WO2001009393A1 - Procede d'elimination d'un materiau forme de microparticules d'un lit fluidise - Google Patents

Procede d'elimination d'un materiau forme de microparticules d'un lit fluidise Download PDF

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Publication number
WO2001009393A1
WO2001009393A1 PCT/EP2000/004797 EP0004797W WO0109393A1 WO 2001009393 A1 WO2001009393 A1 WO 2001009393A1 EP 0004797 W EP0004797 W EP 0004797W WO 0109393 A1 WO0109393 A1 WO 0109393A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluidized bed
fine
bed reactor
separator
fine fraction
Prior art date
Application number
PCT/EP2000/004797
Other languages
German (de)
English (en)
Inventor
Konstantin Milionis
Johann REIDETSCHLÄGER
Original Assignee
Voest-Alpine Industrieanlagenbau 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 Industrieanlagenbau Gmbh filed Critical Voest-Alpine Industrieanlagenbau Gmbh
Priority to AU52167/00A priority Critical patent/AU5216700A/en
Publication of WO2001009393A1 publication Critical patent/WO2001009393A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00654—Controlling the process by measures relating to the particulate material
    • B01J2208/00672—Particle size selection
    • 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

Definitions

  • the invention relates to a method for discharging fine-particulate material from a fluidized bed maintained with a gas stream in the production of reduced ore, in particular sponge iron, preferably for discharging either at least partially reduced or preheated fine ore treated with a reducing gas in the fluidized bed, the material passing through the gas stream is wind-sighted and a large proportion of the material is discharged directly from the fluidized bed via an outlet and a fine portion of the material from which the gas stream leaving the fluidized bed is separated in a separator, in particular a cyclone, and a plant for carrying out the process.
  • a separator in particular a cyclone
  • Methods for reduction in a fluidized bed are known, for example, from US-A-2,909,423, WO-A-96/10094 and EP-A-0 571 358.
  • the reduction of oxide-containing fine ore, in particular iron oxide-containing fine ore takes place in a fluidized bed maintained by a reducing gas within a fluidized bed reactor, the reducing gas being introduced into the fluidized bed via a nozzle grate, flowing through the fluidized bed reactor from bottom to top and the iron oxide-containing material approximately in the fluidized bed reactor Cross flow to the reducing gas flow.
  • the reducing gas containing the fines is removed by a dust separator , like a cyclone, and the separated dust is returned to the fluidized bed.
  • the dust separators or cyclones are preferably arranged inside the fluidized bed reactors (cf. WO-A-96/10094 and US Pat. No. 2,909,423), but they can also be installed outside the fluidized bed reactors.
  • the "sticking" or “fouling” is dependent on the temperature and the degree of reduction of the oxide-containing material. Sticking or sticking in the cyclones and other parts of the system can lead to malfunctions, so that it is no longer possible to operate the system continuously over a longer period of time.
  • the invention aims to avoid these disadvantages and difficulties and has as its object to create a method of the type described above and a system for carrying out the method, which decisively increase the service life of the separating elements, in particular the cyclones. It is a particular object of the invention to enable treatment of fine particulate material over a longer period of time without the risk of operational interruptions caused by “sticking” or “fouling”.
  • This object is achieved in that the fine fraction separated in the separator is divided and a first part of the fine fraction is recirculated into the fluidized bed and a second part of the fine fraction is discharged.
  • the coarse fraction of the material discharged via the outlet is expediently introduced into a further fluidized bed with the second part of the fine fraction discharged, provided that no separate treatment of coarse and fine fraction is required.
  • a preferred embodiment of the method is characterized in that fine ore is reduced in each case with reducing gas in at least two fluidized beds connected in series and the fine ore from a fluidized bed into a fluidized bed downstream of it managed and carried out by this, etc. with air sifting in the fluidized beds and forwarding the coarse fraction of the fine ore via an outlet in each case to the further fluidized bed or to a discharge device and returning a part of the fine fraction of the material deposited in the separator to the fluidized bed and discharging a part of the fine fraction of the separated in the separator Material in the downstream fluidized bed or to the discharge device.
  • the discharge can take place continuously or in cycles.
  • a further preferred embodiment is characterized in that fine ore is reduced in each case with reducing gas in at least two fluidized beds connected in series, and the fine ore is guided from a fluidized bed into a fluidized bed arranged downstream of it and discharged by the latter, and so on. with air sifting in the fluidized beds and forwarding the coarse fraction of the fine ore via an outlet in each case to the further fluidized bed or to a discharge device and returning a part of the fine fraction of the material separated in the separator to the fluidized bed and discharging a part of the fine fraction of the separated in the separator Materials in the upstream fluidized bed.
  • the division of the fine fraction into a first part and a second part is expediently varied, etc. in ranges 20 to 100%, preferably 20 to 80%, proportion of the first part of the fine fraction, remainder of the second part, the first part denoting the part which is discharged from the fluidized bed.
  • a system for carrying out the process according to the invention with at least one fluidized bed reactor, a feed line which opens into the fluidized bed reactor for fine-particulate material to be treated in the fluidized bed reactor, a discharge line for material treated in the fluidized bed reactor, which assumes that a fluidized bed is present in the fluidized bed reactor
  • Gas supply line for introducing a gas stream which maintains the fluidized bed in the fluidized bed reactor and a gas discharge from the fluidized bed reactor which is conducted via a separator, in particular a cyclone is characterized in that a line which leads away the fine fraction of the material which has been separated off in the separator leads to a dividing element a return line leading into the fluidized bed reactor and a discharge line, which leads to a treatment station for the fine fraction downstream of the fluidized bed reactor.
  • the dividing member is preferably formed by a fluidized bed lock designed in the manner of communicating vessels, the return line starting from one of the vessels and the outlet line from the other vessel.
  • the fluidized bed lock is provided with a line supplying a fluidizing gas for the purpose of forming a fluidized bed, wherein a gas return line can advantageously lead from the fluidized bed lock into the fluidized bed reactor.
  • the dividing member can also be formed by a mechanical distributor.
  • An actuator for interrupting or setting a material flow of a certain magnitude or for driving a pulsed operation can advantageously be provided in the return line and in the drain line.
  • the separator designed as a cyclone; it can be arranged either inside the fluidized bed reactor or outside the fluidized bed reactor.
  • the dividing member can equally be arranged either inside or outside the fluidized bed reactor.
  • At least two fluidized bed reactors are provided in series.
  • the downstream treatment station for the fine fraction is preferably the fluidized bed reactor downstream of the fluidized bed ore or the discharge device.
  • the downstream treatment station for the fine fraction is the fluidized bed reactor upstream of the fluidized bed ore.
  • FIG. 1 showing a process diagram according to a first embodiment of the invention.
  • 2 is a step-like arrangement of four fluidized bed reactors of Fig. 1 schematically shown on an enlarged scale.
  • 3 and 4 each show a cross section through a fluidized bed reactor according to different embodiments of the invention.
  • 5 and 6 each show a process diagram of further preferred embodiments of the invention.
  • FIG. 7 shows a detail of the method variant shown in FIG. 5.
  • the plant according to the invention according to the exemplary embodiment has four fluidized bed reduction reactors 1 to 4 connected in series, with iron oxide-containing material, such as fine ore, optionally also additives, being fed via an ore feed line 5 to the first fluidized bed reduction reactor 1 and from fluidized bed reduction reactor to fluidized bed reduction reactor is fed via conveyor lines 6 and the finished reduced material (sponge iron) is hot briquetted in a briquetting system 7.
  • the briquetting system 7 is a so-called riser 8, which is understood to mean an essentially vertical, brick-lined pipe section through which the sponge iron is pneumatically conveyed upwards by means of the reducing gas, and a storage bunker 9 is connected upstream. If necessary, the reduced iron is protected from reoxidation during the briquetting by an inert gas system, not shown.
  • the fine ore Before the fine ore is introduced into the first reduction reactor 1, it is subjected to ore preparation, such as drying and sieving, which are not shown in detail.
  • Reduction gas is conducted in countercurrent to the ore flow from reduction reactor 4 to reduction reactor 3 to 1 and is discharged as top gas via a top gas discharge line 10 from the last reduction reactor 1 in the gas flow direction and cooled and washed in a wet scrubber 11.
  • the top gas is preferably recirculated at least in part, whereby it is mixed with reducing gas freshly supplied via a feed line 12.
  • the feed line 12 opens into the top gas discharge line 10 after the top gas has been compressed by means of a compressor 13.
  • the mixed gas thus formed is passed through a CO scrubber 14 and freed of CO 2 , and is now available as a reducing gas.
  • This reducing gas is heated via the reducing gas supply line 15 in a gas heater 16 arranged downstream of the CO scrubber 14 to a reducing gas temperature of approximately 800 ° C. and fed to the first fluidized bed reactor 4 in the gas flow direction, where it is used to produce fine ores directly reduced iron reacts.
  • the reduction reactors 4 to 1 are in Series switched; the reducing gas passes through the connecting lines 17 from the reduction reactor to the reduction reactor.
  • Part of the top gas is removed from the gas circuit 10, 15, 17 in order to avoid an enrichment of inert gases, such as N 2 .
  • the discharged top gas is fed via a branch line 18 to the gas heater 16 for heating the reducing gas and burned there. Any missing energy is supplemented by a heating gas, such as natural gas, which is supplied via a feed line 19.
  • a separator 20 in particular a dust separator, such as a cyclone, is provided in the reducing gas connecting lines 17 connecting the reducing reactors 2 and 3 and 3 and 4, in which the fine fraction of the treated fine-particulate material entrained by the reducing gas stream, i.e. of fine ore, settles.
  • This fine fraction is fed via a connecting line 21 to a dividing member 22, from which a first part of the fine fraction is recirculated into the fluidized bed reactor 3 or 4, from which it was discharged with the reducing gas stream, etc. the return takes place via the return line 23, which opens into the respective fluidized bed reactor 3 or 4.
  • the second part of the fine fraction is led via an outlet line 24 to the next treatment station following the fluidized bed reactor 3 or 4 from which the fine fraction originates, i.e. the downstream fluidized bed reactor 4, or the conveyor line 6 leading to the briquetting system 7 or to the riser 8 ,
  • actuators 25 are provided for setting the amount of the respective fine fraction, which are additionally used in addition to the setting of the amount of the respective fine fraction via the mode of operation of the fluidized bed lock or of the distribution process 22 for setting the respective fine fraction can.
  • the discharge line 24 can also open directly into the fluidized bed reactor 4 via the line 24 '.
  • each fluidized bed reactor 3, 4 is provided on the inside with at least one cyclone 20, from which a discharge line 21 leads to the partition member 22 arranged outside (FIG. 3) or also inside (FIG. 4) of this fluidized bed reactor.
  • the reducing gas cleaned in the cyclone 20 is conducted via a reducing gas outlet line 26 into the dome region of the fluidized bed reactor 3, 4, which is separated from the lower part of the fluidized bed reactor by a partition wall 27, and emerges from the fluidized bed reactor 3, 4 via a connecting line 17 ,
  • the dividing member 22 designed as a fluidized bed lock is formed by two vessels 28, 29 which are connected to one another in the lower region in the manner of communicating vessels.
  • a fluidizing gas is introduced into each of the vessels 28, 29 via the lines 30, which open at the bottom, so that a fluidized bed 31 formed in each case by the fine fraction is formed in the interior of the vessels.
  • the fluidizing gas is optionally introduced via a gas outlet line 32, which is optionally provided with an actuator 33, or via return lines 23 or the outlet line 24 into the fluidized bed reactor 3 or 4, from which the fine fraction originates ,
  • This fluidizing gas can also be formed by reducing gas, for example.
  • the dividing member 22 can also be formed by a mechanical distributor. It is important that the two parts into which the fine fraction of the material is broken down can be coordinated in terms of quantity, so that on the one hand the recirculated quantity of the fine fraction and on the other hand the discharged quantity of the fine fraction can be optimized.
  • the height of the vessels 28, 29 or the fluidized beds 31 located therein depends on the pressures which the parts of the fines should have after exiting the partition member 22 in order to be able to be recirculated or introduced into the next treatment stage.
  • pressure differences can also be achieved by means of pneumatic gas seals or by a suitable partial or complete deflection of the fine grain flow.
  • 5 and 6 each schematically show a process flow diagram of preferred embodiments of the invention, wherein in the process scheme according to FIG. 5 a part of the fine fraction of the material deposited in the separator 20 of each fluidized bed reactor 1 to 4 into the respective downstream fluidized bed 1 to 4 or is discharged to the discharge device 8. 6 shows an analogous process scheme, however, part of the fine fraction of the material separated in the separator 20 of each fluidized bed reactor 1 to 4 is discharged into the respective upstream fluidized bed 1 to 4.
  • FIG. 7 shows in detail the removal of part of the fine fraction of the fluidized bed reactor 4 in the separator 20 of the last fluidized bed reactor 4 in the flow direction of the ore to the riser 8 via the discharge line 24.
  • the actuator 30 provided in the discharge line 24 can be constantly open or opened in cycles ,
  • the process according to the invention can advantageously also be carried out for single-stage metallurgical processes or only in a few stages of a multi-stage process or also in the last stage of a multi-stage process, the part of the fines removed directly forming part of the product. It can also be advantageous if the separated fine fraction is only returned to the stage from which it was separated in only one or only some of the stages of a multi-stage process.
  • another hot gas for example heated air, can also be used instead of the reducing gas passed through the fluidized bed.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Dispersion Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Manufacture Of Iron (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

La présente invention concerne un procédé d'élimination d'un matériau formé de microparticules d'un lit fluidisé conservé avec un flux gazeux, lors de la fabrication de minerai réduit, en particulier d'éponge de fer, ledit procédé servant de préférence à l'élimination de fines de minerai, soit partiellement réduites en morceaux, soit préchauffées, traitées dans le lit fluidisé avec un gaz réducteur. Selon ce procédé, le matériau est séparé à vent par le flux gazeux et une partie grossière du matériau est directement évacuée du lit fluidisé via un déversoir (6) et une partie fine du matériau est séparée du flux gazeux sortant du lit fluidisé dans un séparateur (20), en particulier un cyclone. Pour augmenter la longévité du séparateur et éviter l'adhérence ou l'encrassement, la partie fine extraite dans le séparateur (20) est séparée en deux parties: l'une est réintroduite dans le lit fluidisé et l'autre est évacuée vers l'extérieur. L'évacuation de la partie fine permet de plus un traitement séparé des parties grossière et fine du produit.
PCT/EP2000/004797 1999-07-29 2000-05-26 Procede d'elimination d'un materiau forme de microparticules d'un lit fluidise WO2001009393A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU52167/00A AU5216700A (en) 1999-07-29 2000-05-26 Method for removing fine-particled material from a fluidised bed

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT0131599A AT407530B (de) 1999-07-29 1999-07-29 Verfahren zum ausbringen von feinteilchenförmigem material aus einem wirbelbett
ATA1315/99 1999-07-29

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WO2001009393A1 true WO2001009393A1 (fr) 2001-02-08

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AT (1) AT407530B (fr)
AU (1) AU5216700A (fr)
WO (1) WO2001009393A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008009433A2 (fr) * 2006-07-21 2008-01-24 Corus Technology Bv Procédé et appareil pour la réduction d'un matériau métallifère en un produit de réduction
EP3039686A1 (fr) * 2013-08-30 2016-07-06 Honeywell International Inc. Unités de réacteurs à lit fluidisé couplées en série comprenant des ensembles plénums cycloniques et procédés d'hydrofluoration associés

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3532489A (en) * 1966-06-03 1970-10-06 Wienert Fritz Otto Method and apparatus for reducing metal oxides
US4976776A (en) * 1988-03-30 1990-12-11 A. Ahlstrom Corporation Method for reduction of material containing metal oxide using a fluidized bed reactor and flame chamber
US5674308A (en) * 1994-08-12 1997-10-07 Midrex International B.V. Rotterdam, Zurich Branch Spouted bed circulating fluidized bed direct reduction system and method
US5762681A (en) * 1994-12-29 1998-06-09 Pohang Iron & Steel Co., Ltd. Fluidized bed type reduction apparatus for iron ores and method for reducing iron ores using the apparatus

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3532489A (en) * 1966-06-03 1970-10-06 Wienert Fritz Otto Method and apparatus for reducing metal oxides
US4976776A (en) * 1988-03-30 1990-12-11 A. Ahlstrom Corporation Method for reduction of material containing metal oxide using a fluidized bed reactor and flame chamber
US5674308A (en) * 1994-08-12 1997-10-07 Midrex International B.V. Rotterdam, Zurich Branch Spouted bed circulating fluidized bed direct reduction system and method
US5762681A (en) * 1994-12-29 1998-06-09 Pohang Iron & Steel Co., Ltd. Fluidized bed type reduction apparatus for iron ores and method for reducing iron ores using the apparatus

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008009433A2 (fr) * 2006-07-21 2008-01-24 Corus Technology Bv Procédé et appareil pour la réduction d'un matériau métallifère en un produit de réduction
WO2008009433A3 (fr) * 2006-07-21 2008-06-12 Corus Technology Bv Procédé et appareil pour la réduction d'un matériau métallifère en un produit de réduction
EP3039686A1 (fr) * 2013-08-30 2016-07-06 Honeywell International Inc. Unités de réacteurs à lit fluidisé couplées en série comprenant des ensembles plénums cycloniques et procédés d'hydrofluoration associés
EP3039686A4 (fr) * 2013-08-30 2017-04-05 Honeywell International Inc. Unités de réacteurs à lit fluidisé couplées en série comprenant des ensembles plénums cycloniques et procédés d'hydrofluoration associés
CN105765664B (zh) * 2013-08-30 2018-05-29 霍尼韦尔国际公司 包括气旋充气组件的串联流化床反应器单元和相关的氢氟化的方法

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ATA131599A (de) 2000-08-15
AT407530B (de) 2001-04-25
AU5216700A (en) 2001-02-19

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