDRI (Cold Direct Reduced Iron) bzw. sogenanntes HBI (hot briquetted iron) erzeugt wird. Steelmaking is currently being carried out in different ways. The classic steel production via the production of pig iron in the blast furnace process of predominantly oxi ¬ Indian iron girders. In this process, about 450 to 600 kg of reducing agent, usually coke per ton of pig iron ver ¬ needs, this process releases both in the production of coke from coal and in the production of pig iron quite significant amounts of CO 2 . In addition, so-called "direct reduction processes" are known (processes according to the trade names, MIDREX, FINMET, ENERGIRON / HYL, etc.), in which predominantly oxidic iron carriers the sponge iron in the form of HDRI (Hot Direct Reduced Iron), CDRI (Cold Direct Reduced Iron) or so-called HBI (hot briquetted iron) is generated.
Zudem gibt es noch sogenannte Schmelzreduktionsverfahren, bei denen der Schmelzprozess, die Reduktionsgaserzeugung und die Direktreduktion miteinander kombiniert werden, beispielsweise Verfahren der Marken COREX, FINEX, HiSmelt oder HiSarna. In addition, there are so-called smelting reduction processes, in which the melting process, the reduction gas production and the direct reduction are combined with one another, for example processes of the brands COREX, FINEX, HiSmelt or HiSarna.
Eisenschwamm in der Form von HDRI , CDRI bzw. HBI werden üblicherweise in Elektroofen weiter verarbeitet, was außerordentlich energieintensiv ist. Die Direktreduktion wird mittels Wasserstoff und Kohlenstoffmonoxid aus Erdgas (Methan) und ggf. Synthesegas auch Koksofengas vorgenommen. Beispielsweise wird beim sogenannten MIDREX-Verfahren zunächst Methan entsprechend der folgenden Reaktion umgesetzt: Iron sponge in the form of HDRI, CDRI or HBI are usually further processed in electric furnace, which is extremely energy-intensive. The direct reduction is carried out by means of hydrogen and carbon monoxide from natural gas (methane) and possibly synthesis gas and coke oven gas. For example In the so-called MIDREX process, methane is first reacted according to the following reaction:
CH4 + C02 2CO + 2H und das Eisenoxid reagiert mit dem Reduktionsgas beispielswei¬ se nach: CH 4 + C0 2 2CO + 2H and the iron oxide reacts with the reducing gas beispielswei ¬ se for:
Fe203 + 6CO(H2) 2Fe + 3C02 (H20) + 3 CO(H2). Fe 2 O 3 + 6 CO (H 2 ) 2 Fe + 3 CO 2 (H 2 O) + 3 CO (H 2 ).
Auch dieses Verfahren stößt somit CO2 aus. This process thus also emits CO 2 .
Aus der DE 198 53 747 Cl ist ein kombinierter Prozess zur Direktreduktion von Feinerzen bekannt, wobei die Reduktion mit Wasserstoff oder einem anderen Reduktionsgas in einer liegenden Wirbelschicht erfolgen soll. From DE 198 53 747 C1 a combined process for the direct reduction of fine ores is known, wherein the reduction is to be carried out with hydrogen or another reducing gas in a horizontal fluidized bed.
Aus der DE 197 14 512 AI ist eine Kraftwerksanlage mit Solar¬ gewinnung, Elektrolyseeinrichtung und einem industriellen Me- tallurgieprozess bekannt, wobei dieser industrielle Prozess entweder die stromintensive Metallherstellung von Aluminium aus Bauxit betrifft oder ein Metallurgieprozess mit Wasser¬ stoff als Reduktionsmittel bei der Herstellung von nichtheißen Metallen wie Wolfram, Molybdän, Nickel oder dergleichen oder ein Metallurgieprozess mit Wasserstoff als Reduktionsmittel unter Anwendung des Direktreduktionsverfahren bei der Herstellung von Eisenmetallen sein soll. Dies wird in dieser Schrift jedoch nicht weiter ausgeführt. From DE 197 14 512 AI a power plant with solar ¬ extraction, electrolysis and an industrial metallurgy process is known, this industrial process either the electricity-intensive metal production of aluminum from bauxite or a metallurgy process with hydrogen ¬ material as a reducing agent in the production of non-ferrous metals such as tungsten, molybdenum, nickel or the like or a metallurgy process with hydrogen as a reducing agent using the direct reduction process in the production of ferrous metals. However, this is not continued in this document.
Aus der WO 2011/018124 sind Verfahren und Anlagen zum Bereitstellen speicherbaren und transportablen kohlenstoffbasierter Energieträger unter Einsatz von Kohlendioxid und unter Einsatz von regenerativer elektrischer Energie und von fossilen Brennstoffen bekannt. Hierbei werden ein Anteil von regenerativ er- zeugtem Methanol und ein Anteil von Methanol bereitgestellt, der mittels nicht regenerativer elektrischer Energie und/oder mittels Direktreduktion und/oder über partielle Oxidation und/oder Reformierung erzeugt wird. WO 2011/018124 discloses methods and systems for providing storable and transportable carbon-based energy carriers using carbon dioxide and using regenerative electrical energy and fossil fuels. In this case, a share of regenerative methanol and a proportion of methanol produced by means of non-regenerative electrical energy and / or direct reduction and / or partial oxidation and / or reforming.
Bei den Direktreduktionsverfahren wird das nach dem Reduktionsschacht austretende Gas nach dessen Reinigung und Abtren¬ nung von Wasser, bei dem HYL-Verfahren zusätzliche C02- Abtrennung, beim MIDREX Verfahren optional zusätzliche C02- Abtrennung zu einem überwiegenden Anteil als Kreislaufgas wieder in den Prozess zurückgeführt. Diesem Gas wird wiederum in der Regel Erdgas zur Bereitstellung von frischem Reduktionsgas zugesetzt. Bei dem HYL-Verfahren wird hierbei das durch die Gasreinigung abgekühlte Gas von etwa 105°C auf etwa 700 bis 1100°C wieder aufgeheizt und anschließend eine partielle Oxi¬ dation mit Sauerstoff durchgeführt. In the direct reduction process the exiting after the reduction shaft gas after its purification and Abtren ¬ voltage of water at the HYL process additional C0 2 - separating, optionally, additional in MIDREX method C0 2 - separation to a predominant proportion as recycle gas back into the process recycled. In turn, this gas is usually added to natural gas to provide fresh reducing gas. In the method according to the HYL-cooled by the gas purge gas is in this case heated from about 105 ° C to about 700 to 1100 ° C again, and then carried out a partial ¬ Oxi-oxidation with oxygen.
Bei dem MIDREX-Verfahren werden CO2 und Wasser mit Erdgas zu H2 und CO in einem beheizten Reformer in einem Temperaturbereich von etwa 700 bis 1100°C umgesetzt. Beiden Verfahren ist jedoch gleich, dass ein Teilstrom des den Reduktionsschacht verlas¬ senden und gereinigten Gases eingesetzt und Erdgas zugesetzt wird . In the MIDREX process, CO 2 and water are converted with natural gas to H 2 and CO in a heated reformer in a temperature range of about 700 to 1100 ° C. However, both methods are the same, that a partial flow of the reduction shaft send out ¬ send and purified gas used and natural gas is added.
Der Reduktionsprozess lässt sich durch die folgende Gleichung darstellen : The reduction process can be represented by the following equation:
(1) Fe203 + 6CO(H2) = 2Fe + 3C02(H20) + 3CO(H2) (1) Fe 2 O 3 + 6 CO (H 2 ) = 2 Fe + 3 CO 2 (H 2 O) + 3 CO (H 2 )
Beim MIDREX-Verfahren finden im Reformer folgende Reaktionen statt : In the MIDREX process, the following reactions take place in the reformer:
(2) CH4 + C02 2CO + 2H2 (2) CH 4 + CO 2 2CO + 2H 2
(3) CH4 + H20 CO + 3H2 Beim HYL-Verfahren findet die folgende Reaktion statt: (3) CH 4 + H 2 OCO + 3H 2 In the HYL method, the following reaction takes place:
(4) CH4 + 2 O2 —► CO + 2H2 (4) CH 4 + 2 O 2 -► CO + 2H 2
Bei beiden Verfahren wird der zusätzlich eingesetzte, fossile Brennstoff, nämlich Erdgas zur Aufheizung der Prozessgase bzw. zur Beheizung des Reformers, verwendet. In both methods, the additionally used, fossil fuel, namely natural gas for heating the process gases or for heating the reformer is used.
Aufgabe der Erfindung ist es, ein Verfahren zum Aufheizen der Prozessgase in Direktreduktionsanlagen zu schaffen, mit welchem das Aufheizen der Prozessgase besser und flexibel an ei¬ nen dem Energiebedarf und der zur Verfügung gestellten Energie angepassten Gesamtprozess angepasst und optimiert ist. The object of the invention is to provide a method for heating the process gases in direct reduction plants, with which the heating of the process gases is adapted and optimized better and more flexibly to ei ¬ nen the energy requirement and the energy provided overall process.
Es ist eine weitere Aufgabe, die CC>2-Emissionen zu reduzieren. It is another task to reduce CC> 2 emissions.
Die Aufgabe wird mit einem Verfahren mit den Merkmalen des Anspruch 1 gelöst. The object is achieved by a method having the features of claim 1.
Vorteilhafte Weiterbildungen sind in Unteransprüchen gekennzeichnet . Advantageous developments are characterized in the subclaims.
Zur Flexibilisierung des Aufheizprozesses wird erfindungsgemäß auf eine elektrische Beheizung der Reduktionsgase bzw. des Re¬ formers umgestellt The flexibility of the heating process according to the invention is converted to electric heating of the reduction gas or the Re ¬ formers
Vorzugsweise kann die elektrische Energie aus erneuerbaren Quellen erzeugt und hiermit fossile Energieträger substituiert werden . Preferably, the electrical energy can be generated from renewable sources and thus be substituted fossil fuels.
Dabei wird vorteilhafterweise die Flexibilität des Prozesses hinsichtlich der eingesetzten Energieträger erhöht dies er- folgt durch kombinierte Beheizung mittels variablen Einsatz von fossilen Energieträgern und elektrische Energie. In this case, the flexibility of the process with regard to the energy sources used is advantageously increased. follows through combined heating by means of variable use of fossil fuels and electrical energy.
Bei der Erfindung ist hierbei von Vorteil, dass elektrischer Strom zu 100 % als Exergie anzusehen ist, so dass dieser voll¬ ständig in Hochtemperaturwärme gewandelt werden kann. Die un¬ mittelbare Wandlungsfähigkeit von elektrischer Energie in Wär¬ me lässt eine hohe Flexibilisierung auch insbesondere im Hin¬ blick auf den Einsatz von kostengünstig am Markt verfügbaren Stromspitzen zu. In the case of the invention, it is advantageous that 100% of electric current is to be regarded as exergy, so that it can be fully converted into high-temperature heat at all times. The un ¬ indirect versatility of electric energy in Wär ¬ me allows high flexibility and especially in Hin ¬ view of the use of available inexpensively on the market current peaks.
Zudem ist von Vorteil, dass Strom aus erneuerbaren Energie¬ quellen wie Wasser, Windkraft oder Sonnenenergie in seiner Entstehung keine CC>2-Emissionen verursacht. In addition, that electricity produced from renewable energy sources ¬ such as water, wind and solar energy in its creation no CC is advantageous causing> 2 emissions.
Die Erfindung wird beispielhaft anhand einer Zeichnung erläu¬ tert. Es zeigen hierbei: The invention is exemplified with reference to a drawing erläu ¬ tert. It show here:
Figur 1 beispielhaft das HYL-Energiron-Verfahren nach dem FIG. 1 shows by way of example the HYL-Energiron method according to FIG
Stand der Technik mit einer erdgasbeheizten Prozessgaserwärmung;  State of the art with a natural gas heated process gas heating;
Figur 2 das HYL-Energiron -Verfahren nach der Erfindung mit einer elektrischen Beheizung der Prozessgaserwärmung; FIG. 2 shows the HYL-Energiron method according to the invention with an electrical heating of the process gas heating;
Figur 3 stark schematisiert das MIDREX-Verfahren; FIG. 3 is a highly schematic representation of the MIDREX method;
Figur 4 stark schematisiert ein teures und aufwändiges CO2- optimiertes MIDREX-Verfahren nach dem Stand der Technik mit einem CC>2-Entfernungsaggregat (z.B. VPSA - Vacuum-Pressure Swing Adsorption) . Der HYL-Prozess wird in Figur 2 beispielhaft anhand einer Ka¬ pazität von zwei Millionen Tonnen Direct Reduced Iron (DRI) pro Jahr inklusive eines Elektrolichtbogenofens (EAF, Electro Are Furnace) gezeigt. Das Prozessgas aus dem Schacht, in dem das Eisenerz reduziert wird, wird zunächst über eine Wasserab¬ trennung und dann eine CC>2-Abtrennung geführt. Der zirkulierende Gasvolumenstrom liegt hierbei bei etwa 500.000 m3 pro Stun¬ de. Diesem Gasstrom werden etwa 72.000 m3 pro Stunde Erdgas zugesetzt, wobei hiervon 56.000 m3 für die Reduktion verwendet werden und hiervon etwa 16.000 m3 für die Prozessgaserhitzung von 105 auf 970°C abgezweigt werden. Dem erhitzten Prozessgas wird anschließend Sauerstoff zugegeben, und dieses dann wieder in den Reduktionsschacht eingeführt. FIG. 4 is a highly schematic diagram of an expensive and complex CO 2 -improved MIDREX process according to the state of the art with a CC 2 removal unit (eg VPSA-Vacuum-Pressure Swing Adsorption). The HYL process is in Figure 2 by way of example using a Ka ¬ capacity of two million tonnes of Direct Reduced Iron (DRI) per year, including an electric arc furnace (EAF, Electro Are Furnace) shown. The process gas from the shaft, in which the iron ore is reduced, is first passed through a Wasserab ¬ separation and then a CC> 2 separation. The circulating gas volume flow here is about 500,000 m 3 per hour ¬ de. About 72,000 m 3 per hour of natural gas are added to this gas stream, of which 56,000 m 3 are used for the reduction and about 16,000 m 3 of which are diverted from 105 to 970 ° C for the process gas heating. The heated process gas is then added oxygen, and then introduced this back into the reduction shaft.
Bei dem erfindungsgemäßen Verfahren (Figur 2) wird das Reduktionsgas ebenfalls aus dem Schacht entnommen und über eine Wasserabtrennung und CC>2-Abtrennung geführt. Durch die elektrische Beheizung der Prozessgasaufwärmung muss lediglich eine Menge von etwa 56.000 m3 pro Stunde Erdgas zugesetzt werden, welches entsprechend der bereits genannten Formeln mit Sauer¬ stoff in CO und Wasserstoff gespalten wird. Aus der Tabelle der Figur 2 erkennt man, dass pro Tonne reduziertem Eisen 21 % CO2 auf diese Weise eingespart werden. Zudem wird der Prozess durch die elektrische Beheizung exakter regelbar und flexibler einset zbar . In the process of the invention (Figure 2), the reducing gas is also removed from the shaft and passed through a water separation and CC> 2 separation. By electrically heating the process gas heating only an amount of about 56,000 m 3 per hour of natural gas must be added, which is cleaved in accordance with the aforementioned formulas with sour ¬ material in CO and hydrogen. It can be seen from the table of FIG. 2 that per tonne of reduced iron 21% CO 2 is saved in this way. In addition, the process becomes more precisely controllable and more flexible by the electric heating.
In Figur 3 ist das MIDREX-Verfahren gezeigt, bei dem das Abgas im Reduktionsschacht ebenfalls entnommen wird und in einen Prozessgasstrom und einen Heizgasstrom aufgeteilt wird. Der Prozessgasstrom wird durch einen Prozessgaskompressor geführt bis ihm Erdgas zugeführt wird, insbesondere bei einer Anlage, die gegebenenfalls auf 2 Mio. Tonnen reduziertes Eisen pro Jahr ausgelegt ist, eine Menge von etwa 63.000 m3 Erdgas pro Stunde. Dieses Prozessgas durchläuft einen Wärmetauscher, in- dem es mit den Abgasen aus dem Reformer auf 600 °C vorgeheizt wird und anschließend den Reformer durchläuft und dabei auf 980°C aufgeheizt wird und als Prozessgas unter Zusatz von wei¬ terem Erdgas und Sauerstoff dem Schacht erneut zugeführt wird. Das Heizgas wird ebenfalls aus dem Schachtofen entnommen, mit Erdgas angereichert und zusammen mit vorgeheizter Verbrennungsluft dem Reformer zugesetzt. Die insgesamt benötigte Men¬ ge an Erdgas beträgt etwa 68.200 m3 pro Stunde, wobei durch eine elektrische Heizung des Reformers etwa 5.100 m3 pro Stun¬ de Abgas durch 52 Megawatt elektrischer Leistung ausgeglichen werden können. Hierdurch können einerseits 7,5 % CO2 pro Tonne reduzierten Eisenerzes eingespart werden. Zudem wird auch die¬ ser Prozess durch die elektrische Beheizung flexibler und ge¬ nauer regelbar. FIG. 3 shows the MIDREX method, in which the exhaust gas in the reduction shaft is likewise removed and divided into a process gas stream and a heating gas stream. The process gas stream is passed through a process gas compressor until natural gas is supplied to it, in particular at a plant which is optionally designed for 2 million tonnes of reduced iron per year, an amount of about 63,000 m 3 natural gas per hour. This process gas passes through a heat exchanger, it is preheated to 600 ° C with the exhaust gases from the reformer and then passes through the reformer and is heated to 980 ° C and is fed as a process gas with the addition of wei ¬ terem natural gas and oxygen to the shaft again. The heating gas is also removed from the shaft furnace, enriched with natural gas and added to the reformer together with preheated combustion air. The total required Men ¬ ge of natural gas is about 68,200 m 3 per hour, with about 5.100 m 3 per stun ¬ de exhaust gas by 52 megawatts of electric power can be compensated for by an electric heater of the reformer. This can save on the one hand 7.5% CO 2 per ton of reduced iron ore. In addition, the process is flexible and ser ¬ ge ¬ more precisely controlled by the electrical heating.
Bei der Erfindung ist von Vorteil, dass eine einfach und rasch einsetzbare Option zur Substitution von fossilen Energieträgern durch Strom aus erneuerbaren Energien geschaffen wird. Zudem werden CC>2-Emissionen von Direktreduktionsanlagen verringert. Darüber hinaus gelingt es, Direktreduktionsanlagen effektiv und flexibel zu betreiben. Insbesondere kann bei einer an die Verfügbarkeit von regenerativen Energien angepasste Stahlerzeugung mit einer elektrisch, und insbesondere mit elektrischem Strom aus erneuerbaren Energien beheizten Pro- zessgasvorwärmung verbessert und aneinander angepasst werden. In the invention, it is advantageous that a simple and rapidly deployable option for the substitution of fossil fuels by electricity from renewable energies is created. In addition, CC> 2 emissions from direct reduction plants are reduced. In addition, it is possible to operate direct reduction plants effectively and flexibly. In particular, in the case of steel production adapted to the availability of regenerative energies, process gas preheating heated electrically and in particular using electricity from renewable energies can be improved and adapted to each other.
Darüber hinaus ist von Vorteil, dass mit einer derartigen Anlage zur Verfügung stehende Stromspitzen kostengünstig genutzt werden können. In addition, it is advantageous that current peaks available with such a system can be used cost-effectively.

Claims

Patentansprüche claims
1. Verfahren zum Reduzieren von Eisenerz im Direktreduktionsverfahren, wobei durch ein Reduktionsaggregat wie einen Reduktionsschacht das zu reduzierende Eisenerz durchge¬ führt wird und mit einem Reduktionsgas in Kontakt ge¬ bracht wird, wobei das Reduktionsgas in das Reduktionsag¬ gregat eingebracht wird und das Aggregat durchströmt und nach dem Durchströmen des Aggregats aus dem Aggregat ab¬ gezogen wird, wobei das Gas nach dem Verlassen des Aggre¬ gats aufbereitet und gegebenenfalls mit neuen Gasantei¬ len angereichert und zurückgeführt wird, wobei das gene¬ rierte Gasgemisch oder die Reduktionsgasprodukte aus dem generierten Gasgemisch vor dem Eintritt in das Reduktionsaggregat auf 700 bis 1100 vorzugsweise 850 bis 1000°C erhitzt werden, dadurch gekennzeichnet, dass die Erhit¬ zung überwiegend insbesondere vollständig elektrisch er¬ folgt . 1. A method for reducing iron ore in the direct reduction process, wherein by a reduction unit as a reduction shaft, the at reducing iron ore Runaway ¬ leads and ge ¬ introduced with a reducing gas in contact, wherein the reducing gas is introduced into the Reduktionsag ¬ gregat and the aggregate flows through and after passing through the aggregate of the aggregate is pulled from ¬, the gas being processed after leaving the gensets ¬ gats and optionally supplemented with new Gasantei ¬ len and recirculated, wherein the gene ¬ tured gas mixture or the reducing gas products from the generated gas mixture be heated to 700 to 1100, preferably 850 to 1000 ° C prior to entry into the reduction unit, characterized in that the Erhit ¬ tion mainly predominantly completely electrically he follows ¬ .
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass zur elektrischen Beheizung Strom aus regenerativer Energiequellen verwendet wird. 2. The method according to claim 1, characterized in that electricity from renewable energy sources is used for electrical heating.
3. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass das Gas nach dem Verlassen des Ag¬ gregats mit Erdgas, Koksofengas oder einem Synthesegas aus Biomasse oder Kohle angereichert wird. 3. The method according to any one of the preceding claims, characterized in that the gas is enriched after leaving the AG ¬ gregats with natural gas, coke oven gas or a synthesis gas from biomass or coal.
4. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass das Gasgemisch mit Sauerstoff ange¬ reichert wird. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass das aus dem Reduktionsschacht abge¬ zogene Gas mit Erdgas, Koksofengas oder einem Synthesegas aus Biomasse oder Kohle angereichert wird, und anschlie¬ ßend aufgeheizt wird. 4. The method according to any one of the preceding claims, characterized in that the gas mixture is enriched ¬ with oxygen. Method according to one of the preceding claims, characterized in that the abge from the reduction shaft ¬ coated gas with natural gas, coke oven gas or a synthesis gas from biomass or coal is enriched, and is subsequently heated ¬ ßend.
Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass das aus dem Reduktionsschacht abge¬ zogene Gas mit Erdgas, Koksofengas oder einem Synthesegas aus Biomasse oder Kohle angereichert wird, und anschlie¬ ßend in einem Reformer umgewandelt wird. Method according to one of the preceding claims, characterized in that the abge from the reduction shaft ¬ coated gas with natural gas, coke oven gas or a synthesis gas from biomass or coal is enriched, and is subsequently converted in a reformer ¬ ßend.
Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass mittels ständiger Evaluierung der Gas- bzw. Strompreise ein kostenoptimierten Einsatz der Energieträger gewährleistet wird. Method according to one of the preceding claims, characterized in that by means of constant evaluation of the gas or electricity prices, a cost-optimized use of the energy carriers is ensured.
EP13762102.5A 2012-09-14 2013-09-10 Method for heating process gases for direct reduction plants Withdrawn EP2895629A1 (en)

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DE201210109284 DE102012109284A1 (en) 2012-09-14 2012-09-28 Producing steel, comprises reducing iron ore with hydrogen, processing the obtained intermediate product from reduced iron ore and optionally metallurgically further processing the impurities
DE102013104002.0A DE102013104002A1 (en) 2013-04-19 2013-04-19 Process for heating process gases for direct reduction plants
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WO2014040990A3 (en) 2014-06-12
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