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WO2024237847A1 - Procédé de production de fer fondu ou d'un alliage correspondant à partir de fer réduit direct à faible teneur en carbone dans un four à arc électrique - Google Patents

Procédé de production de fer fondu ou d'un alliage correspondant à partir de fer réduit direct à faible teneur en carbone dans un four à arc électrique Download PDF

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Publication number
WO2024237847A1
WO2024237847A1 PCT/SE2024/050471 SE2024050471W WO2024237847A1 WO 2024237847 A1 WO2024237847 A1 WO 2024237847A1 SE 2024050471 W SE2024050471 W SE 2024050471W WO 2024237847 A1 WO2024237847 A1 WO 2024237847A1
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WO
WIPO (PCT)
Prior art keywords
carbon
dri
slag
eaf
process according
Prior art date
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Pending
Application number
PCT/SE2024/050471
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English (en)
Inventor
Pär LJUNGQVIST
Niklas KOJOLA
Joel CARLSSON
Hedda POUSETTE
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Hybrit Development AB
Original Assignee
Hybrit Development AB
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 Hybrit Development AB filed Critical Hybrit Development AB
Priority to AU2024271891A priority Critical patent/AU2024271891A1/en
Priority to CN202480020748.XA priority patent/CN120958147A/zh
Publication of WO2024237847A1 publication Critical patent/WO2024237847A1/fr
Priority to MX2025011040A priority patent/MX2025011040A/es
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

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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
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
    • C21C5/52—Manufacture of steel in electric 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
    • C21B13/12—Making spongy iron or liquid steel, by direct processes in electric 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
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
    • C21C5/52—Manufacture of steel in electric furnaces
    • C21C5/527—Charging of the electric furnace
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
    • C21C5/56—Manufacture of steel by other methods
    • C21C5/562—Manufacture of steel by other methods starting from scrap

Definitions

  • the present disclosure relates to a process for producing molten iron or an alloy thereof from low-carbon direct reduced iron in an electric arc furnace. More specifically, the disclosure relates to a process for producing molten iron or an alloy thereof from low-carbon direct reduced iron in an electric arc furnace as defined in the introductory parts of the independent claims.
  • Steel is the world's most important engineering and construction material. It is difficult to find any object in the modern world that does not contain steel, or depend on steel for its manufacture and/or transport. In this manner, steel is intricately involved in almost every aspect of our modern lives.
  • the total global production of crude steel is approximately 1 900 million tonnes annually, by far exceeding any other metal, and is expected to reach 2 800 million tonnes in 2050 of which 50% is expected to originate from virgin iron sources.
  • HYBRIT short for HYdrogen BReakthrough Ironmaking Technology - is a joint venture between SSAB, LKAB and Vattenfall, funded in part by the Swedish Energy Agency, and aims to reduce CO2 emissions and decarbonize the steel industry.
  • Central to the HYBRIT concept is a shaft-based direct reduction to produce sponge iron from virgin ore.
  • direct reduction the ore is reduced in a solid-state reduction process at temperatures below the melting point of iron.
  • Shaft-based direct reduction processes utilize pelletized iron ore as the feedstock and produce a porous crude iron product known as sponge iron or direct reduced iron (DRI).
  • H- DR hydrogen direct reduction
  • the hydrogen gas may be produced by electrolysis of water using mainly fossil-free and/or renewable primary energy sources.
  • the critical step of reducing the iron ore may be achieved without requiring fossil fuel as an input, and with water as a by-product instead of CO2.
  • Sponge iron produced by direct reduction is typically subsequently processed in an electric arc furnace in order to melt and refine the crude iron prior to any further secondary metallurgical processing.
  • DRI produced by hydrogen direct reduction H2-DRI
  • H2-DRI hydrogen direct reduction
  • Sponge iron produced using traditional fossil-based carbonaceous reductants typically comprises significant amounts of dispersed carbon (typically up to 5 wt%), due to carbon incorporation from the carbonaceous reducing gas during reduction of the iron ore.
  • the dispersed carbon is predominantly in the form of cementite (FesC), with a lesser proportion consisting of graphite dispersed throughout the sponge iron.
  • the eutectic (melting) temperature of the iron-cementite system is 1147 °C (lower than the melting point of pure iron, 1536 °C), and cementite exothermally dissociates in the molten bath.
  • foaming slag serves to insulate the molten metal bath, leading to improved energy efficiency, decreased consumption of the EAF electrodes, and lesser risk of incorporating undesired nitrogen in the melt.
  • conventional processes typically require a refining stage in the EAF subsequent to melting and prior to tapping, whereby oxygen is provided to the bath until the carbon is brought to acceptable levels.
  • Sponge iron produced by hydrogen direct reduction lacks carbon and therefore is more difficult to melt in the EAF.
  • the localised rate of charging DRI exceeds the melting capacity of the furnace, the accumulation of unmelted mounds (“ferro bergs") of DRI may result, and such ferrobergs may require extended time and electricity consumption in order to be melted and disperse. This decreases the efficiency of the process.
  • the lack of carbon also means that no carbon boil, and therefore no foaming slag, will be obtained without the provision of exogenous carbon.
  • scrap metal may also have a low carbon content, potentially leading to issues regarding melting and carbon boil.
  • the EAF is typically operated with a large excess of carbon in the bath. This ameliorates the problem of lack of carbon boil, but at the cost of needing extensive refining post-melting and pre-tapping in order to drive off the excess carbon.
  • scrap metal is typically loaded as a single batch to the furnace prior to closing the EAF roof and initiating melting of the entire batch.
  • the process is for producing molten iron or an alloy thereof from low-carbon direct reduced iron (DRI) in an electric arc furnace (EAF).
  • DRI comprises less than 0.1 wt% carbon.
  • the process comprises a combined charging and melting stage comprising continuously charging DRI to a molten metal bath in the EAF and concurrently operating the EAF to continuously melt the DRI.
  • DRI DRI
  • electric power carbon
  • oxygen optionally one or more slag formers
  • bath temperature slag composition and offgas composition are determined.
  • a DRI feed rate, an applied power, a carbon feed rate, an oxygen feed rate and a slag former feed rate are adapted in order to maintain the process within the following operational window: bath temperature of from about 1580 °C to about 1750 °C;
  • FeO in slag of from about 25 wt% to about 40 wt%; slag B2 basicity of from about 1.5 to about 3.5, wherein the B2 basicity is calculated as (wt% CaO)/(wt% SiOz);
  • MgO in slag of from about 8 wt% to about 13 wt%; and carbon monoxide (CO) in offgas > 26 Nm 3 /h/m 2 .
  • Fig. 1 a graph plotting a variety of EAF heats in terms of feedstock (C-free or 1.5% C DRI), FeO in slag (%) and DRI feed rate (ton/h). For each heat it is indicated whether a ferroberg was formed or not.
  • Fig. 2 is a graph plotting a variety of EAF heats in terms of feedstock (C-free or 1.5% C DRI), FeO in slag (%) and CO in offgas (Nm 3 /h). For each heat it is indicated whether a adequately foaming slag was obtained or not.
  • the present disclosure relates to a process for producing molten iron or an alloy thereof from low-carbon direct reduced iron (DRI) in an electric arc furnace (EAF).
  • alloy of molten iron it is for example meant molten steel.
  • the process is applicable to any electric arc furnace including AC and DC electric arc furnaces, but may be particularly suited to a three-electrode AC electric arc furnace.
  • the main feedstock for the process is low-carbon DRI, that is to say DRI that comprises less than 0.1 wt% carbon.
  • the DRI may preferably comprise less than 0.05 wt% carbon, and may even more preferably be essentially carbon-free. Such carbon-free DRI may for example be obtained as a product from hydrogen-based direct reduction of iron ore.
  • the DRI may be in the form of pellets, cold-briquetted iron (CBI) or hot-briquetted iron (HBI).
  • CBI cold-briquetted iron
  • HBI hot-briquetted iron
  • the DRI may preferably have an average metallization of greater than or equal to 95 %.
  • Metallization is defined in a manner conventional within the art as ( Fe m etaiiic / Fe to tai) x 100.
  • Metallization was determined herein using X-ray diffractometry (XRD), but may also be determined using other methods. Such other methods include:
  • ISO 10276-1:2000 (Chemical analysis of ferrous materials — Determination of oxygen in steel and iron Part 1: Sampling and preparation of steel samples for oxygen determination) in combination with ISO 10276-2:2003 (Chemical analysis of ferrous materials — Determination of oxygen content in steel and iron — Part 2: Infrared method after fusion under inert gas).
  • the process may use further metallic feedstocks in limited amounts.
  • conventional carbon-containing DRI or scrap metal may be used as up to 20 wt% of the total amount of metallic feedstock, with the balance consisting of low-carbon (or essentially carbon-free) DRI. If such further feedstocks are used, these may be continuously fed to the EAF in the same manner as the low-carbon DRI.
  • the herein disclosed process utilizes a combined charging and melting stage. This is in contrast to conventional EAF processes that more typically have separate charging and melting stages, wherein crude metal is first charged in a batch to the EAF, prior to closing the roof of the EAF and initiating melting by application of power.
  • a combined charging and melting stage entails that DRI is continuously charged to the EAF, and the charging and melting of the DRI are performed concurrently. Initially, after turnaround of the furnace, the EAF may typically contain a "hot-heel" from the previous melt, and this hot heel may assist in melting the initially charged DRI.
  • DRI, electric power, carbon, oxygen and optionally one or more slag formers are provided as inputs to the EAF. The aim is to maintain the process within the following operational window: bath temperature of from about 1580 °C to about 1750 °C;
  • FeO in slag of from about 25 wt% to about 40 wt%; slag B2 basicity of from about 1.5 to about 3.5, wherein the B2 basicity is calculated as (wt% CaO)/(wt% SiO2);
  • MgO in slag of from about 8 wt% to about 13 wt%; and carbon monoxide (CO) in offgas > 26 Nm 3 /h/m 2 .
  • Bath temperature, slag composition and offgas composition may be readily measured or otherwise determined using means and methods conventional in the art.
  • a limit of about > 26 Nm 3 /h/m 2 carbon monoxide in the EAF offgas is found to provide adequate foaming of the slag provided that other parameters are maintained within the specified window.
  • the unit of reference is normal cubic meters carbon monoxide per hour relative to the surface area of the EAF bath in square meters. Electric arc furnaces typically have vertical or near-vertical walls and the surface area of the bath is therefore more-or-less constant during the heat. The bath surface area can easily be calculated from the diameter or other relevant dimensions of the EAF.
  • the carbon monoxide (CO) limit of > 26 Nm 3 /h/m 2 in the offgas is based on a theoretical 100% carbon yield, i.e. that all carbon charged to the process is dissolved in the bath and contributes to either increasing the carbon content of the bath or forming CO by reduction of FeO.
  • a proportion of carbon charged to the EAF will combust without dissolving in the bath and will not contribute to e.g. slag foaming.
  • a typical carbon yield for an effective industrial EAF process is about 75%, and therefore the CO in offgas may be maintained at > 35 Nm 3 /h/m 2 (26/0.75) in order to account for the "non-utilized" carbon.
  • the CO in offgas may be maintained at > 43 Nm 3 /h/m 2 (26/0.6) in order to account for the "non-utilised" carbon.
  • the CO in the offgas may be maintained at less than 150 Nm 3 /h/m 2 , such as less than 120 Nm 3 /h/m 2 , such as less than 90 Nm 3 /h/m 2 , such as less than 60 Nm 3 /h/m 2 . This may assist in avoiding waste of material inputs, and may prevent excessive foaming of the slag.
  • the carbon content of the molten metal bath may be maintained at less than less than 0.7 wt%, such as less than 0.5 wt%, such as less than 0.3 wt%, such as less than or equal to 0.2 wt%.
  • maintaining low carbon in the bath means that there is a diminished or no need for a separate refining stage in order to remove excess carbon. Consequently, shorter tap-to-tap times and further increased productivity may be obtained.
  • the carbon content of the molten metal be determined by direct measurement or determination of bath composition, or may be determined by a differential determination with reference to carbon charged and CO in the offgas.
  • the bath temperature may be maintained at a temperature less than 1700 °C, such as at a temperature less than 1650 °C.
  • Lower bath temperatures may provide increased energy efficiency and result in lower levels of phosphorus impurities in the molten iron.
  • the FeO in the slag may be maintained at from about 30 wt% to about 40 wt%. Within this window there may be a lower tendency to form ferrobergs and the resulting steel may have lower phosphorus impurities.
  • the slag B2 basicity may be maintained at from about 1.5 to about 2.5. Within this window, the resulting steel may have lower phosphorus impurities and a good foaming slag is obtained.
  • the MgO in the slag may be maintained at from about 8 wt% to about 13 wt%. Operating within such a range helps limit refractory wear whilst still providing an adequate slag viscosity, and thereby adequate slag foaming.
  • the charging and melting stage may be complete once the desired level of the molten bath has been reached in the EAF.
  • the various inputs may interact with each other and may affect more than one of the parameters in the operational window. For example, starting from nominal levels of all inputs, the following effects may occur. Increasing the DRI feed rate may tend to decrease the bath temperature, and decreasing the DRI feed rate may tend to increase the bath temperature. Increasing the applied power may tend to increase the bath temperature and decreasing the applied power may tend to decrease the bath temperature. Increasing the carbon feed rate may tend to increase CO in the offgas and decrease FeO in the slag. Decreasing the carbon feed rate may tend to decrease CO in the offgas and increase FeO in the slag.
  • Varying the feed rate of slag formers may increase or decrease the slag B2 basicity, and may increase or decrease the MgO in slag, depending on whether the slag formers comprise CaO, SiO? and/or MgO (or analogues thereof).
  • Each of the inputs may initially be provided at nominal levels and thereafter adjusted based on determination of the various operational parameters.
  • Theoretical nominal feed rates for the various inputs may be calculated as follows.
  • the nominal applied power P nom should be at or close to the maximum appropriate for the system, such as greater than 90% of the maximum rated power, or greater than 95% of the maximum rated power.
  • the DRI feed rate should be adjusted thereafter.
  • a suitable nominal DRI feed rate m DRI - n °m may be determined empirically, or may be calculated using the following equation: wherein ⁇ DR nom j s t ⁇ e nomjna
  • P nom is the nominal applied power in units of energy per unit time (e.g. kW/h)
  • P loss is the estimated system power losses in units of energy per unit time (e.g. kW/h, may e.g. be empirically determined for any given system and nominal power),
  • E DR i-spec j s the specific energy required to melt one unit mass of DRI (e.g. the specific heat required to bring the DRI from ambient to melting temperature, plus the specific heat of melting), expressed in units of energy per unit mass (e.g. kWh/ton).
  • a suitable nominal carbon feed rate may be a carbon feed rate sufficient to provide CO in offgas of > 35 Nm 3 /h/m 2 for an industrial EAF process with good carbon yield. This correlates to approximately 44 kg/h/m 2 CO, which correlates to approximately 19 kg/h/m 2 carbon. For an industrial process having a lower carbon yield, such as about 60%, meaning a required CO in offgas of > 43 Nm 3 /h/m 2 , this correlates to approximately 54 kg/h/m 2 CO, which correlates to approximately 23 kg/h/m 2 carbon.
  • a suitable nominal oxygen feed rate may be an oxygen feed rate sufficient to provide CO in offgas of > 35 Nm 3 /h/m 2 for a typical industrial EAF. This correlates to approximately 18 Nm 3 /h/m 2 .
  • Suitable nominal slag former feed rates will depend on the intrinsic composition of slag formers in the DRI, as well as the nominal feed rate of the DRI.
  • the actual nominal feed rates used may be within a suitable range of these calculated theoretical nominal rates, for example within +/- 20 % of the theoretical nominal rate, such as within +/- 10% of the theoretical nominal rate, such as within +/- 5 % of the theoretical nominal rate.
  • the DRI may be continuously charged to the furnace using means known in the art.
  • the DRI may be continuously charged to the furnace through the EAF roof (e.g. fifth hole) or by side charging.
  • Carbon may be charged to the furnace by top feeding (e.g. through roof of EAF) or by injection into the melt, as known in the art.
  • the carbon may be conventional metallurgical quality carbon (e.g. anthracite) or may be biocarbon. Using biocarbon may provide a steel having lower sulfur levels.
  • Oxygen may be supplied to the furnace using means known in the art, such as using oxygen lances.
  • Slag formers may be charged to the furnace by top feeding or injection, as known in the art.
  • Suitable slag formers may include, but are not limited to, CaO, SiOz, calcined dolomite, and combinations thereof.
  • the autogenous slag formed by melting the DRI may have sufficient properties such that no additional slag formers are required.
  • a tapping stage may be initiated directly. This is in contrast to typical EAF processes that may typically require one or more refining stages in order to burn out oxidisable impurities and remove excess carbon.
  • all material inputs are stopped. Tapping may be conditional on the bath having obtained a suitable tapping temperature, such as greater than or equal to 1600 °C, such as greater than or equal to 1630 °C, such as greater than or equal to 1650 °C. If the bath has not reached the tapping temperature, application of electric power may continue until the appropriate temperature has been reached. Thereafter, the power is stopped and the EAF is tapped of the molten iron or alloy thereof.
  • the outlines of an optimal process window had already been established from previous pilot campaigns using a variety of H2-DRI and NG-DRI materials.
  • the previous pilot campaigns consist of a total of approximately 200 heats to investigate the melting of: hydrogen-reduced DRI pellets (type B) both with and without carbon, hydrogen-reduced HBI (type A) both with and without carbon, DRI pellets produced using conventional natural gas-based reducing gas, and HBI produced using conventional natural gas-based reducing gas.
  • This optimal window had been established to provide good foaming, good productivity (i.e. no ferrobergs), and a stable process (i.e. steady temperature and slag characteristics).
  • the feedstock for each heat was either carbon-free H2-DRI, or, for comparative purposes, H2-DRI that was subsequently carburized using a natural gas-based carburizing gas to a carbon content of approximately 1.5%. All DRI feedstock used was provided by the Hybrit pilot DRI plant. The metallization degree per batch of ingoing DRI for each heat was typically between 90% - 100%.
  • the pilot scale 3-electrode AC electric arc furnace used has a circular diameter of approximately 2.1 m, providing a bath surface area during operation of approximately 3,46 m 2 .
  • Some heats were performed using biocarbon and some performed using anthracite.
  • the carbon was either top-fed or injected, and the carbon used was suitably adapted with regard to e.g. particle size for the specific charge method.
  • biocarbon and anthracite demonstrated similar carbon yields, and the yields obtained by top-feeding and injection were also similar. It was found that heats where biocarbon was used typically had lower final sulfur content in the steel, although sulfur levels were generally acceptable for all heats.
  • Figure 1 is a graph plotting the various heats in terms of feedstock (C-free or 1.5% C DRI), FeO in slag (%) and DRI feed rate (ton/h). For each heat it is indicated whether a ferroberg was formed or not. It can be seen that ferrobergs were formed only when using the C-free DRI feedstock, there were no instances of ferroberg formation when melting carbon-containing DRI. Looking to the heats using carbon-free DRI, it can be seen that FeO in slag is a critical parameter. No ferroberg formation was observed in heats having from about 30% to about 40% FeO in slag, whereas for lower and higher slag FeO proportions ferroberg formation was observed in some heats. For this Figure it can also be seen that within the identified %FeO in slag window, ferroberg formation is relatively insensitive to DRI feed rate, and heats have been performed having relatively high feedrates without ferroberg formation being observed.
  • Figure 2 is a graph plotting the various heats in terms of feedstock (C-free or 1.5% C DRI), FeO in slag (%) and CO in offgas (Nm 3 /h). For each heat it is indicated whether a good foaming was obtained or not. It can be seen that poor foaming tends to be correlated with low CO in offgas ( ⁇ approx. 100 Nm 3 /h) and high FeO in slag (> approx. 37 %). Note that the CO levels indicated in Figure 2 are not corrected for carbon yield.
  • the phosphorous content of the steel was found to decrease with an increasing FeO-content of the slag and with temperature below 1650 °C in the bath. Nitrogen content was in general found to be acceptable. Sulfur content was in general acceptable and varied depending primarily on whether biocarbon or anthracite was used.
  • the optimal process window as defined herein can be derived.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Refinement Of Pig-Iron, Manufacture Of Cast Iron, And Steel Manufacture Other Than In Revolving Furnaces (AREA)
  • Treatment Of Steel In Its Molten State (AREA)
  • Vertical, Hearth, Or Arc Furnaces (AREA)

Abstract

La divulgation concerne un procédé de production de fer fondu ou d'un alliage correspondant à partir de fer réduit direct (DRI) à faible teneur en carbone dans un four à arc électrique (EAF). Le DRI comprend moins de 0,1 % en poids de carbone. Le procédé comprend une étape de chargement et de fusion combinés comprenant le chargement continu de DRI dans un bain de métal fondu dans l'EAF et le fonctionnement simultané de l'EAF pour faire fondre en continu le DRI. Pendant cette étape, le procédé est maintenu dans la fenêtre opérationnelle/température de bain suivantes d'environ 1 580 °C à environ 1 750 °C ; - FeO dans un laitier d'environ 25 % en poids à environ 40 % en poids ; - une basicité B2 de laitier d'environ 1,5 à environ 3,5, la basicité B2 étant calculée en tant que (% en poids de CaO)/(% en poids de SiO2) ; - du MgO dans le laitier d'environ 8 % en poids à environ 13 % en poids ; et - du monoxyde de carbone (CO) dans le gaz d'échappement > 26 Nm3/h/m2.
PCT/SE2024/050471 2023-05-16 2024-05-15 Procédé de production de fer fondu ou d'un alliage correspondant à partir de fer réduit direct à faible teneur en carbone dans un four à arc électrique Pending WO2024237847A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU2024271891A AU2024271891A1 (en) 2023-05-16 2024-05-15 A process for producing molten iron or an alloy thereof from low-carbon direct reduced iron in an electric arc furnace
CN202480020748.XA CN120958147A (zh) 2023-05-16 2024-05-15 用于在电弧炉中由低碳直接还原铁生产铁水或其合金的方法
MX2025011040A MX2025011040A (es) 2023-05-16 2025-09-18 Un proceso para producir hierro fundido o una aleacion de este a partir de hierro reducido directamente de bajo contenido de carbono en un horno de arco electrico

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE2350593-6 2023-05-16
SE2350593A SE547419C2 (en) 2023-05-16 2023-05-16 A process for producing molten iron or an alloy thereof from low-carbon direct reduced iron in an electric arc furnace

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WO2024237847A1 true WO2024237847A1 (fr) 2024-11-21

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PCT/SE2024/050471 Pending WO2024237847A1 (fr) 2023-05-16 2024-05-15 Procédé de production de fer fondu ou d'un alliage correspondant à partir de fer réduit direct à faible teneur en carbone dans un four à arc électrique

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CN (1) CN120958147A (fr)
AU (1) AU2024271891A1 (fr)
MX (1) MX2025011040A (fr)
SE (1) SE547419C2 (fr)
WO (1) WO2024237847A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN119932250B (zh) * 2025-04-09 2025-07-29 河北张宣高科科技有限公司 一种冷态直接还原铁在康斯迪电炉的冶炼方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6875251B2 (en) * 2002-05-15 2005-04-05 Hatch Ltd. Continuous steelmaking process
LU102322B1 (en) * 2020-12-17 2022-06-21 Wurth Paul Sa Green production route for low carbon, low nitrogen steel
CA3221620A1 (fr) * 2021-07-07 2023-01-12 Niklas KOJOLA Briquettes de fer

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6875251B2 (en) * 2002-05-15 2005-04-05 Hatch Ltd. Continuous steelmaking process
LU102322B1 (en) * 2020-12-17 2022-06-21 Wurth Paul Sa Green production route for low carbon, low nitrogen steel
CA3221620A1 (fr) * 2021-07-07 2023-01-12 Niklas KOJOLA Briquettes de fer

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SE2350593A1 (en) 2024-11-17
SE547419C2 (en) 2025-09-23
AU2024271891A1 (en) 2025-09-18
MX2025011040A (es) 2025-10-01
CN120958147A (zh) 2025-11-14

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