EP1430159A1 - Procede de reduction d'un materiau particulaire contenant un metal, en particulier contenant du minerai de fer - Google Patents

Procede de reduction d'un materiau particulaire contenant un metal, en particulier contenant du minerai de fer

Info

Publication number
EP1430159A1
EP1430159A1 EP02766919A EP02766919A EP1430159A1 EP 1430159 A1 EP1430159 A1 EP 1430159A1 EP 02766919 A EP02766919 A EP 02766919A EP 02766919 A EP02766919 A EP 02766919A EP 1430159 A1 EP1430159 A1 EP 1430159A1
Authority
EP
European Patent Office
Prior art keywords
reaction zone
reducing gas
particulate material
reduction
temperature
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Withdrawn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
EP02766919A
Other languages
German (de)
English (en)
Inventor
Leopold Werner Kepplinger
Johann REIDETSCHLÄGER
Johannes Schenk
Siegfried Zeller
Konstantin Milionis
Hanspeter Ofner
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.)
Primetals Technologies Austria GmbH
Original Assignee
Voest Alpine Industrienlagenbau GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Voest Alpine Industrienlagenbau GmbH filed Critical Voest Alpine Industrienlagenbau GmbH
Publication of EP1430159A1 publication Critical patent/EP1430159A1/fr
Withdrawn legal-status Critical Current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
    • C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • 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

Definitions

  • the invention relates to a process for the reduction of iron-containing particulate, in particular fine-particulate material in an at least two-stage process, wherein reducing gas is passed through at least two reaction zones connected in series and formed by moving particulate material and the particulate material passes through the reaction zones in reverse order to the reducing gas. wherein the particulate material is heated in the first reaction zone for the particulate material and reduced in the further reaction zone or the further reduction zones.
  • the reducing gas is generated by catalytic reforming of desulfurized and preheated natural gas with superheated steam in a conventional reformer furnace.
  • the reformed gas is then cooled in a heat exchanger and subsequently the H 2 content in the reducing gas is increased by CO conversion using an iron oxide catalyst.
  • the resulting CO and the reformer CO are then removed in a CO 2 scrubber.
  • This gas is mixed with the partially consumed reducing gas (top gas), heated and the fine ore is reduced in three stages (three fluidized bed reactors) in countercurrent.
  • the ore flow begins with drying and subsequent sieving.
  • the ore then goes into a preheating reactor in which natural gas is burned.
  • the fine ore is reduced under increased pressure.
  • direct reduction occurs due to the kinetics of the known methods for magnetite formation, etc. in a layer that grows continuously from the outside inwards and forms on every particle or grain of the iron oxide-containing material. It has been shown in practice that magnetite formation is inhibitory for direct reduction with reducing gas. So it is only possible with increased effort to achieve a more or less complete reduction of the iron oxide-containing material used.
  • the reaction kinetics of magnetite formation are influenced by the composition of the gas and the solid.
  • the molecules of the reducing gas must reach the reaction site from the external gas flow through the adhering gas boundary layer and through the macro and micro pores.
  • the oxygen expansion takes place there.
  • the oxidized gas returns in the same way.
  • the ore grain is thus reduced from the outside in.
  • the porosity increases because the expanded oxygen leaves voids and the original volume of the ore grain hardly shrinks.
  • the reaction front moves into the ore grain from the outside in.
  • the concentration of the reducing gas decreases with dense layers from the outside to the inside.
  • the gas first diffuses from the outside through the already reduced shell to the reaction front, where it reacts and then diffuses back as a reaction product.
  • the phase boundary reaction takes place on the walls of the pores within the reaction front, while the gas can also diffuse inside.
  • the reaction kinetics are inhibited because the reducing gas is prevented from diffusing by this layer and therefore the mass transfer of the reducing gas cannot take place as with porous ore grains.
  • a magnetite layer is formed very quickly, e.g. The faster, the closer the temperature of the iron oxide-containing material is to the limit temperature of about 580 ° C. According to the Baur-Glaessner diagram, this formation of a dense magnetite layer occurs on the surface of an iron ore grain upon contact with the reducing gas predominantly up to a temperature of the iron ore of 580 ° C. At a temperature of the iron ore below 400 ° C, the magnetite formation is slowed down despite contact with the reducing gas, and therefore dense magnetite layers are formed less quickly.
  • this appearance means that there is an increased need for reduction, a higher dust exposure (and thus an increased oxide consumption) and a larger amount of waste.
  • a temperature of the iron oxide-containing material either below 400 ° C or above 580 ° C or a temperature in Range from 400 to 580 ° C, with a temperature setting below 400 ° C, the temperature range between 400 ° C and 580 ° C in the flow direction of the iron oxide-containing material downstream of the first fluidized bed zone within a period of 10 minutes, preferably within 5 minutes, and with one Setting the temperature to above 580 ° C the temperature range between 400 ° C and 580 ° C within a period of a maximum of 10 minutes, preferably 5 minutes, and in addition at a temperature setting in the range of 400 ° C to 580 ° C, the iron oxide-containing material in this temperature range remains for a maximum of 10 minutes, preferably 5 minutes, and is passed on to the next fluidized bed zone immediately after the desired temperature has been reached.
  • the transition of the temperature of the iron oxide-containing material when heated from 400 to 580 ° C. is accomplished in the shortest possible time and a holding in this critical temperature range is avoided. If this temperature range is passed quickly, the magnetite layer formation is extremely low, despite a reducing gas with a high or optimal reduction potential.
  • the invention aims at further developing the method known from WO-A-99/09220 in such a way that the particulate material intended for reduction can be heated to the highest possible preheating temperature in the first reaction zone, but with the formation of phases which are difficult to reduce, such as Magnetite in iron ore can be largely avoided, if not at all, and the disadvantages of such phases described above cannot occur.
  • a time limit for preheating should be avoided, so that the material turnover per unit of time is determined solely by the reduction and not by the preheating.
  • This object is achieved according to the invention for iron ore in that, in order to achieve a maximum preheating temperature, the reducing gas added to the first reaction zone is conditioned, so that no or almost no reduction takes place, but a preheating temperature for the particulate material in the boundary region of the beginning of a reduction is achieved, either the degree of oxidation of the reducing gas is increased or the temperature of the reducing gas is reduced or both measures are carried out together and in the second reactor zone for the iron ore Temperature level of at least about 600 ° C, preferably in the range between 600 and 700 ° C, in particular between 620 and 660 ° C, is set and the iron oxide-containing material is reduced to wustite.
  • the reducing gas added to the first reaction zone is conditioned so that no or almost no reduction takes place, but a preheating temperature for the particulate material is achieved in the boundary region of the beginning of a reduction, whereby either the degree of oxidation of the reducing gas is increased or the temperature of the reducing gas is reduced or both measures are carried out together and in the first reaction zone for the particulate material a maximum reduction rate of 0.2% oxygen breakdown per minute, preferably 0.05% oxygen breakdown per minute, is observed.
  • This process is particularly suitable for the use of iron ore.
  • a higher preheating temperature than that of the prior art can be achieved, which can even be so high that a reduction would take place by means of the preheating reducing gas - if untreated - but this is prevented by increasing the degree of oxidation of the reducing gas. It is essential according to the invention that the particulate material is heated to a preheating temperature which is in the border area of the beginning of a reduction caused by the preheating gas.
  • the temperature level and the degree of oxidation are preferably set independently of fresh reducing gas used for the reduction of the particulate material, ie. H. while avoiding any influence on the chemical composition and the temperature of the reducing gas freshly added to the particulate material for final reduction.
  • the method according to the invention is particularly suitable for particle-shaped material, etc. for material with a particle size up to 12 mm, preferably up to 10 mm, either in the form of monograin or in the form of grain belt.
  • the process according to the invention allows a temperature level between 350 ° and 550 ° C., preferably between 400 and 470 ° C., to be set in the first reaction zone.
  • the temperature level in the first reaction zone for the particulate material is advantageously set by injecting H 2 O in liquid and / or vapor form into this reaction zone and / or into the reducing gas supplied to this reaction zone.
  • the temperature level is set in the first reaction zone for the particulate material by adding cold gas into this reaction zone and / or into the reducing gas supplied to this reaction zone, such as by adding cold CO 2 and / or cold reducing gas.
  • a further expedient embodiment is characterized in that the degree of oxidation of the reducing gas is adjusted in the first reaction zone for the particulate material by supplying vaporous and / or liquid H 2 O into this reaction zone and / or into the reducing gas supplied to this reaction zone.
  • the degree of oxidation of the reducing gas in the first reduction zone for the particulate material can also be set by injecting CO 2 and / or CO 2 / H 2 O mixtures into this reaction zone and / or into the reducing gas supplied to this reaction zone.
  • an average residence time for the particulate material of up to 40 minutes, preferably up to 30 minutes, can be maintained in the first reaction zone for the particulate material and a temperature level between 760 and 850 ° C., preferably in the last reaction zone for the iron ore in the range of 770 and 800 ° C.
  • the latter measures prevent "sticking" - caking of the particles that remain in the fluidized bed when iron ore is reduced by sponge iron.
  • the invention is expediently implemented by one or more of the following measures:
  • the cooling gas exiting from the reaction zone downstream of the first reaction zone for the particulate material is only partially introduced into the first reaction zone after cooling and washing, and the reducing gas emerging from the first reaction zone for the particulate material is expediently at least partially introduced into the first reaction zone recirculated.
  • the aim is that the CO content of the reducing gas is less than 20%, preferably in a range between 4 and 10%, and that in the first reaction zone for the particulate iron ore for the reducing gas, a steam-carbon ratio in the range of 2 , 5 to 5, preferably in the range 2.5 to 4, is set.
  • the temperature in the reaction zones is advantageously cooled, preferably by regulating the temperature of the reducing gas and / or by H 2 O or CO 2 injection.
  • FIG. 1 illustrates a process diagram according to a preferred embodiment.
  • 2 shows the Baur-Glaessner diagram, in which the course of the reduction is shown without measures according to the invention and with measures according to the invention.
  • 3 a and 3 b illustrate reduction processes using a hematite grain. •
  • the first fluidized bed reactor 1 has four fluidized bed reactors 1 to 4 connected in series, with iron oxide-containing material, such as fine ore, being fed via an ore feed line 5 to the first fluidized bed reactor 1, in which heating to a predetermined temperature takes place, as will be explained in more detail later is performed.
  • the fine ore e.g. with a chemical composition according to the table below, passed from fluidized bed reactor to fluidized bed reactor via conveying lines 6, fluidized bed zones being formed in each of the fluidized bed reactors 1 to 4.
  • the finished reduced material sponge iron
  • the fine ore Before the fine ore is introduced into the first fluidized bed reactor 1, it is subjected to an ore preparation, such as drying and sieving, which is not shown in detail.
  • Reducing gas is conducted in countercurrent to the ore flow from the fluidized bed reactor 4 to the fluidized bed reactor 3 to 1 and is discharged as top gas via a top gas discharge line 8 from the last fluidized bed reactor 1 in the gas flow direction and cooled and washed in a wet scrubber 9.
  • the reduction gas is produced by reforming natural gas supplied via line 11 and desulfurized in a desulfurization system 12 in a reformer 10.
  • the gas formed from natural gas and steam and leaving reformer 10 essentially consists of H 2 , CO, CH 2 , H 2 O and CO 2 .
  • This reformed natural gas is fed via the reformed gas line 13 to one or more heat exchangers 14, in which it is cooled to 80 to 150 ° C., as a result of which water is condensed out of the gas.
  • the reformed gas line 13 opens into the top gas line 8 after the top gas has been compressed by means of a compressor 15.
  • the mixed gas thus formed is passed through a CO 2 scrubber 16 and freed of CO 2 and H 2 S. It is now available as a reducing gas.
  • This reducing gas is heated via a reducing gas feed line 17 in a gas heater 18 arranged downstream of the CO 2 scrubber 16 to a reducing gas temperature of approximately 840 ° C. and fed to the first fluidized bed reactor 4 in the gas flow direction, where it reacts with the fine ores to produce direct-reduced iron.
  • the fluidized bed reactors 4 to 1 are connected in series; the reducing gas passes from the fluidized bed reactor to the fluidized bed reactor via the connecting lines 19.
  • the number of fluidized bed reactors depends on the circumstances, such as the properties of the reducing gas, the desired reduction gradient, etc. For example, the fluidized bed reactor 3 shown in broken lines could be eliminated, so that the process proceeds in three stages.
  • top gas Part of the top gas is removed from the gas cycle 8, 17, 19 in order to avoid an enrichment of inert gases, such as ⁇ 2 .
  • the discharged top gas is fed via a branch line 20 to the gas heater 18 for heating the reducing gas and burned there. Any missing energy is supplemented by natural gas, which is supplied via the feed line 21.
  • the sensible heat of the reformed natural gas emerging from the reformer 10 and of the reformer fumes is used in a recuperator 22 to preheat the natural gas after passing through the desulfurization system 12, to generate the steam required for the reforming and to supply the gas heater 18 via line 23 Preheat the combustion air and possibly also the reducing gas.
  • the combustion air supplied to the reformer 10 via the line 24 is also preheated.
  • the reduction process is carried out according to a first preferred variant as follows:
  • iron ore is introduced in the amount of 110 t / h.
  • the iron ore is dried and has a temperature of about 70 ° C.
  • the fresh reduct gas supplied to the fluidized bed reactor 4 via line 17 has a temperature of 840 ° C. and is supplied in an amount of 2,150 Nm 3 / t ore. Its chemical composition is shown in the table below.
  • the temperature of this reducing gas is 720 ° C. when it enters the second fluidized bed reactor and 1,640 ° C. when it enters the fluidized bed reactor. From this it emerges at a temperature of 450 ° C.
  • the iron ore is preheated to a temperature of about 450 ° C., which is possible without or almost without magnetite formation by lowering the reduction potential of the reducing gas supplied to the fluidized bed reactor 1 or increasing its degree of oxidation.
  • This is done according to the invention by injecting water that has a temperature of 40 ° C. In an amount of 15 Nm 3 / h, it is either introduced directly into the fluidized bed reactor 1, etc. via line 25, or via line 26 into the line connecting the fluidized bed reactors 2 and 1 19 fed. This results in a reduction in the temperature of the reducing gas by approximately 100 ° C. and a reduction in the reduction potential or increase in the degree of oxidation according to the definition:
  • a change in the composition of the reducing gas as it passes through the upper fluidized bed reactor 1 essentially results only from the addition of water, since no reaction takes place.
  • the degree of oxidation before or after the water injection increases proportionally by the amount of water injected.
  • the iron ore, preheated to 450 ° C., is partially reduced in the fluidized bed reactor 2 and reaches the fluidized bed reactor 3 at a temperature of 640 ° C. After the finished reduction in the fluidized bed reactor 4, it has a metallization of 92.5%.
  • the measure according to the invention makes it possible to reduce the reduction potential of the partially consumed reducing gas used for heating the iron ore to such an extent that a reduction, if any, does not take place, etc. with almost any idle time of the iron ore in the fluidized bed reactor 1. It has been found in experiments that a certain very slight pre-reduction can take place, which, however, is harmless for a reduction in the subsequent fluidized bed reactors 2 to 4. Such a preliminary reaction can take place up to a maximum of 0.2% oxygen breakdown / minute. Most ores have reduction rates of ⁇ 0.05% O 2 degradation per minute.
  • preheating is thus carried out in the border area of the beginning of a reduction, the temperature of the temperature used for the preheating being essential Reducing gas is kept as high as possible, in order firstly to achieve a high preheating temperature and secondly to be able to set a high temperature level in the fluidized bed reactor 2, at which wustite formation occurs directly, without inhibition by magnetite.
  • this should be at least about 600 ° C., preferably 620-660 ° C.
  • Setting a high preheat temperature can be a variant of the invention are achieved by supplying a flow of liquid CO 2 through lines 25 and 26 also in accordance with, wherein the the embodiments above supplied under water by a stream of 50 Nm 3 / h CO 2 at the same effect could be replaced. It is also possible to use mixtures of CO 2 and H 2 O for conditioning the reducing gas.
  • a counterflow between the preheating gas and the particulate material to be preheated is not important for the method according to the invention, but a heat exchange can be carried out in various ways, e.g. also take place in cross flow. .
  • the Baur-Glaessner diagram shows that a reduction process without measures according to the invention results in magnetite formation in the first fluidized bed reactor for the material to be reduced. This process is illustrated with round dots and a dashed line.
  • the Baur-Glaessner diagram is to be understood as a thermodynamic diagram and is therefore independent of the reaction kinetics and thus also of the history of the reduction.
  • the curved dashed brackets in the Baur-Glaessner diagram which are labeled 1 to 4, identify the reduction-type process according to the prior art in the reactors of the same number, that is to say without measures according to the invention; the squares and the solid line and the solid brackets 1 to 4 illustrate the reduction process according to the invention as it takes place in reactors 1 to 4 with the same number.
  • FIG. 3A shows schematically the magnetite formation in the case of conventional reduction, a dense magnetite being formed from a hematite grain by low-temperature reduction in the fluidized bed reactor 1 at approximately 550 ° C., from which the subsequent reduction at high temperatures in the fluidized bed reactors 2, 3 and 4 results dense metallic iron with entrapped wustite and an edge zone covering the grain of magnetite is formed.
  • the reduction according to the invention is illustrated in FIG.
  • the process according to the invention provides a significant improvement in the energy balance, since the high preheating in the fluidized bed reactor 1, which can be 50 ° C. or even higher than the known preheating process, reduces the reducing gas temperature in the reactors downstream for the particulate material, i.e. in the Fluidized bed reactors 2 to 4, is possible, in particular the reducing gas temperature can be reduced in the last reactor for the particulate material, whereby the risk of "sticking" of the finished reduced material, ie the sponge iron, in the fluidized bed is very substantially reduced an improvement in the flow behavior of the fine parts in the transfer lines, since the risk of sticking is also minimized here.
  • Another major advantage is the reduction in the risk of high-temperature corrosion (metal dusting) in gas biting, gas transport and gas distribution.
  • Another important advantage of the process according to the invention is that it is possible with simple means to set a temperature profile in the entire reactor cascade, since only the amount of water or, if appropriate, the amount of CO 2 has to be set for this. In contrast to this, previously a gas quantity control had to be carried out in which the entire cascade had to be reacted to the empty pipe speed by constant pressure changes.
  • the process according to the invention is advantageous not only for the reduction of iron ore, but also for other metal oxides, such as tungsten oxide, vanadium oxide or molybdenum oxide, which metals serve, for example, as additives for the production of hard metals.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Manufacture Of Iron (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L'invention concerne un procédé de réduction d'un matériau particulaire contenant du minerai de fer, lequel comprend au moins deux étapes au cours desquelles du gaz de réduction est conduit à travers au moins deux zones de réaction disposées l'une derrière l'autre en série et formées par le matériau particulaire en mouvement, et le matériau particulaire traverse les zones de réaction dans l'ordre inverse, par rapport au gaz de réduction. Le matériau particulaire est chauffé dans la première zone de réaction et soumis à une réduction dans l'autre zone de réaction. Pour que l'on puisse atteindre une température de préchauffage maximale sans formation de magnétite, le gaz de réduction conduit à la première zone de réaction est conditionné de sorte qu'il n'y ait pas ou presque pas de réduction, mais que la température de préchauffage soit cependant atteinte pour le matériau particulaire dans la région limite du début d'une réduction, le degré d'oxydation du gaz de réduction étant augmenté et/ou la température du gaz de réduction étant abaissée. Dans la seconde zone de réaction, destinée au minerai de fer, la température est maintenue à une valeur d'au moins 600 DEG C, de préférence dans une plage comprise entre 600 et 700 DEG C, en particulier entre 620 et 660 DEG C, et le matériau contenant de l'oxyde de fer est réduit en wustite.
EP02766919A 2001-09-27 2002-08-28 Procede de reduction d'un materiau particulaire contenant un metal, en particulier contenant du minerai de fer Withdrawn EP1430159A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
AT15332001 2001-09-27
AT0153301A AT410803B (de) 2001-09-27 2001-09-27 Verfahren zur reduktion von metallhältigem, insbesondere eisenerzhältigem, teilchenförmigem material
PCT/AT2002/000254 WO2003027332A1 (fr) 2001-09-27 2002-08-28 Procede de reduction d'un materiau particulaire contenant un metal, en particulier contenant du minerai de fer

Publications (1)

Publication Number Publication Date
EP1430159A1 true EP1430159A1 (fr) 2004-06-23

Family

ID=3688320

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02766919A Withdrawn EP1430159A1 (fr) 2001-09-27 2002-08-28 Procede de reduction d'un materiau particulaire contenant un metal, en particulier contenant du minerai de fer

Country Status (12)

Country Link
US (2) US20040237718A1 (fr)
EP (1) EP1430159A1 (fr)
JP (1) JP4331605B2 (fr)
KR (1) KR20040033073A (fr)
CN (1) CN1284866C (fr)
AT (1) AT410803B (fr)
AU (1) AU2002331402B2 (fr)
CA (1) CA2465990C (fr)
EG (1) EG23312A (fr)
MX (1) MXPA04002778A (fr)
WO (1) WO2003027332A1 (fr)
ZA (1) ZA200402384B (fr)

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AU2003289518B2 (en) 2002-12-23 2007-09-06 Posco An apparatus for manufacturing moltens irons to improve operation of fluidized bed type reduction apparatus and manufacturing method using the same
US7870717B2 (en) * 2006-09-14 2011-01-18 Honeywell International Inc. Advanced hydrogen auxiliary power unit
CN105586462A (zh) * 2014-11-07 2016-05-18 株式会社Posco 铁水制造设备的排空用立管排出装置
CN106048212B (zh) * 2016-06-07 2017-11-28 东南大学 一种分级还原燃烧制取烧结矿并分离co2的装置及方法
CN106048214B (zh) * 2016-06-07 2017-11-28 东南大学 一种合成气还原燃烧制取烧结矿并分离co2的装置及其方法
CN106467930B (zh) * 2016-09-28 2019-05-17 中国科学院过程工程研究所 一种钒钛磁铁矿流态化高温快速氧化还原的系统及方法
CN106319126B (zh) * 2016-09-28 2019-05-17 中国科学院过程工程研究所 一种用于钒钛磁铁矿流态化氧化还原的系统及方法
CN112858161B (zh) * 2021-01-12 2022-03-11 西南石油大学 一种测定气体水合物和管道壁面粘附力的装置及方法
CN113373273A (zh) * 2021-06-17 2021-09-10 北京金博威科技有限公司 颗粒状铁矿石的气基还原方法、气基还原系统和应用
CN113403441A (zh) * 2021-06-17 2021-09-17 北京金博威科技有限公司 颗粒直接还原铁的生产方法、生产系统和应用

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Also Published As

Publication number Publication date
US7597739B2 (en) 2009-10-06
JP4331605B2 (ja) 2009-09-16
CA2465990A1 (fr) 2003-04-03
CN1284866C (zh) 2006-11-15
WO2003027332A1 (fr) 2003-04-03
AT410803B (de) 2003-08-25
JP2005502790A (ja) 2005-01-27
AU2002331402B2 (en) 2008-05-29
MXPA04002778A (es) 2004-06-29
CN1558958A (zh) 2004-12-29
ATA15332001A (de) 2002-12-15
KR20040033073A (ko) 2004-04-17
ZA200402384B (en) 2005-06-29
US20040237718A1 (en) 2004-12-02
CA2465990C (fr) 2012-02-07
EG23312A (en) 2004-11-30
US20070245853A1 (en) 2007-10-25

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