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EP0048008A1 - Method and apparatus for the direct production of hot metal from lump iron ore - Google Patents

Method and apparatus for the direct production of hot metal from lump iron ore Download PDF

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Publication number
EP0048008A1
EP0048008A1 EP81107215A EP81107215A EP0048008A1 EP 0048008 A1 EP0048008 A1 EP 0048008A1 EP 81107215 A EP81107215 A EP 81107215A EP 81107215 A EP81107215 A EP 81107215A EP 0048008 A1 EP0048008 A1 EP 0048008A1
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EP
European Patent Office
Prior art keywords
melter gasifier
gas stream
shaft furnace
direct reduction
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.)
Granted
Application number
EP81107215A
Other languages
German (de)
French (fr)
Other versions
EP0048008B1 (en
Inventor
Ralph Weber
Bernt Rollinger
Rolf Dr. Hauk
Michael Nagl
Bernhard Rinner
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.)
Deutsche Voest Alpine Industrieanlagenbau GmbH
Original Assignee
Voestalpine AG
Deutsche Voest Alpine Industrieanlagenbau GmbH
Korf Engineering 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 Voestalpine AG, Deutsche Voest Alpine Industrieanlagenbau GmbH, Korf Engineering GmbH filed Critical Voestalpine AG
Priority to AT81107215T priority Critical patent/ATE8799T1/en
Publication of EP0048008A1 publication Critical patent/EP0048008A1/en
Application granted granted Critical
Publication of EP0048008B1 publication Critical patent/EP0048008B1/en
Expired 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
    • C21B13/14—Multi-stage processes processes carried out in different vessels or 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
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
    • C21B13/002—Reduction of iron ores by passing through a heated column of carbon
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/44—Removing particles, e.g. by scrubbing, dedusting

Definitions

  • the invention relates to a method according to the preamble of patent claim 1. It also relates to a device according to the preamble of patent claim 8.
  • a method and a ' device of this type are known from DE-OS 28 43 303.
  • the reducing gas generated in the melter gasifier still has a temperature of about 1200 to 1400 ° C. at the point of exit from the melter gasifier and is also high in dust. load part. Therefore, it can only be fed to the direct reduction shaft furnace after cleaning and cooling to the temperature of around 800 ° C required for the direct reduction process. Direct introduction into the reduction furnace would quickly result in the bulk material sticking together and clogging the gaps due to the amount of dust carried along, making the direct reduction process impossible. Therefore, a direct connection between the direct reduction shaft furnace and the melter gasifier is prevented and the hot sponge iron is conveyed from the direct reduction shaft furnace into the melter gasifier by means of a lock designed as a shut-off device.
  • the object of the invention is to enable a continuous transport of the hot sponge iron particles from the direct reduction shaft furnace into the melter gasifier in a method and a device of the type mentioned in the introduction, without causing the difficulties mentioned.
  • the process is intended to ensure reliable, long-term transport of iron sponge particles heated to just below the softening temperature from the direct reduction shaft furnace into the melter gasifier.
  • the inventive solution is dispensed with the locks, the hot, the over 1200 0 C and prevent polluted reducing gas from the melter gasifier from passing through the discharge opening into the reduction shaft furnace. It has been shown that a small part of the reducing gas generated in the melter gasifier can be introduced into the reduction unit in countercurrent to the sponge iron particles if this gas is cooled in front of the discharge device to temperatures below the softening temperature of the sponge iron being conveyed. In the cooling process it appears essential that this does not reduce the quality of the reducing gas. It has proven to be particularly advantageous, sufficient in the Usually to below 100 ° C, add cooled and cleaned reducing gas.
  • a substantial proportion of the dust carried is deposited in the area of the outlet side of the discharge device and is discharged together with the sponge iron particles by the discharge device. Because: with the proportion of the uncleaned reducing gas flowing in directly via the discharge device in relation to the gas blown into the reduction zone, cleaned and cooled to process temperature, the flow resistance in the flow path of the uncleaned reducing gas must be considerably higher than in the flow path of the cleaned and up Process temperature cooled cooling gas. The flow resistance for the first-mentioned flow path is primarily determined by the discharge device and the pouring column up to the injection nozzles for the cleaned and cooled reducing gas.
  • a discharge device should therefore be used which has a relatively high flow resistance, while the flow resistance in the main flow path of the reducing gas should be kept as small as possible by suitable selection of dedusting and cooling devices.
  • Screw conveyors the conveyor part of which is designed as a paddle screw and the outlet opening of which opens directly into a downpipe connected to the melter gasifier, have proven to be particularly suitable as the discharge device.
  • the screw conveyors cause a relatively high pressure loss and at the same time form a good dust filter that "cleans itself” together with the sponge iron particles due to the constant discharge of the collected dust particles.
  • the device schematically shown in Fig. 1 for the direct production of molten pig iron from lumpy iron ore contains a melter gasifier 1 of the type described in DE-OS 28 43 303. Above the melter gasifier is a direct reduction shaft furnace 2 suspended in a steel structure, not shown, arranged in the Principle is described for example in DE-OS 29 35 707.
  • the direct reduction shaft furnace is supplied with 3-piece iron ore via a gas-tight double bell lock, which sinks in the form of a loose bed in the shaft furnace and is reduced to sponge iron at a temperature between 760 and 850 ° C by means of a hot reducing gas blown in via a central gas inlet 4.
  • the used reducing gas leaves the shaft furnace 2 via an upper gas outlet 5 and can be returned to the reducing gas circuit in a known manner or used in some other way.
  • the hot sponge iron obtained by reducing the lumpy iron ore is discharged from the direct reduction shaft furnace 2 at a temperature of about 750 ° to 800 ° C. and continuously charged into the melter gasifier from above.
  • a coal fluidized bed 8 is formed in the melter gasifier from coal introduced through openings 6 and oxygen-containing gas, in particular oxygen and air, which is blown in through twelve radially arranged nozzles 7, in which even larger iron sponge particles are noticeably decelerated and up to the entry into a high-temperature zone in the lower section of the coal fluidized bed one substantial amount in their temperature and finally be melted.
  • the coal fluidized bed 8 there is a calming space into which radial nozzles 9 open, through which water vapor, hydrocarbons or a reducing gas, for example cooled down to 50 ° C., are blown in to cool the hot reducing gas generated in the melter gasifier.
  • the reducing gas generated in the melter gasifier leaves the melter gasifier above the settling chamber through two gas outlets 10 with a temperature between 1200 and 1400 ° C. and a pressure of about 2 bar. It then arrives at a mixing point 11, in which it is at a sufficiently low temperature for the cooling gas. Direct reduction necessary temperature, usually from 760 to 850 ° C, is brought.
  • the mixing point is designed such that a part of the kinetic energy of the cooling gas is recovered as pressure after mixing with the hot reducing gas supplied by the melter gasifier, and the pressure loss in the hot gas path is thus kept as low as possible.
  • the gas reaches a cyclone separator 12, in which the coke dust and ash entrained with the gas flow are largely separated.
  • the hot gas stream cooled and cleaned to the prescribed process temperature is divided, namely about 60 vol .-% of which are blown as the first partial gas stream 13 through the gas inlet 4 into the reduction zone of the direct reduction shaft furnace 2, while the other part for cooling gas extraction is an injection cooler 14 and then a washing tower 15 is supplied.
  • the cooling gas emerging here is compressed by a compressor 16 and at a temperature of approximately 50 ° C. for temperature control of the hot reducing gas of the mixing point 11 emerging from the melter gasifier, to control the temperature of the reducing gas in the melter, the nozzles 9 and, as described later, a ring line 22.
  • each screw conveyor 17 is arranged radially symmetrically to the central axis of the furnace, which are designed as paddle screws and are supported on one side.
  • the outlet opening 18 of each screw conveyor is connected to a connecting line in the form of a downpipe 19 which opens through the ceiling of the melter gasifier 1 into the settling chamber of this gasifier. Accordingly, six axially symmetrically arranged downpipes are also provided in the present case.
  • a nozzle 21 from a ring line 22 opens into each downpipe, to which the compressor 16 feeds a stream of the reducing gas, which has been cooled to 50 ° C and is supplied by the melter gasifier, and which is called the third partial gas stream 23.
  • second partial gas stream 24 The entire gas stream from unpurified reducing gas flowing directly from the melter gasifier into the downpipes is referred to as second partial gas stream 24.
  • the temperature of the second partial gas stream 24 'flowing into the downpipes 19 is cooled to a temperature between 760 and 850 ° C. by means of the cooling gas introduced in a controlled amount via the nozzles 21 before the gas streams via the Screw conveyor 17 get into the reduction shaft furnace.
  • the cooling gas is supplied in such a way that there is particularly good swirling with the rising raw gas.
  • the dust contained in the ascending gas stream when entering the screw conveyor 17 settles essentially in the area of the screw conveyor and is successively conveyed back together with the sponge iron particles back into the downpipe in question and into the melter gasifier.
  • the second partial gas stream 24 i.e. That is, the amount of raw gas flowing directly upwards from the melter gasifier via the six downpipes 19 to a maximum of 30% by volume of the total amount of reducing gas introduced into the direct reduction shaft furnace.
  • the flow resistance for the second partial gas stream 24 in the flow path up to the reduction zone in the direct reduction shaft furnace i.e. So up to the level of the gas inlet 4 is greater than the flow resistance for the first partial gas flow 13 in the flow path from the gas outlet 10 to the gas inlet 4.
  • This requirement meets the design of the discharge device 17 as a screw conveyor, the conveyor part is designed as a paddle screw.
  • the flow resistance and thus the pressure losses in the flow path of the first partial gas stream 13 are deliberately kept low.
  • the inventive design of the method and the device enables a direct continuous transport of the hot sponge iron particles from the direct reduction shaft furnace 2 into the melter gasifier 1 without locks or other complex devices for sealing against the hot reducing gas being required, which at the high temperature and A rt of the material to be conveyed can only be realized with difficulty with the required operational safety.
  • the screw conveyor is. flanged to a socket 31 welded to the jacket of the direct reduction shaft furnace.
  • a socket 31 welded to the jacket of the direct reduction shaft furnace.
  • an outlet socket 32 on the outlet side 18 of the conveyor for flange-mounting a downpipe 19 (see also FIG. 1).
  • the conveying part envelops a cladding tube 33, which is also flanged to the socket 31.
  • the screw conveyor 17 contains a conveyor part 36 protruding into the furnace, a bearing part 34 flanged out of the furnace on the connecting piece 31 and a drive part 44.
  • the conveying part 36 has the shape of an interrupted worm gear formed by paddles 37, the envelope 38 of the paddle screw shown in broken lines tapering conically towards the free end of the shaft 35. This free end extends almost to the middle of the shaft furnace and ensures the conical tapering of the envelope. an even removal of the bulk material from the bulk column.
  • the shaft 35 is water-cooled and hollow for this purpose with an inner tube 39, which ends just before the free end of the shaft 35 and into which the cooling water is introduced, which is then diverted at the free end and in the annular gap between the central tube 39 and the inner wall of the shaft 35 flows back.
  • the drive 44 is constructed as follows. To rotate the shaft 35, a ratchet mechanism 45 with a wheel 40, in the teeth of which a pawl 41 engages, which is rotatably attached to a lever 42, which in turn is rotatably seated on the shaft 35, and by means of a hydraulically or pneumatically actuated piston 43 by one predetermined angular movement can be pivoted back and forth.
  • the pawl 41 rotates the wheel 40 by an amount corresponding to the tooth pitch or a multiple of the tooth pitch.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture Of Iron (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Vertical, Hearth, Or Arc Furnaces (AREA)
  • Refinement Of Pig-Iron, Manufacture Of Cast Iron, And Steel Manufacture Other Than In Revolving Furnaces (AREA)
  • Revetment (AREA)
  • Artificial Fish Reefs (AREA)
  • Manufacture Of Metal Powder And Suspensions Thereof (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)

Abstract

Heiße Eisenschwammpartikel werden aus einem Direktreduktionsschactofen (2) durch Schneckenförderer (17) über Verbindungsleitungen (19) direkt in einen Einschmelzvergaser (1) gefördert und ein sich über diesen direkten Weg ausbildender Gasstrom (24) von Einschmelzvergaser (1) in den Direktreduktionsschachtofen (2) nach Kühlung auf unterhalb 950°C auf maximal 30 Vol.-% der dem Direktreduktionsschachtofen (2) insgesamt zugeführten Reduktionsgasmenge begrenzt.Hot sponge iron particles are conveyed from a direct reduction choke furnace (2) by screw conveyors (17) via connecting lines (19) directly into a melter gasifier (1) and a gas stream (24) from the melter gasifier (1) that forms via this direct path into the direct reduction shaft furnace (2) After cooling to below 950 ° C., it is limited to a maximum of 30 vol.% of the total amount of reducing gas supplied to the direct reduction shaft furnace (2).

Description

Die Erfindung betrifft ein Verfahren gemäß dem Oberbegriff des Patentanspruchs 1..Sie bezieht sich ferner auf eine Vorrichtung gemäß dem Oberbegriff des Patentanspruchs 8.The invention relates to a method according to the preamble of patent claim 1. It also relates to a device according to the preamble of patent claim 8.

Ein Verfahren und eine'Vorrichtung dieser Art sind durch die DE-OS 28 43 303 bekannt geworden. Das im Einschmelzvergaser erzeugte Reduktionsgas weist an der Austrittsstelle aus dem Einschmelzvergaser noch eine Temperatur von etwa 1200 bis 1400°C auf und ist außerdem mit einem hohen Staub- . anteil beladen. Deshalb kann es erst nach dem Reinigen und Abkühlen auf die für den Direktreduktionsprozess erforderliche Temperatur von etwa 800°C dem Direktreduktionsschachtofen zugeführt werden. Ein unmittelbares-Einleiten in den Reduktionsofen würde binnen kurzer Zeit zum Verkleben des Schüttgutes und zum Zusetzen der Zwischenräume durch den mitgeführten Staubanteil führen und damit den Direktreduktionsprozess unmöglich machen. Deshalb wird eine direkte Verbindung zwischen dem Direktreduktionsschachtofen und dem Einschmelzvergaser verhindert und der heiße Eisenschwamm wird mittels einer als Absperrorgan ausgebildeten Schleuse vom Direktreduktionsschachtofen in den Einschmelzvergaser gefördert.A method and a ' device of this type are known from DE-OS 28 43 303. The reducing gas generated in the melter gasifier still has a temperature of about 1200 to 1400 ° C. at the point of exit from the melter gasifier and is also high in dust. load part. Therefore, it can only be fed to the direct reduction shaft furnace after cleaning and cooling to the temperature of around 800 ° C required for the direct reduction process. Direct introduction into the reduction furnace would quickly result in the bulk material sticking together and clogging the gaps due to the amount of dust carried along, making the direct reduction process impossible. Therefore, a direct connection between the direct reduction shaft furnace and the melter gasifier is prevented and the hot sponge iron is conveyed from the direct reduction shaft furnace into the melter gasifier by means of a lock designed as a shut-off device.

Derartige Schleusen haben sich wegen der hohen Temperaturen und wegen der Baschaffenheit des Schüttgutes als störanfällig erwiesen. Es kommt vor, daß sich an den Schließstellen der Absperrorgane Material festsetzt und damit kein gasdichter Abschluß mehr gewährleistet ist. Die heißen aufsteigenden Gase, die das Schüttgut über ihren Erweichungspunkt erwärmen, führen dann bald zu weiteren Schwierigkeiten infolge eines Zusammenbackens der Eisenschwammpartikel.Such locks have proven to be prone to failure because of the high temperatures and because of the bulk of the bulk material. It happens that material closes at the closing points of the shut-off devices and therefore no more gas-tight closure is guaranteed. The hot rising gases that heat the bulk material above their softening point will soon lead to further difficulties due to caking of the iron sponge particles.

Aufgabe der Erfindung ist es, bei einem Verfahren und einer Vorrichtung der einleitend genannten Art einen kontinuierlichen Transport der heißen Eisenschwammpartikel aus dem Direktreduktionsschachtofen in den Einschmelzvergaser zu ermöglichen, ohne daß es zu den erwähnten Schwierigkeiten kommt. Das Verfahren soll im Hinblick auf einen hohen thermischen Wirkungsgrad des Gesamtprozesses einen auf Dauer betriebssicheren Transport von auf knapp unterhalb der Erweichungstemperatur erhitzten Eisenschwammpartikeln aus dem Direktreduktionsschachtofen in den Einschmelzvergaser ermöglichen.The object of the invention is to enable a continuous transport of the hot sponge iron particles from the direct reduction shaft furnace into the melter gasifier in a method and a device of the type mentioned in the introduction, without causing the difficulties mentioned. In view of the high thermal efficiency of the overall process, the process is intended to ensure reliable, long-term transport of iron sponge particles heated to just below the softening temperature from the direct reduction shaft furnace into the melter gasifier.

Diese Aufgabe ist bei einem Verfahren der genannten Art durch die kennzeichnenden Merkmale des Anspruches 1 gelöst. Vorteilhafte Ausgestaltungen des Verfahrens sind den Ansprüchen 2 bis 7 zu entnehmen. Die erfindungsgemäße Vorrichtung ist durch die Merkmale des Anspruchs 8 gekennzeichnet, vorteilhafte Ausgestaltungen der Vorrichtung sind den restlichen Ansprüchen zu entnehmen.This object is achieved in a method of the type mentioned by the characterizing features of claim 1. Advantageous embodiments of the method can be found in claims 2 to 7. The device according to the invention is characterized by the features of claim 8, advantageous refinements of the device can be found in the remaining claims.

Bei der erfindungsgemäßen Lösung wird auf die Schleusen verzichtet, die das über 12000C heiße und verschmutzte Reduktionsgas aus dem Einschmelzvergaser daran hindern, über die Austragöffnung in den Reduktionsschachtofen zu gelangen. Es hat sich gezeigt, daß ohne Schwierigkeiten ein kleiner Teil des im Einschmelzvergaser erzeugten Reduktionsgases im Gegenstrom zu den Eisenschwammpartikeln in das Reduktionsaggregat eingeleitet werden kann, wenn dieses Gas vor der Austragvorrichtung auf Temperaturen unterhalb der Erweichungstemperatur des geförderten Eisenschwammes abgekühlt wird. Beim Abkühlprozess erscheint es wesentlich, daß dieser die Güte des Reduktionsgases nicht verringert.:Als besonders vorteilhaft hat es sich erwiesen, ausreichend, in der Regel auf unterhalb 100°C,abgekühltes und gereinigtes Reduktionsgas beizumischen. Ein wesentlicher Anteil des mitgeführten Staübs setzt sich im Bereich der Austrittsseite der Austragvorrichtung ab und wird durch die Austragvorrichtung zusammen mit den Eisenschwammpartikeln ausgetragen. Da-: mit der Anteil des über die Austragvorrichtung direkt einströmenden ungereinigten Reduktionsgases im Verhältnis zu dem in die Reduktionszone eingeblasenen, gereinigten und auf Prozesstemperatur abgekühlten Gas klein gehalten wird, muß der Strömungswiderstand im Strömungsweg des ungereinigten Reduktionsgases wesentlich höher als im Strömungsweg des gereinigten und auf Prozesstemperatur abgekühlten Reduktionsgases sein. Der Strömungswiderstand wird für den erstgenannten Strömungsweg in erster Linie durch die Austragvorrichtung und die Schüttsäule bis zu den Einblasdüsen für das gereinigte und gekühlte Reduktionsgas bestimmt. Es sollte deshalb eine Austragvorrichtung zur Anwendung kommen, die einen verhältnismäßig hohen Strömungswiderstand aufweist, während der Strömungswiderstand im Hauptströmungsweg des Reduktionsgases durch geeignete Auswahl von Entstaubungs-und Kühlvorrichtungen möglichst klein gehalten werden soll. Als Austragvorrichtung haben sich Schneckenförderer, deren Förderteil als Paddelschnecke ausgebildet ist und deren Austrittsöffnung jeweils unmittelbar in ein mit dem Einschmelzvergaser verbundenes Fallrohr mündet, als besonders geeignet erwiesen. Die Schneckenförderer bedingen einen verhältnismäßig hohen Druckverlust und bilden zugleich ein gutes Staubfilter, das sich durch den ständigen Austrag der aufgefangenen Staubteilchen zusammen mit den Eisenschwammpartikeln "selbst reinigt".In the inventive solution is dispensed with the locks, the hot, the over 1200 0 C and prevent polluted reducing gas from the melter gasifier from passing through the discharge opening into the reduction shaft furnace. It has been shown that a small part of the reducing gas generated in the melter gasifier can be introduced into the reduction unit in countercurrent to the sponge iron particles if this gas is cooled in front of the discharge device to temperatures below the softening temperature of the sponge iron being conveyed. In the cooling process it appears essential that this does not reduce the quality of the reducing gas. It has proven to be particularly advantageous, sufficient in the Usually to below 100 ° C, add cooled and cleaned reducing gas. A substantial proportion of the dust carried is deposited in the area of the outlet side of the discharge device and is discharged together with the sponge iron particles by the discharge device. Because: with the proportion of the uncleaned reducing gas flowing in directly via the discharge device in relation to the gas blown into the reduction zone, cleaned and cooled to process temperature, the flow resistance in the flow path of the uncleaned reducing gas must be considerably higher than in the flow path of the cleaned and up Process temperature cooled cooling gas. The flow resistance for the first-mentioned flow path is primarily determined by the discharge device and the pouring column up to the injection nozzles for the cleaned and cooled reducing gas. A discharge device should therefore be used which has a relatively high flow resistance, while the flow resistance in the main flow path of the reducing gas should be kept as small as possible by suitable selection of dedusting and cooling devices. Screw conveyors, the conveyor part of which is designed as a paddle screw and the outlet opening of which opens directly into a downpipe connected to the melter gasifier, have proven to be particularly suitable as the discharge device. The screw conveyors cause a relatively high pressure loss and at the same time form a good dust filter that "cleans itself" together with the sponge iron particles due to the constant discharge of the collected dust particles.

Die Erfindung wird durch ein Ausführungsbeispiel anhand von zwei Figuren näher erläutert. Es zeigen

  • Fig. 1 eine schematische Darstellung des Verfahrens und der Vorrichtung,
  • Fig. 2 in einem Längsschnitt einen Schneckenförderer zum Heißaustrag der Eisenschwammpartikel.
The invention is explained in more detail by an embodiment with reference to two figures. Show it
  • F ig. 1 shows a schematic representation of the method and the device,
  • Fig. 2 in a longitudinal section a screw conveyor for hot discharge of the sponge iron particles.

Die in Fig. 1 schematisch dargestellte Vorrichtung zur direkten Erzeugung von flüssigem Roheisen aus stückigem Eisenerz enthält einen Einschmelzvergaser 1 der in der DE-OS 28 43 303 beschriebenen Art. Oberhalb des Einschmelzvergasers ist ein in einer nicht dargestellten Stahlkonstruktion aufgehängter Direktreduktionsschachtofen 2 angeordnet, der im Prinzip beispielsweise in der DE-OS 29 35 707 beschrie- ― ben ist. Dem Direktreduktionsschachtofen wird über einen gasdichten Doppelglockenverschluß 3 stückiges Eisenerz zugeführt, das in Form einer losen Schüttung im Schachtofen absinkt und mittels eines über einen mittleren Gaseinlaß 4 eingeblasenen heißen Reduktionsgases einer Temperatur zwischen 760 und 850°C zu Eisenschwamm reduziert wird. Das verbrauchte Reduktionsgas verläßt den Schachtofen 2 über einen oberen Gasauslaß 5 und kann in bekannter Weise in den Reduktionsgaskreislauf zurückgeführt oder anderweitig ausgenutzt werden.The device schematically shown in Fig. 1 for the direct production of molten pig iron from lumpy iron ore contains a melter gasifier 1 of the type described in DE-OS 28 43 303. Above the melter gasifier is a direct reduction shaft furnace 2 suspended in a steel structure, not shown, arranged in the Principle is described for example in DE-OS 29 35 707. The direct reduction shaft furnace is supplied with 3-piece iron ore via a gas-tight double bell lock, which sinks in the form of a loose bed in the shaft furnace and is reduced to sponge iron at a temperature between 760 and 850 ° C by means of a hot reducing gas blown in via a central gas inlet 4. The used reducing gas leaves the shaft furnace 2 via an upper gas outlet 5 and can be returned to the reducing gas circuit in a known manner or used in some other way.

Der durch Reduktion des stückigen Eisenerzes erhaltene heiße Eisenschwamm wird mit einer Temperatur von etwa 750° bis 800°C unten aus dem Direktreduktionsschachtofen 2 ausgetragen und kontinuierlich von oben in den Einschmelzvergaser chargiert. Im Einschmelzvergaser wird aus über öffnungen 6 eingebrachter Kohle und durch zwölf radial angeordnete Düsen 7 eingeblasenem sauerstoffhaltigem Gas, insbesondere Sauerstoff und Luft, ein Kohlefließbett 8 gebildet, in dem auch größere Eisenschwammpartikel merklich abgebremst und bis zum Eintritt in eine Hochtemperaturzone im unteren Abschnitt des Kohlefließbettes um einen wesentlichen Betrag in ihrer Temperatur erhöht und schließlich aufgeschmolzen werden.The hot sponge iron obtained by reducing the lumpy iron ore is discharged from the direct reduction shaft furnace 2 at a temperature of about 750 ° to 800 ° C. and continuously charged into the melter gasifier from above. A coal fluidized bed 8 is formed in the melter gasifier from coal introduced through openings 6 and oxygen-containing gas, in particular oxygen and air, which is blown in through twelve radially arranged nozzles 7, in which even larger iron sponge particles are noticeably decelerated and up to the entry into a high-temperature zone in the lower section of the coal fluidized bed one substantial amount in their temperature and finally be melted.

Oberhalb des Kohlefließbettes 8 schließt sich ein Beruhigungsraum an, in den radiale Düsen 9 münden, durch die zur Kühlung des im Einschmelzvergaser erzeugten heißen Reduktionsgases Wasserdampf, Kohlenwasserstoffe oder ein beispielsweise auf 50°C herabgekühltes Reduktionsgas eingeblasen werden. Das im Einschmelzvergaser erzeugte Reduktionsgas verläßt den Einschmelzvergaser oberhalb des Beruhigungsraumes durch zwei Gasauslässe 10 mit einer Temperatur zwischen 1200 und 1400°C und einem Druck von etwa 2 bar. Es gelangt dann zu einer Mischstelle 11, in der es mit Kühlgas ausreichend niedriger Temperatur auf die für die . Direktreduktion notwendige Temperatur, in der Regel von 760 bis 850°C, gebracht wird. Die Mischstelle ist strömungstechnisch so ausgebildet, daß ein Teil der kinetischen Energie des Kühlgases nach Durchmischung mit dem heißen vom Einschmelzvergaser gelieferten Reduktionsgas als Druck wiedergewonnen wird und damit der Druckverlust im Heißgasweg möglichst gering gehalten wird. Von der Mischstelle gelangt das Gas zu einem Zyklonabscheider 12, in dem der mit dem Gasstrom mitgerissene Koksstaub und Asche weitgehend abgeschieden werden. Sodann wird der auf die vorgeschriebene Prozesstemperatur abgekühlte und gereinigte Heißgasstrom geteilt, und zwar werden etwa 60 Vol.-% hiervon als erster Teilgasstrom 13 durch den Gaseinlaß 4 in die Reduktionszone des Direktreduktionsschachtofens 2 eingeblasen, während der andere Teil zur Kühlgasgewinnung einem Einspritzkühler 14 und dann einem Waschturm 15 zugeführt wird. Das hier austretende Kühlgas wird durch einen Kompressor 16 komprimiert und mit einer Temperatur von etwa 50°C zur Temperaturregelung des aus dem Einschmelzvergaser austretenden heißen Reduktionsgases der Mischstelle 11, zur Temperaturregelung des Reduktionsgases im Einschmelzvergaser den.Düsen 9 und ferner, wie später beschrieben, einer Ringleitung 22 zugeführt.Above the coal fluidized bed 8 there is a calming space into which radial nozzles 9 open, through which water vapor, hydrocarbons or a reducing gas, for example cooled down to 50 ° C., are blown in to cool the hot reducing gas generated in the melter gasifier. The reducing gas generated in the melter gasifier leaves the melter gasifier above the settling chamber through two gas outlets 10 with a temperature between 1200 and 1400 ° C. and a pressure of about 2 bar. It then arrives at a mixing point 11, in which it is at a sufficiently low temperature for the cooling gas. Direct reduction necessary temperature, usually from 760 to 850 ° C, is brought. In terms of flow technology, the mixing point is designed such that a part of the kinetic energy of the cooling gas is recovered as pressure after mixing with the hot reducing gas supplied by the melter gasifier, and the pressure loss in the hot gas path is thus kept as low as possible. From the mixing point, the gas reaches a cyclone separator 12, in which the coke dust and ash entrained with the gas flow are largely separated. Then the hot gas stream cooled and cleaned to the prescribed process temperature is divided, namely about 60 vol .-% of which are blown as the first partial gas stream 13 through the gas inlet 4 into the reduction zone of the direct reduction shaft furnace 2, while the other part for cooling gas extraction is an injection cooler 14 and then a washing tower 15 is supplied. The cooling gas emerging here is compressed by a compressor 16 and at a temperature of approximately 50 ° C. for temperature control of the hot reducing gas of the mixing point 11 emerging from the melter gasifier, to control the temperature of the reducing gas in the melter, the nozzles 9 and, as described later, a ring line 22.

Für den Heißaustrag der Eisenschwammpartikel aus dem.Direktreduktionsschachtofen 2 sind symmetrisch zur Mittelachse des.Ofens radial sechs Schneckenförderer 17 angeordnet, die als Paddelschnecken ausgebildet und einseitig gelagert sind. Die Austrittsöffnung 18 jedes Schneckenförderers steht mit einer Verbindungsleitung in Form eines Fallrohres 19 in Verbindung, die durch die Decke des Einschmelzvergasers 1 in den Beruhigungsraum dieses Vergasers mündet. Es sind demnach im vorliegenden Fall auch sechs axialsymmetrisch angeordnete Fallrohre vorgesehen. Möglichst nahe am Eintritt in den Einschmelzvergaser mündet in jedes Fallrohr eine Düse 21 aus einer Ringleitung 22, der vom Kompressor 16 ein als dritter Teilgasstrom 23 bezeichneter Strom des auf 50°C abgekühlten und gereihigten vom Einschmelzvergaser gelieferten Reduktionsgases zugeführt wird.For the hot discharge of the sponge iron particles from the direct reduction shaft furnace 2, six screw conveyors 17 are arranged radially symmetrically to the central axis of the furnace, which are designed as paddle screws and are supported on one side. The outlet opening 18 of each screw conveyor is connected to a connecting line in the form of a downpipe 19 which opens through the ceiling of the melter gasifier 1 into the settling chamber of this gasifier. Accordingly, six axially symmetrically arranged downpipes are also provided in the present case. As close as possible to the entrance to the melter gasifier, a nozzle 21 from a ring line 22 opens into each downpipe, to which the compressor 16 feeds a stream of the reducing gas, which has been cooled to 50 ° C and is supplied by the melter gasifier, and which is called the third partial gas stream 23.

Während bei bekannten Verfahren und Anlagen durch aufwendige Maßnahmen verhindert wird, daß das ungereinigte und zu heiße Reduktionsgas ohne Aufbereitung in den Direktreduktionsschachtofen gelangen kann, wird bei dem vorliegenden Verfahren ein begrenzter Gasstrom unmittelbar vom Einschmelzvergaser über die Austragvorrichtung 17 für den heißen Eisenschwamm im Gegenstrom zu diesem zugelassen. Der gesamte, direkt aus dem Einschmelzvergaser in die Fallrohre strömende Gasstrom aus ungereinigtem Reduktionsgas ist als zweiter Teilgasstrom 24 bezeichnet. Die Temperatur des in die Fallrohre 19 einströmenden zweiten Teilgasstromes 24 'wird mittels des über die Düsen 21 in geregelter Menge eingeleiteten Kühlgases auf eine Temperatur zwischen 760 und 850°C abgekühlt, bevor die Gasströme über die Schneckenförderer 17 in den Reduktionsschachtofen gelangen. Das Kühlgas wird so zugeführt, daß eine besonders gute Verwirbelung mit dem aufsteigenden Rohgas eintritt. Der beim Eintritt in den Schneckenförderer 17 im aufsteigenden Gasstrom enthaltene Staub setzt sich im wesentlichen im Bereich des Schneckenförderers ab und wird sukzessive zusammen mit den Eisenschwammpartikeln wieder in das betreffende Fallrohr und in den Einschmelzvergaser zurück befördert.While in known methods and systems, complex measures prevent the unpurified and too hot reducing gas from entering the direct reduction shaft furnace without preparation, in the present method a limited gas flow is directly from the melter gasifier via the discharge device 17 for the hot sponge iron in counterflow to the latter authorized. The entire gas stream from unpurified reducing gas flowing directly from the melter gasifier into the downpipes is referred to as second partial gas stream 24. The temperature of the second partial gas stream 24 'flowing into the downpipes 19 is cooled to a temperature between 760 and 850 ° C. by means of the cooling gas introduced in a controlled amount via the nozzles 21 before the gas streams via the Screw conveyor 17 get into the reduction shaft furnace. The cooling gas is supplied in such a way that there is particularly good swirling with the rising raw gas. The dust contained in the ascending gas stream when entering the screw conveyor 17 settles essentially in the area of the screw conveyor and is successively conveyed back together with the sponge iron particles back into the downpipe in question and into the melter gasifier.

Wesentlich ist eine Begrenzung des zweiten Teilgasstromes 24, d.h. also der über die sechs Fallrohre 19 unmittelbar vom Einschmelzvergaser nach oben strömenden Rohgasmenge auf einen Anteil von maximal 30 Vol.-% der gesamten in den Direktreduktionsschachtofen eingeleiteten Reduktionsgasmenge. Zu diesem Zweck ist es erforderlich, daß der Strömungswiderstand für den zweiten Teilgasstrom 24 im Strömungsweg bis zur Reduktionszone im Direktreduktionsschachtofen, d.h. also bis zur Ebene des Gaseinlasses 4, größer ist als der Strömungswiderstand für den ersten Teilgasstrom 13 im Strömungsweg vom Gasauslaß 10 bis zum Gaseinlaß 4. Dieser Forderung kommt die Ausbildung der Austragvorrichtung 17 als Schneckenförderer, deren Förderteil als Paddelschnecke ausgebildet ist, entgegen. Im übrigen werden der Strömungswiderstand und damit die Druckverluste im Strömungsweg des ersten Teilgasstromes 13 bewußt klein gehalten.It is essential to limit the second partial gas stream 24, i.e. That is, the amount of raw gas flowing directly upwards from the melter gasifier via the six downpipes 19 to a maximum of 30% by volume of the total amount of reducing gas introduced into the direct reduction shaft furnace. For this purpose it is necessary that the flow resistance for the second partial gas stream 24 in the flow path up to the reduction zone in the direct reduction shaft furnace, i.e. So up to the level of the gas inlet 4, is greater than the flow resistance for the first partial gas flow 13 in the flow path from the gas outlet 10 to the gas inlet 4. This requirement meets the design of the discharge device 17 as a screw conveyor, the conveyor part is designed as a paddle screw. In addition, the flow resistance and thus the pressure losses in the flow path of the first partial gas stream 13 are deliberately kept low.

Durch die erfindungsgemäße Ausbildung des Verfahrens und der Vorrichtung wird ein unmittelbarer kontinuierlicher Transport der heißen Eisenschwammpartikel aus dem Direktreduktionsschachtofen 2 in den Einschmelzvergaser 1 ermöglicht, ohne daß Schleusen oder andere aufwendige Einrichtungen zur Abdichtung gegenüber dem heißen Reduktionsgas erforderlich sind, die bei der hohen Temperatur und der Art des zu fördernden Materials nur unter Schwierigkeiten mit der erforderlichen Betriebssicherheit realisierbar sind.The inventive design of the method and the device enables a direct continuous transport of the hot sponge iron particles from the direct reduction shaft furnace 2 into the melter gasifier 1 without locks or other complex devices for sealing against the hot reducing gas being required, which at the high temperature and A rt of the material to be conveyed can only be realized with difficulty with the required operational safety.

In Fig. 2 ist teilweise im Längsschnitt einer der sechs Schneckenförderer 17 dargestellt. Der Schneckenförderer ist . an einem mit dem Mantel des Direktreduktionsschachtofens verschweißten Stutzen 31 angeflanscht. Im Stutzen 31 befindet sich an der Austrittsseite 18 des Förderers ein Austrittsstutzen 32 zum Anflanschen eines Fallrohres 19 (siehe auch Fig. 1). Als Verschleißschutz für das Mauerwerk umhüllt den Förderteil ein Hüllrohr 33, das ebenfalls am Stutzen 31 angeflanscht ist.2 one of the six screw conveyors 17 is shown partially in longitudinal section. The screw conveyor is. flanged to a socket 31 welded to the jacket of the direct reduction shaft furnace. In the socket 31 there is an outlet socket 32 on the outlet side 18 of the conveyor for flange-mounting a downpipe 19 (see also FIG. 1). As a wear protection for the masonry, the conveying part envelops a cladding tube 33, which is also flanged to the socket 31.

Der Schneckenförderer 17 enthält einen in den Ofen hineinragenden Förderteil 36 sowie einen am Stutzen 31 angeflanschten aus dem Ofen herausragenden Lagerteil 34 und einen Antriebsteil 44.The screw conveyor 17 contains a conveyor part 36 protruding into the furnace, a bearing part 34 flanged out of the furnace on the connecting piece 31 and a drive part 44.

Der Förderteil 36 hat die Form eines durch Paddeln 37 gebildeten unterbrochenen Schneckengangs, wobei sich die gestrichelt eingezeichnete Umhüllende 38 der Paddelschnecke zum freien Ende der Welle 35 hin konisch verjüngt. Dieses freie Ende reicht bis nahezu in die Mitte des Schachtofens und gewährleistet durch die konische Verjüngung der Umhüllenden . eine gleichmäßige Entnahme des Schüttgutes aus der Schüttsäule.The conveying part 36 has the shape of an interrupted worm gear formed by paddles 37, the envelope 38 of the paddle screw shown in broken lines tapering conically towards the free end of the shaft 35. This free end extends almost to the middle of the shaft furnace and ensures the conical tapering of the envelope. an even removal of the bulk material from the bulk column.

Die Welle 35 ist wassergekühlt und für diesen Zweck hohl ausgebildet mit einem Innenrohr 39, das kurz vor dem freien Ende der Welle 35 endet und in das das Kühlwasser eingeführt wird, welches sodann am freien Ende umgeleitet wird und im Ringspalt zwischen dem zentralen Rohr 39 und der Innenwand der Welle 35 zurückströmt.The shaft 35 is water-cooled and hollow for this purpose with an inner tube 39, which ends just before the free end of the shaft 35 and into which the cooling water is introduced, which is then diverted at the free end and in the annular gap between the central tube 39 and the inner wall of the shaft 35 flows back.

Der Antrieb 44 ist wie folgt aufgebaut. Zum Drehen der Welle 35 dient ein Klinkenschaltwerk 45 mit einem Rad 40, in dessen Zähne eine Klinke 41 eingreift, die drehbar an einem Hebel 42 befestigt ist, der wiederum drehbar auf der Welle 35 sitzt und mittels eines hydraulisch oder pneumatisch betätigbaren Kolben 43 um eine vorgegebene Winkelbewegung hin und her geschwenkt werden kann. Hierbei wird durch die Klinke 41 das Rad 40 jeweils um einen der Zahnteilung oder einem Vielfachen der Zahnteilung entsprechenden Betrag weitergedreht.The drive 44 is constructed as follows. To rotate the shaft 35, a ratchet mechanism 45 with a wheel 40, in the teeth of which a pawl 41 engages, which is rotatably attached to a lever 42, which in turn is rotatably seated on the shaft 35, and by means of a hydraulically or pneumatically actuated piston 43 by one predetermined angular movement can be pivoted back and forth. Here, the pawl 41 rotates the wheel 40 by an amount corresponding to the tooth pitch or a multiple of the tooth pitch.

Bei größeren Durchmessern des Direktreduktionsschachtofens kann es erforderlich sein, die Welle des Schneckenförderers durch den Ofen zu führen und beidseitig in der Wand des Ofengefäßes zu lagern. In diesem Fall ist es zweckmäßig, die Schneckengänge vom Zentrum aus gegenläufig, d. h. zum Umfang fördernd, anzuordnen.With larger diameters of the direct reduction shaft furnace, it may be necessary to pass the shaft of the screw conveyor through the furnace and to store it on both sides in the wall of the furnace vessel. In this case, it is advisable to reverse the screw flights from the center, i. H. promoting to scope.

Claims (12)

1. Verfahren zur. direkten Erzeugung von flüssigem Roheisen aus stückigem Eisenerz, das in einem Direktreduktionsschachtofen in Form einer losen Schüttung mittels eines heißen Reduktionsgases zu Eisenschwamm reduziert und dann durch eine Austragvorrichtung im heißen Zustand einem Einschmelzvergaser zugeführt wird, in dem aus eingebrachter Kohle und eingeblasenem sauerstoffhaltigen Gas die zum Schmelzen des Eisenschwamms erforderliche Wärme und das Reduktionsgas erzeugt werden, von dem ein erster Teilgasstrom nach einer Abkühlung auf die für die Reduktion vorgeschriebene Temperatur und einer Entstaubung in die Reduktionszone des Direktreduktionsschachtofens eingeblasen wird, dadurch gekennzeichnet, daß die heißen Eisenschwammpartikel durch die Austragvorrichtung auf direktem Weg über wenigstens eine Verbindungsleitung (19) in den Einschmelzvergaser (1) gefördert werden und ein sich über diesen direkten Weg zwischen Einschmelzvergaser und Direktreduktionsschachtofen (2) im Gegenstrom zu den Eisenschwammpartikeln ausbildender zweiter Teilgasstrom (24) des Reduktionsgases auf maximal 30 Vol.-% der insgesamt in den Direktreduktionsschachtofen eingeleiteten Reduktionsgasmenge begrenzt und im Bereich der Verbindungsleitung auf eine Temperatur von unterhalb 950°C gekühlt wird.1. Procedure for. Direct production of molten pig iron from lumpy iron ore, which is reduced to sponge iron in a direct reduction shaft furnace in the form of a loose bed by means of a hot reducing gas and is then fed through a discharge device in the hot state to a melter gasifier, in which the melted coal and injected oxygen-containing gas are used to melt it required heat of the sponge iron and the reducing gas are generated, from which a first partial gas stream is blown into the reduction zone of the direct reduction shaft furnace after cooling to the temperature prescribed for the reduction and dedusting, characterized in that the hot sponge iron particles are discharged directly through the discharge device at least one connecting line (19) are conveyed into the melter gasifier (1) and one itself Using this direct route between the melter gasifier and the direct reduction shaft furnace (2) in counterflow to the sponge iron particles forming the second partial gas stream (24) of the reducing gas to a maximum of 30 vol.% of the total amount of reducing gas introduced into the direct reduction shaft furnace and in the area of the connecting line to a temperature of below 950 ° C is cooled. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der Anteil des zweiten Teilgasstromes (24) an der dem Direktreduktionsschachtofen (2) zugeführten Reduktionsgasmenge zwischen 5 und 15 Vol.-% liegt.2. The method according to claim 1, characterized in that the proportion of the second partial gas stream (24) in the direct reduction shaft furnace (2) supplied reducing gas amount is between 5 and 15 vol .-%. 3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß der Anteil des zweiten Teilgasstroms (24) an der dem Direktreduktionsschachtofen (2) zugeführten Reduktionsgasmenge zwischen 8 und 10 Vol.-% liegt.3. The method according to claim 2, characterized in that the proportion of the second partial gas stream (24) in the direct reduction shaft furnace (2) supplied reducing gas amount is between 8 and 10 vol .-%. 4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der zweite Teilgasstrom (24) im Bereich der Verbindungsleitung (19) auf eine Temperatur zwischen 750 und 850°C gekühlt wird.4. The method according to any one of claims 1 to 3, characterized in that the second partial gas stream (24) in the region of the connecting line (19) is cooled to a temperature between 750 and 850 ° C. 5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß der zweite Teilgasstrom (24) im Bereich der Verbindungsleitung (19) durch Beimischen eines dritten Teilgasstromes (23) des im Einschmelzvergaser (1) erzeugten Reduktionsgases gekühlt wird, nachdem dieses gereinigt und ausreichend abgekühlt worden ist.5. The method according to any one of claims 1 to 4, characterized in that the second partial gas stream (24) is cooled in the region of the connecting line (19) by admixing a third partial gas stream (23) of the reducing gas generated in the melter gasifier (1) after it has been cleaned and has been cooled sufficiently. 6. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß das Gas des dritten Teilgasstromes (23) auf eine Temperatur von etwa 50°C abgekühlt wird, bevor es mit dem zweiten Teilgasstrom (24) vermischt wird.6. The method according to claim 5, characterized in that the gas of the third partial gas stream (23) is cooled to a temperature of about 50 ° C before it is mixed with the second partial gas stream (24). 7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß der Strömungswiderstand für den ersten Teilgasstrom (13) im Strömungsweg zwischen dem Einschmelzvergaser (1) und dem Eintritt (4) in die Reduktionszone wesentlich kleiner als der Strömungswiderstand für den zweiten und dritten Teilgasstrom (24, 23) im Strömungsweg zwischen dem Einschmelzvergaser und dem Eintritt in die Reduktionszone gehalten wird. : 7. The method according to any one of claims 1 to 6, characterized in that the flow resistance for the first partial gas flow (13) in the flow path between the melter gasifier (1) and the inlet (4) in the reduction zone is substantially smaller than the flow resistance for the second and third partial gas stream (24, 23) is kept in the flow path between the melter and the entry into the reduction zone. : 8. Vorrichtung zur Durchführung des Verfahrens nach einem der Ansprüche 1 bis 7 mit einem oberhalb eines Einschmelzvergasers angeordneten Direktreduktionsschachtofen , der am unteren Ende eine Austragsvorrichtung (17) für heißen Eisenschwamm mit mindestens einer Austrittsöffnung aufweist, die mit dem Einschmelzvergaser in Verbindung steht, dadurch gekennzeichnet, daß an die Austrittsöffnung (18) der Austragsvorrichtung eine unmittelbar in den Einschmelzvergaser (1) mündende Verbindungsleitung (19) mit einem zusätzlichen seitlichen Gaseinlaß für Kühlgas angeschlossen ist.8. Device for performing the method according to one of claims 1 to 7 with a direct reduction shaft furnace arranged above a melter gasifier, which has at the lower end a discharge device (17) for hot sponge iron with at least one outlet opening which is connected to the melter gasifier, characterized that a connection line (19) opening directly into the melter gasifier (1) and having an additional lateral gas inlet for cooling gas is connected to the outlet opening (18) of the discharge device. 9. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß die Austragsvorrichtung in Form von über den Querschnitt verteilt angeordneten Schneckenförderern (17) ausgebildet ist.9. The device according to claim 8, characterized in that the discharge device is designed in the form of screw conveyors distributed over the cross section (17). 10. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß die Austragsvorrichtung in Form von fliegend gelagerten, radial angeordneten Schneckenförderern (17) ausgebildet ist.10. The device according to claim 8, characterized in that the discharge device is in the form of cantilevered, radially arranged screw conveyors (17). 11. Vorrichtung nach Anspruch 9 oder 10, dadurch gekennzeichnet, daß der Förderteil (36) der Schneckenförderer (17) in Form eines durch Paddeln (37) gebildeten unterbrochenen Schneckengangs ausgebildet ist.11. The device according to claim 9 or 10, characterized in that the conveying part (36) of the screw conveyor (17) is designed in the form of an interrupted screw flight formed by paddles (37). 12. Vorrichtung nach einem der Ansprüche 9 bis 11, dadurch gekennzeichnet, daß sich die Umhüllende (38) des Förderteils (36) der Schneckenförderer (17) zur Eintrittsseite des Schneckenförderers hin konisch verjüngt.12. Device according to one of claims 9 to 11, characterized in that the envelope (38) of the conveying part (36) of the screw conveyor (17) tapers conically towards the entry side of the screw conveyor.
EP81107215A 1980-09-12 1981-09-12 Method and apparatus for the direct production of hot metal from lump iron ore Expired EP0048008B1 (en)

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PL133135B1 (en) 1985-05-31
US4409023A (en) 1983-10-11
CA1189705A (en) 1985-07-02
AU542484B2 (en) 1985-02-21
KR830007847A (en) 1983-11-07
JPS57120607A (en) 1982-07-27
ES8206634A1 (en) 1982-08-16
US4448402A (en) 1984-05-15
DE3034539A1 (en) 1982-03-25
ES505397A0 (en) 1982-08-16
PH18291A (en) 1985-05-20
PL232996A1 (en) 1982-04-26
BR8105812A (en) 1982-06-08
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GB2084196A (en) 1982-04-07
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GB2084196B (en) 1984-08-08
MX158677A (en) 1989-02-27
EP0048008B1 (en) 1984-08-01
UA6580A1 (en) 1994-12-29
AU7476681A (en) 1982-03-18
ATE8799T1 (en) 1984-08-15

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