US20030110891A1 - Iron ore reduction method and installation therefor - Google Patents

Iron ore reduction method and installation therefor Download PDF

Info

Publication number
US20030110891A1
US20030110891A1 US10/275,254 US27525402A US2003110891A1 US 20030110891 A1 US20030110891 A1 US 20030110891A1 US 27525402 A US27525402 A US 27525402A US 2003110891 A1 US2003110891 A1 US 2003110891A1
Authority
US
United States
Prior art keywords
grate
process according
load
zone
gas
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.)
Abandoned
Application number
US10/275,254
Other languages
English (en)
Inventor
Bernard Vanderheyden
Rene Munnix
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.)
Centre de Recherches Metallurgiques CRM ASBL
Original Assignee
Individual
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 Individual filed Critical Individual
Assigned to CENTRE DE RECHERCHES METALLURGIQUES, A.S.B.L. reassignment CENTRE DE RECHERCHES METALLURGIQUES, A.S.B.L. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MUNNIX, RENE, VANDERHEYDEN, BERNARD
Publication of US20030110891A1 publication Critical patent/US20030110891A1/en
Abandoned legal-status Critical Current

Links

Images

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
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0046—Making spongy iron or liquid steel, by direct processes making metallised agglomerates or iron oxide
    • C21B13/0053—On a massing grate
    • 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

Definitions

  • the present invention relates to a process for reducing iron ore and to an installation for implementing it.
  • iron sponge is a ferrous material obtained from iron oxide by a reduction operation referred to as direct reduction operation.
  • Iron oxide is traditionally obtained from ores, in which it is accompanied by various undesirable substances forming the gangue.
  • Another interesting source of iron oxide is also formed by the surface oxides collected at various stages of steel-making processes, such as mill slivers and wash sludges. This category of oxides does not comprise gangue but often contains impurities, such as oil or grease residues.
  • iron ore includes both the customary iron ores and oxides derived from steel-making processes, either separately or in the form of mixtures in any proportions.
  • the present invention relates to a process for manufacturing iron sponge based on the economically acceptable use of a gaseous carbonaceous reducing agent. Moreover, this process more easily fits the framework of respect for environmental norms thanks to the judicious use of the generated gaseous waste.
  • the extremely high productivity of the process of the present invention allows to reduce the impact of the investment pertaining to it when calculating the cost price of the iron sponge produced.
  • a process for reducing iron ores with a view to manufacturing iron sponge, in which a gaseous carbonaceous reducing agent is used is characterised in that a load comprising iron ore is deposited on a grate, in that said grate is displaced in order to move said load into at least 3 separate treatment zones, the first zone comprising an operation for the formation of the load on the grate, the last comprising an operation for unloading the load comprising reduced iron ore from the grate, the intermediate zone or zones comprising, on the one hand, operations for supplying gaseous fluids, referred to as inlet gases, including a hot gaseous carbonaceous reducing agent, and forcing said gaseous flux through the load resting on the grate, and, on the other hand, operations for collecting the gaseous fluids, referred to as exit gases, resulting from said above-mentioned forced passage in such a way that said ore is raised to a temperature between 850° C.
  • inlet gases including a hot gaseous
  • the metallisation rate is the ratio of the percentage of metallic iron (Fe) to the total percentage of iron.
  • grate should be considered as an element for supporting the load of iron ore. Moreover, due to its construction, said grate can, on the one hand, be crossed by a gaseous flux and, on the other hand, serve to transfer the load through the different treatment zones.
  • the load deposited on the grate successively passes through at least one zone in which the temperature of the inlet gas is 450° C. ⁇ 150° C., at least one zone in which the temperature of the inlet gas is 500° C. ⁇ 150° C., at least one zone in which the temperature of the inlet gas is 1200° C. ⁇ 150° C., and at least one zone in which the temperature of the inlet gas is 1000° C. ⁇ 200° C.
  • the load deposited on the mobile grate comprises iron ore, which is preferably hematite that is partially hydrated and appropriately prepared for forming said load.
  • the load deposited on the grate in the loading zone comprises ore mainly made up, in terms of volume, of iron ore sized between 5 mm and 40 mm, preferably between 5 mm and 10 mm.
  • the iron ore can also be incorporated in the load deposited on the mobile grate in the form of pellets or granules, for example.
  • both the pellets and the granules are obtained by a pelletising operation.
  • the pellets have a relatively homogeneous structure in terms of volume, while the granules have an element that acts as a nucleus and serves as a tying base for finer particles.
  • the load deposited on the grate in the loading zone comprises iron ore pellets with a diameter between 5 mm and 20 mm, preferably between 5 mm and 10 mm.
  • the load deposited on the grate in the loading zone comprises iron ore granules with a size between 2 mm and 10 mm, preferably between 4 mm and 7 mm.
  • a layer in the context of the presence of pellets or granules in the load deposited on the grate, a layer, referred to as a protection layer, is deposited on the grate and the load is deposited on said protection layer.
  • the protection layer has a dual role, on the one hand, preventing the passage of the loaded materials through the grate and, on the other hand, avoiding adhesion of the materials making up the load in the case of partial melting of the materials.
  • the protection layer has a thickness between 30 mm and 100 mm, preferably between 40 and 60 mm.
  • the protection layer comprises at least one of the following elements: baked pellets, sized ore that may or may not have been pre-reduced or sized scrap iron, either alone or in combination with one or more of the above-mentioned elements.
  • the protection layer made of constituents with a particle size between 5 mm and 40 mm, preferably between 10 mm and 15 mm.
  • An advantageous procedure for achieving the protection layer consists in using elements issued from what is referred to as “the upper particle size range” resulting from an grinding operation of at least part of the iron ore to be reduced. These elements are “larger” and serve as obstructions in the protection layer to prevent the elements of the load from falling through the mobile grate.
  • a carbonaceous substance preferably coal or coke dust
  • a carbonaceous substance is incorporated into the load deposited on the mobile grate in a proportion between 1 kg and 40 kg of carbon present in said carbonaceous substance per ton of iron ore loaded before reduction.
  • This variant of the composition of the load allows to obtain satisfactory conditions for the reduction of said load of iron ore, i.e. with a metallisation rate at the unloading higher than 60%, even when gas fluxes forced through said load having a low reducing potential, owing for example to the presence of CO2 and/or H2O, are used.
  • the latter serves as a means of transport for successively moving the load deposited within zones in which the conditions are controlled, both with regard to temperature and with regard to the composition of the inlet gases passing through the load.
  • the flux of carbonaceous inlet gases through the load deposited on the grate is directed downwards, preferably by creating a vacuum between 500 and 2000 mm water column underneath the grate.
  • the iron ore heats up on contact with the inlet gases, i.e. those that are drawn through the layer forming the load, and it is successively reduced into magnetite, wustite and finally metallic iron.
  • said load needs to be raised to temperatures between 850° C. and 1300° C., preferably between 1050° C. and 1150° C.
  • the flux of inlet gases forced through the load in at least one treatment zone is formed at least partially by exit gas collected underneath the grate, said collected gas has preferably undergone at least one treatment, such as a scrubbing, a desulphurisation, a drying, a dust-removal, a reheating or a decarbonation operation.
  • the collected gas is not reheated before it is recycled towards a treatment zone in which it is forced through the load, it is advantageously mixed with gas issued from a coal gasification stage with a view to cooling the latter to a useful temperature for passing through the load, i.e. of the order of 1200° C. ⁇ 150° C. or 1000° C. ⁇ 200° C.
  • gas issued from a coal gasification stage with a view to cooling the latter to a useful temperature for passing through the load, i.e. of the order of 1200° C. ⁇ 150° C. or 1000° C. ⁇ 200° C.
  • the flux of inlet gases forced through the load in a zone directly located after the loading zone is at least partially formed by fumes generated by the combustion of exit gas collected underneath the grate
  • said exit gas collected is preferably chosen among the exit gases collected with the lowest reducing potential, e.g. with a low CO content, said collected gas has advantageously undergone at least one scrubbing or dust-removal operation.
  • hot reducing gas is produced from coal in a gasifier and said reducing gas obtained is used to form, at least in part, the gaseous carbonaceous reducing agent, which is forced to pass through the layer forming the load, which is deposited on the mobile grate, said gasifier being preferably supplied either with oxygen-enriched air or tonnage or pure oxygen.
  • the main advantage of using a gasifier in order to generate the reducing gas consists in that it is possible to produce a reduced iron or DRI of very high quality since it has a low content both of gangue and of sulphur. This result is linked with the possibility, both theoretically and physically, to eliminate directly at the level of the gasifier the ashes and sulphur from the coal used in said gasifier, these no longer being present in the DRI obtained on the mobile grate.
  • a hot reducing gas is produced by means of one or more “oxygen/coal” burners in at least one zone for treating the load on the mobile grate, these preferably being zones in which the temperature of the inlet gas is higher than 800° C., said burners using either oxygenated air, pure oxygen or a mixture of the two, preferably supplied with pulverised coal, and said obtained reducing gas is used to form, at least in part, the gaseous carbonaceous reducing agent, which is forced through the layer forming the load, which is deposited on the mobile grate.
  • steam is used to control the temperature of the hot reducing gas produced in a gasifier or by “oxygen/coal” burners during the formation of the flux of gas forced through the load
  • the steam is preferably generated by a steam boiler, the fuel for which is formed, at least in part, by gases emerging from the layer forming the load and collected underneath the mobile grate, said collected exit gases preferably emerge from one or more zones in which the exit gases are too low in CO to be used as reducing gases, by being directly recycled for example, and too rich in CO2 to be decarbonated at low cost, this typically being equivalent to 20% ⁇ % CO ⁇ 40% and 35 ⁇ % CO2 ⁇ 55% on dry gas.
  • the vacuum created underneath the grate and/or the displacement speed of the mobile grate is/are modulated in such a way as to obtain a reduced ore with a metallisation rate between 60% and 100%, preferably between 85% and 95%, in the unloading zone.
  • the reduced ore is commonly called DRI.
  • the DRI obtained on the mobile grate is directly unloaded towards a smelting furnace.
  • the previous embodiment allows to optimise the use of the sensitive heat of the DRI in a significant way since, when it is unloaded, said DRI is at a temperature between 800° C. and 1200° C. Due to this, the operation of direct transfer towards a smelting furnace exerts a favourable influence on the energy balance of said smelting furnace.
  • the following description relates to a preferred embodiment of the process of the invention, in which the mobile grate successively passes through 6 zones, namely a loading zone, four zones for the treatment of the load with a view to reducing the iron ore, and one unloading zone, referred to as zones 1 , 2 , 3 , 4 , 5 and 6 , respectively.
  • zones 1 , 2 , 3 , 4 , 5 and 6 respectively.
  • reference will be made by means of letters and numbers to the sole attached figure, which is merely enclosed as a non-limitative illustration in the sense that some elements can exist within the context of the process that is the subject of the present invention without, however, being shown in the figure or can be shown in the figure without a reference in the text.
  • the different physical states of the iron ore to be reduced have been schematised and identified by the customary chemical formulae. As it passes along the grate, the ore changes from Fe2O3 to Fe2O4, then to FeO and, finally, to Fe.
  • a mobile grate (G) successively passes through a loading zone, four treatment zones, and one unloading zone, a layer comprising iron ore is deposited, preferably continuously and in a constant thickness, on the mobile grate (G) in the first zone (Z 1 ), referred to as the loading zone, in order to form the load (C) to be reduced, the grate (G) is displaced, preferably continuously, so as to move the load (C) by means of the movement of the mobile grate (G) from the loading zone (Z 1 ) to the unloading zone (Z 6 ), successively passing through the treatment zones (Z 2 ), (Z 3 ), (Z 4 ) and (Z 5 ), the temperature of the gaseous flux forced to pass downwards through the load (C) deposited on the mobile grate (G) in zones (Z 2 ) to (Z 5 ) is regulated to 450° C. ⁇ 150° C.
  • the gases emerging underneath the grate (G) from the layer are collected underneath the grate (G) in each of said zones (Z 2 ) to (Z 5 ), and at least part of the gases collected from at least one of the zones (Z 2 ) to (Z 5 ) is recycled towards means that control the gaseous fluxes forced through the load.
  • the load (C) is deposited on the mobile grate (G) and, after the loading phase, undergoes preheating without reduction in one zone, the rest of the heating is then combined with a reduction operation in the following 3 zones until an ore with a metallisation rate of at least 60% is obtained, this involving the recycling of the gases collected underneath the grate (G).
  • a gaseous flux comprising hot reducing gas formed from the gasification of coal into CO and H2, preferably in a pulverised form, in the presence of oxygen and steam is forced through the load (C) arranged on the mobile grate (G) in zones (Z 4 ) and (Z 5 );
  • At least part of the gas emerging underneath the grate (G) is collected in zone (Z 3 ), it is subjected to a scrubbing operation, possibly also to a drying operation, and part is then directed towards a steam generator, in which the collected gas is used as fuel, and another part is directed towards a combustion chamber supplied with a significant excess of air and in which fumes are generated at a temperature of 450° C. ⁇ 150° C., on the one hand, the fumes are introduced into zone (Z 2 ), and, on the other hand, are mixed with exit gases collected in zone (Z 2 ) to obtain a gas at a temperature that is above the acid dew point, the gas obtained being dedusted and then evacuated to the atmosphere via a flue;
  • At least part of the gas emerging underneath the grate in zone (Z 4 ) is collected, it is subjected to a scrubbing operation and possibly a drying operation, and it is recycled, after decarbonation, towards zones (Z 4 ) and (Z 5 ) in order to form at least partly the gaseous flux forced through the layer forming the load (C) in these zones (Z 4 ) and (Z 5 );
  • At least part of the gas emerging underneath the grate in zone (Z 5 ) is collected, it is cooled, possibly by introducing water into it, it is dedusted and it is used in zone (Z 3 ) to form the gaseous fluid forced through the layer forming the load in said zone (Z 3 ).
  • exit gas in zone (Z 4 ) has two significant advantages, said gas serves, on the one hand, to dilute the reducing gas produced by gasification of the coal and to control the temperature of the mixture obtained and, on the other hand, it reduces the consumption of coal by increasing the quantity of reducing gas available per unit weight of coal.
  • FIGURE shows an installation for implementing the process of the present invention according to a preferred embodiment.
  • a grate preferably formed by mobile carriages provided at their bottoms with elements, such as bars, that promote the passage of a gaseous flux, the grate being provided with means for displacing it in the direction of the arrow,
  • [0058] means for defining an atmosphere (A 2 ), preferably a hood (H 2 ),
  • [0059] means for defining an atmosphere (A 3 ), preferably a hood (H 3 ),
  • [0060] means for defining an atmosphere (A 4 ), preferably a hood (H 4 ),
  • [0061] means for defining an atmosphere (A 5 ), preferably a hood (H 5 ),
  • [0074] means for introducing pulverised coal (CP), oxygen (O2) and steam (VP) from the steam generator (V) into (H 4 ) and (H 5 ) in order to produce reducing gas from pulverised coal, oxygen and steam,
  • CP pulverised coal
  • O2 oxygen
  • VP steam
  • [0075] means for supplying (H 4 ) and (H 5 ) with gaseous fluid that is recycled and collected in (R 4 ), then passes into the scrubber (L 2 ), possibly also a dryer, then into the compressor (P 3 ) and finally into the decarbonator (E 1 ),
  • [0076] means for guiding the exit gas collected in (R 2 ), mixing it with fumes emerging from (R) and sending the resulting gas towards a deduster (D 1 ), then towards a flue (O) via an extraction means (P 1 ),
  • [0077] means for guiding the exit gas collected in (R 3 ) so as to send it towards a scrubber (L 1 ), possibly also a dryer, a compressor (P 2 ) and then towards the steam generator (V) or the combustion chamber (R), where it is used as a fuel.
  • a scrubber possibly also a dryer, a compressor (P 2 ) and then towards the steam generator (V) or the combustion chamber (R), where it is used as a fuel.
  • oxy-coal burners (B) are vertically placed in the roof of the hood (H 4 ) and (H 5 ) of zones (Z 4 ) and (Z 5 ) on a number of lines parallel to one another and parallel to the displacement direction of the grate (G).
  • This arrangement allows the ashes produced by the combustion of the coal to settle in grooves, between which the ore forming the load remains “clean” and has better permeability to gases. In this way, a phenomenon of complete or partial clogging of the layer forming the load on the grate by the ashes of the burnt coal is avoided, this phenomenon being highly damageable to the heating and reduction rate of the load (C).
  • Zones (Z 4 ) and (Z 5 ) are equipped with hoods (H 4 ) and (H 5 ), which are provided with oxy-coal burners supplied with pulverised coal, oxygen and steam so as to produce, as a mixture with recycled gas, a hot and highly reducing gas, i.e. at a temperature of 1200° C. in (H 4 ) and 1000° C. in (H 5 ), the flux of which is forced through the load deposited on the grate from the top downwards.
  • the hot reducing gas which is rich in CO and H2 gives rise to an exit gas containing CO2 and H2O derived from the CO and H2, following the reduction process of the iron ore.
  • the exit gas collected in zone (Z 4 ) underneath the grate is recycled in zones (Z 4 ) and (Z 5 ), after having undergone the scrubbing, condensation of the steam and finally decarbonation treatments.
  • the decarbonation is achieved by absorption in a solvent such as methyl diethanolamine and, to this end, the exit gas is compressed at a pressure of around 5 bar absolute, then expanded after treatment, e.g. in a turbine on the same axis as the compressor so as to minimise the energy consumption for the compression by recovering the mechanical power generated during expansion in the turbine.
  • the exit gas collected underneath the grate in zone (Z 5 ) it is generally at a temperature between 500° C. and 1000° C. and, if necessary, it is worthwhile to cool it, by injecting water for example, before proceeding to dust-removal in a multicyclone, and then to recycle it towards zone (Z 3 ), where it acts as an initiator for the reduction of the iron ore layer forming the load by continuing the heating of the latter that has begun in zone (Z 2 ).
  • the exit gas collected underneath the grate in zone (Z 3 ) is first of all scrubbed and dried, then used as a fuel, partly in the boiler for producing steam and partly in the combustion chamber.
  • the fumes produced in the combustion chamber (R) are at a temperature of around 600° C.
  • the process of the invention is particularly advantageous when reducing ores sized within a particle size range from ⁇ 8 mm to ⁇ 40 mm, brought by moderate milling to a particle size around the 5-10 mm fraction with a maximum size of 15 mm and the minimum possible fines of less than 5 mm.
  • the ore ground so as to be 100% ⁇ 15 mm can advantageously be re-screened to 10 mm, for example, in such a way as to separate the 10-15 mm fraction and use it as a constituent of the protection layer that can be deposited on the mobile grate.
  • the ore is preferentially iron ore based on partially hydrated hematite (combined water content of the order of 2% to 6%).
  • the hematite is more suitable for processing than magnetite since it is more reducible, and the effect of the above-mentioned combined water content, after its loss during heating of the load to 600° C. on the grate, is to give rise to a large specific surface area and hence to promote high reactivity.
  • an excessive combined water content has the disadvantage of producing excess crackling of the ore grains, an effect that is deleterious as regards the permeability of the layer and hence deleterious to the productivity of the reduction process.
  • the vacuum applied underneath the grate in order to assist the passage of the gaseous fluid through the layer is typically of the order of 500 to 2000 mm water column.
  • the hoods for guiding the gas into the different zones should operate under a constant relative pressure that is very slightly negative, of the order of ⁇ 2 mm water column, in order to avoid any risk that CO or H2 will escape into the working environment. Moreover, it is clear that any entry of parasitic air into the hoods should be avoided so as to avoid burning the reducing gas present there.
  • the DRI produced on the mobile grate is unloaded in zone (Z 6 ) at a temperature of the order of 1000° C.
  • the thermal self-sufficiency i.e. that the coal used in the process is sufficient both to generate the reducing gas required for the functioning of said reduction process and to supply the heat required both for the production of steam and the preheating of the ore;

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Manufacture Of Iron (AREA)
US10/275,254 2000-05-22 2001-05-17 Iron ore reduction method and installation therefor Abandoned US20030110891A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
BE2000/0340 2000-05-22
BE2000/0340A BE1013448A3 (fr) 2000-05-22 2000-05-22 Procede de reduction de minerais de fer et installation pour sa mise en oeuvre.

Publications (1)

Publication Number Publication Date
US20030110891A1 true US20030110891A1 (en) 2003-06-19

Family

ID=3896537

Family Applications (1)

Application Number Title Priority Date Filing Date
US10/275,254 Abandoned US20030110891A1 (en) 2000-05-22 2001-05-17 Iron ore reduction method and installation therefor

Country Status (9)

Country Link
US (1) US20030110891A1 (fr)
EP (1) EP1287168A1 (fr)
JP (1) JP2003534453A (fr)
KR (1) KR20020091264A (fr)
AU (1) AU2001259967A1 (fr)
BE (1) BE1013448A3 (fr)
BR (1) BR0111363A (fr)
CA (1) CA2407401A1 (fr)
WO (1) WO2001090424A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8287621B2 (en) 2010-12-22 2012-10-16 Nu-Iron Technology, Llc Use of bimodal carbon distribution in compacts for producing metallic iron nodules
JP2013117050A (ja) * 2011-12-05 2013-06-13 Mitsubishi-Hitachi Metals Machinery Inc 部分還元鉄製造方法および部分還元鉄製造装置
US10337076B2 (en) * 2014-02-10 2019-07-02 Primetals Technologies Austria GmbH Pneumatic ore charging
WO2021139136A1 (fr) * 2020-01-09 2021-07-15 中南大学 Procédé de frittage utilisant un milieu gazeux composite vecteur d'énergie et s'accompagnant d'une réduction des émissions

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101712829B1 (ko) * 2014-09-24 2017-03-08 주식회사 포스코 소성로 및 이를 이용한 부분환원철 제조방법

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3264091A (en) * 1963-06-20 1966-08-02 Mcdowell Wellman Eng Co Process for producing highly metallized pellets
US3501288A (en) * 1964-04-30 1970-03-17 Erika Krainer Method of prereducing sinters and pellets
US4023963A (en) * 1974-05-10 1977-05-17 Creusot-Loire Entreprises Process for the direct reduction of minerals on a continuous grate

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR704106A (fr) * 1929-10-14 1931-05-13 Gutehoffnungshuette Oberhausen Procédé et dispositif pour la fabrication d'éponges métalliques
FR1239066A (fr) * 1958-10-29 1960-08-19 Huettenwerk Oberhausen Ag Procédé de traitement d'oxydes métalliques, en particulier d'oxyde de fer, finement granuleux
DE1962417B1 (de) * 1969-12-12 1971-12-30 Huettenwerk Oberhausen Ag Verfahren und Einrichtung zur Vorreduktion von Eisenerzen
FR2197071A2 (en) * 1972-08-24 1974-03-22 Creusot Loire Sponge iron prodn - by hydrogen redn of iron ore
FR2181558A1 (en) * 1972-04-28 1973-12-07 Creusot Loire Sponge iron prodn - by hydrogen redn of iron ore
DE3421878A1 (de) * 1984-06-13 1985-12-19 Klöckner-Humboldt-Deutz AG, 5000 Köln Verfahren und anlage zur kontinuierlichen erzeugung von roheisen

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3264091A (en) * 1963-06-20 1966-08-02 Mcdowell Wellman Eng Co Process for producing highly metallized pellets
US3501288A (en) * 1964-04-30 1970-03-17 Erika Krainer Method of prereducing sinters and pellets
US4023963A (en) * 1974-05-10 1977-05-17 Creusot-Loire Entreprises Process for the direct reduction of minerals on a continuous grate

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8287621B2 (en) 2010-12-22 2012-10-16 Nu-Iron Technology, Llc Use of bimodal carbon distribution in compacts for producing metallic iron nodules
US8690988B2 (en) 2010-12-22 2014-04-08 Nu-Iron Technology, Llc Use of bimodal carbon distribution in compacts for producing metallic iron nodules
JP2013117050A (ja) * 2011-12-05 2013-06-13 Mitsubishi-Hitachi Metals Machinery Inc 部分還元鉄製造方法および部分還元鉄製造装置
US10337076B2 (en) * 2014-02-10 2019-07-02 Primetals Technologies Austria GmbH Pneumatic ore charging
WO2021139136A1 (fr) * 2020-01-09 2021-07-15 中南大学 Procédé de frittage utilisant un milieu gazeux composite vecteur d'énergie et s'accompagnant d'une réduction des émissions

Also Published As

Publication number Publication date
KR20020091264A (ko) 2002-12-05
AU2001259967A1 (en) 2001-12-03
CA2407401A1 (fr) 2001-11-29
BR0111363A (pt) 2003-05-20
JP2003534453A (ja) 2003-11-18
EP1287168A1 (fr) 2003-03-05
BE1013448A3 (fr) 2002-02-05
WO2001090424A1 (fr) 2001-11-29

Similar Documents

Publication Publication Date Title
US9181594B2 (en) Process and device for producing pig iron or liquid steel precursors
US9574247B2 (en) Method and device for operating a smelting reduction process
US5338336A (en) Method of processing electric arc furnace dust and providing fuel for an iron making process
RU2078142C1 (ru) Способ получения чугуна из железосодержащего окисного материала (варианты)
KR19980040225A (ko) 용융선철 및 용융강 예비생성물을 생산하기 위한 방법 및 장치
RU2630136C2 (ru) Способ и устройство для ввода тонкодисперсного материала в псевдоожиженный слой восстановительного агрегата с псевдоожиженным слоем
RU2445377C2 (ru) Способ получения жидкого чугуна или жидких стальных промежуточных продуктов из тонкодисперсного материала, содержащего оксид железа
US3849115A (en) Sintering process
KR19990087540A (ko) 용융선철 또는 용강 중간제품의 생산방법 및 동 생산방법을실행하는 설비
AU2010209883B2 (en) Method and system for producing pig iron or fluid steel pre-products
KR100769794B1 (ko) 고로에서 선철 또는 액상의 1차 강 제품을 생산하기 위한 방법 및 플랜트
US20030110891A1 (en) Iron ore reduction method and installation therefor
CN115491489A (zh) 基于链篦机-回转窑的预还原球团制备装置及方法
KR100240810B1 (ko) 용융선철 또는 강 시제품의 제조방법 및 이를 수행하기 위한 플랜트
CA2775709A1 (fr) Systeme et procede de fabrication de fer metallique
AU727111B2 (en) Method of producing liquid pig iron or liquid steel pre-products
RU2176672C2 (ru) Способ получения губчатого железа
JPS59123707A (ja) 溶融還元炉反応生成ガスの利用方法
CN114921602B (zh) 一种超短流程炼钢装置系统
CN114990274B (zh) 一种粉状铁矿气基/氢基悬浮还原粉状dri装置系统
JPH0723500B2 (ja) 粉状鉱石の溶融還元方法
Buttiens et al. Technologies to reduce environmental burdens. Evolutions in Europe
UC et al. 97lQ2232 Experience and developments in the injection of gases and coal into the QSL reactor at Onsan, Korea
JPH01195224A (ja) 溶銑樋式溶融還元製鉄操業法

Legal Events

Date Code Title Description
AS Assignment

Owner name: CENTRE DE RECHERCHES METALLURGIQUES, A.S.B.L., BEL

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:VANDERHEYDEN, BERNARD;MUNNIX, RENE;REEL/FRAME:013799/0644

Effective date: 20020927

STCB Information on status: application discontinuation

Free format text: EXPRESSLY ABANDONED -- DURING EXAMINATION