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WO2000037687A1 - Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe - Google Patents

Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe Download PDF

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Publication number
WO2000037687A1
WO2000037687A1 PCT/KR1998/000451 KR9800451W WO0037687A1 WO 2000037687 A1 WO2000037687 A1 WO 2000037687A1 KR 9800451 W KR9800451 W KR 9800451W WO 0037687 A1 WO0037687 A1 WO 0037687A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluidized bed
iron ore
furnace
bed furnace
fine iron
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.)
Ceased
Application number
PCT/KR1998/000451
Other languages
English (en)
Inventor
Hang Goo Kim
Il Ock Lee
Heung Won Kang
Sun Kwang Jeong
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
Research Institute of Industrial Science and Technology RIST
Posco Holdings Inc
Original Assignee
Voest Alpine Industrienlagenbau GmbH
Research Institute of Industrial Science and Technology RIST
Pohang Iron and Steel Co Ltd
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, Research Institute of Industrial Science and Technology RIST, Pohang Iron and Steel Co Ltd filed Critical Voest Alpine Industrienlagenbau GmbH
Priority to PCT/KR1998/000451 priority Critical patent/WO2000037687A1/fr
Priority to EP98961657A priority patent/EP1060273A1/fr
Priority to JP2000589740A priority patent/JP2002533642A/ja
Priority to BR9815681-0A priority patent/BR9815681A/pt
Priority to CA002322130A priority patent/CA2322130A1/fr
Priority to AU16934/99A priority patent/AU1693499A/en
Publication of WO2000037687A1 publication Critical patent/WO2000037687A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

Definitions

  • the present invention relates to a fluidized bed type reducing apparatus and a reducing method, in which a fine iron ore of a wide particle size distribution is reduced by fluidized bed type furnaces into directly reduced iron of 85% or more of reduction degree, so that a melter- gasifier can melt it to manufacture a molten iron.
  • the present invention relates to a complex fluidized bed type fine iron ore reducing apparatus and a reducing method, in which a high temperature reducing gas having 60 ⁇ 100% of CO + H2 at 800-900°C is utilized in the consideration of the wide particle size distribution, the degradation and the reducibility at a high temperature, so that the reaction rate of the solid fine iron ore, the gas utilization degree and the gas consumption rate can be most advantageously improved, thereby making it possible to achieve a good economy and the optimum operation.
  • a high temperature reducing gas having 60 ⁇ 100% of CO + H2 at 800-900°C is utilized in the consideration of the wide particle size distribution, the degradation and the reducibility at a high temperature, so that the reaction rate of the solid fine iron ore, the gas utilization degree and the gas consumption rate can be most advantageously improved, thereby making it possible to achieve a good economy and the optimum operation.
  • the iron particles used in the blast furnace are of large size, and therefore, the iron ore can be reduced with the fixed bed type furnaces.
  • the gas velocity is very slow like that in the fixed bed type furnace, sticking may occur, and therefore, the operation may be interrupted.
  • the fluidized bed type furnaces are necessarily used in order to ensure a good gas permeability and a brisk movement of fine iron ore particles in the bed.
  • Japanese Utility Model Gazette Sho-58-217615 is an i 2 example of the fluidized bed type furnace which is for reducing a fine iron ore.
  • This fluidized bed type furnace is divided into a cylindrical reducing furnace and a cyclone.
  • the cylindrical reducing furnace includes: a raw iron ore charging inlet; a reducing gas inlet for introducing a reducing gas; and a discharging outlet for discharging a reduced iron ore.
  • a gas distributor Within the lower portion of the reducing furnace, there is installed a gas distributor. The reducing gas is introduced through gas distributor, while the fine iron ore is fed through the charging inlet. Then the iron ore is reacted with the reducing gas while being agitated.
  • the form of the fluidized bed is such that the reducing gas forms bubbles above the gas distributor, and that the bubbles pass through an iron ore particle layer while increasing in their size.
  • this conventional fluidized bed type furnace aims at reducing the elutriation loss of the fine iron ore out of the furnace, at minimizing the gas consumption rate, and at maximizing the gas utilization degree.
  • the particle size is sternly restricted, and therefore, it cannot cope with an iron ore having a wide particle size distribution. That is, the particle size distribution cannot be wide, but should be limited to 0- 0.5 mm, 0-1 mm, or 1-2 mm.
  • the particle size of the raw fine iron ore in the world is mostly 8 mm or less. Therefore, the raw iron ore has to be screened by means of a sieve to exclude the coarse particles, or the iron ore has to be crushed. As a result, the production rate is lowered, and the _# 3 additional process and facilities are required, thereby aggravating the economy.
  • Korean Patent No. 074056 discloses a twin type fluidized bed furnaces for reducing fine iron ore.
  • FIG. 1 illustrates the twin type fluidized bed reducing furnace.
  • the twin type fluidized bed reducing furnace includes: a first fluidized bed furnace 10 for reducing a coarse iron ore; a second fluidized bed furnace 20 for reducing medium/fine iron ores; and a cyclone 30 for capturing extremely fine iron ore particles.
  • a reducing gas supplying hole 11 is formed on the bottom of the first fluidized bed furnace 10, and a gas distributor 12 is installed in the lower part of the furnace 10. Further, a first discharging hole 13 is formed on a side wall of the furnace 10, and a second discharging hole 15 is formed on an upper portion of the side wall of the furnace 10. The second discharging hole 15 is connected through a first conduit 16 to a lower portion of the second fluidized bed furnace 20. Further, an iron ore supplying hole 14 is formed on a lower portion of the other side of the first furnace 10. Further, a reducing gas supplying hole 21 is formed on the bottom of the second fluidized bed furnace 20, and a gas distributor 22 is installed within the lower portion of the furnace 20.
  • a third discharging hole 23 is formed on a side of the furnace 20, and the top of the furnace 20 is connected to the cyclone 30.
  • the bottom of the cyclone 30 is connected through a 6th conduit 35 to a lower portion of the furnace 20.
  • a gas discharging hole 33 is formed on the top of the cyclone 30 so as to exhaust V
  • a fine iron ore is supplied through the iron ore supplying hole 14 into the first fluidized bed furnace 10, Under this condition, a reducing gas is supplied through the first reducing gas supplying hole 11, and the gas velocity of the reducing gas is adjusted, so that only the coarse iron ore particles would remain within the first fluidized bed furnace 10. In this manner, a bubbling or turbulent fluidized bed is formed, and the coarse particles are reduced within the fluidized bed of the first furnace 10.
  • the medium/fine iron ore particles are carried(elutriated) through the first conduit 16 into the second fluidized bed furnace 20.
  • a reducing gas is supplied through the second gas supplying hole 21 into the second furnace 20 so as to form a bubbling or turbulent fluidized bed. Therefore, the medium/fine iron ores are reduced by the turbulent fluidized bed within the second furnace 20.
  • the iron ore is reduced after being separated into the coarse iron ore and the medium/fine iron ores by adjusting the gas velocity.
  • a fine iron ore having a wide particle size distribution is stabilized, and the concentrations of the iron ore are made uniform in the fluidized bed. Therefore, by the separation the reduction degree can be improved, and the particle elutriation loss can be decreased, while the gas consumption rate is also decreased.
  • the present invention is intended to overcome the above described disadvantages of the conventional techniques .
  • the complex fluidized bed type apparatus for reducing a fine iron ore includes: first and second fluidized bed furnaces and a cyclone, with a gas distributor being installed in the lower portion of each of the furnaces, and with a reducing gas supplying hole being formed on the bottom of each of them; the fine iron ore being separated into coarse iron ore particles and medium/fine iron ore particles within the first fluidized bed furnace, the coarse iron ore particles being reduced -_#
  • the medium /fine iron ore particles being transported through a second discharging hole into the second fluidized bed furnace so as to be reduced while forming a fluidized bed, before being discharged through an iron ore discharging hole; and the cyclone separating extremely fine iron ore particles from a exhaust gas of the second fluidized bed furnace to circulate the fine iron ore particles back to the second fluidized bed furnace, characterized in that: the first fluidized bed furnace is installed within a freeboard zone (upper portion of the second fluidized bed furnace) within the second fluidized bed furnace; the second discharging hole for discharging the medium/fine iron ore particles and the gas from the first fluidized bed furnace is connected through a first conduit into a lower portion of the second fluidized bed furnace; and the cyclone is connected from its bottom through a 6th conduit (which passes through an upper portion of the second fluidized bed furnace) into the lower portion of the second fluidized bed furnace.
  • the gas velocity within the first fluidized bed furnace is 1.2-2.5 times as fast as the minimum fluidization velocity of the iron ore staying within the furnace. Further, the gas velocity within the second fluidized bed furnace is 1.2-1.8 times as fast as the minimum fluidization velocity of the iron ore staying within the furnace.
  • FIG. 1 illustrates the conventional twin type fluidized bed furnaces for reducing fine iron ore
  • FIG. 2 illustrates the constitution of the complex fluidized bed apparatus for reducing a fine iron ore according to the present invention.
  • the complex fluidized bed type apparatus for reducing a fine iron ore includes: a complex fluidized bed furnace consisting of first and second fluidized bed furnaces 100 and 200, the first furnace 100 being for separating the fine iron ore into coarse iron ore particles and medium/fine iron ore particles and for reducing the coarse iron ore particles while forming a bubbling fluidized bed; the second furnace 200 being for reducing the medium/fine iron ore particles transported from the furnace 100 while forming a bubbling fluidized bed; and a cyclone 300 for separating the extremely fine iron ore particles from a exhaust gas of the second fluidized bed furnace 200 to circulate the fine particles back to the second fluidized bed furnace 200.
  • the first fluidized bed furnace 100 is installed within the second fluidized bed furnace 200, so that the heat loss and the installation space can be drastically decreased.
  • FIG. 2 illustrates the constitution of the complex fluidized bed type apparatus for reducing a fine iron ore according to the present invention.
  • the apparatus for reducing a fine iron ore according to the present invention includes: a first fluidized bed furnace 100 installed within a freeboard zone above a fluidized bed of _# 8 medium/fine iron ore particles within a second fluidized bed furnace 200, for separating the fine iron ore into coarse iron ore particles and medium/fine iron ore particles by the means of an adjusted gas velocity in the furnace 100, to reduce the coarse particles remained within the first fluidized bed furnace 100 while forming a bubbling or turbulent fluidized bed by a reducing gas supplied through a first gas supplying hole 101, and to transport the medium/fine particles through a first conduit 106 into a lower portion of the second fluidized bed furnace 200; the second fluidized bed furnace 200 being for reducing the medium/fine iron ore particles (transported from the first fluidized bed furnace with a exhaust gas ) by a reducing gas of a low gas velocity supplied
  • the first fluidized bed furnace 100 has an approximately cylindrical shape, and has a first gas supplying hole 101 on its bottom.
  • a gas distributor 102 is installed within the lower portion of the furnace 100.
  • the side wall of the furnace 100 has a first discharging hole 103 which is connected to a third conduit 108.
  • On another side of the furnace 100 there is formed an iron ore supplying hole 104 which is connected to a second conduit 107.
  • Above the hole 104 there is formed a second discharging hole 105 for discharging the iron ore and the gas, and the hole 105 is connected through a first conduit 106 into the lower portion of the second fluidized bed furnace 200.
  • the second fluidized bed furnace 200 consists of two cylindrical parts, a wide upper portion and a narrow lower portion.
  • the second furnace 200 includes: an expanded portion 200c having a large inner diameter, a narrow portion 200a having a small inner diameter, and a tapered portion 200b for connecting the expanded portion 200c to the narrow portion 200a.
  • the iron ore particles are made to move briskly by the help of the bubbling gas flow, and in this manner, the gas utilization degree is improved. Further, owing to the large diameter of the expanded portion 200c, the flying of the extremely fine iron ore particles are slowed, thereby inhibiting the elutriation loss of the particles .
  • a second gas supplying hole 201 is formed on the bottom of the narrow portion 200a, for receiving the reducing gas.
  • a second gas distributor 202 is installed within the lower portion of the narrow portion 200a.
  • a third discharging hole 203 which is connected to a 5th conduit 205 for discharging the reduced iron ore.
  • a fourth discharging hole 204 is formed on the top of the expanded portion 200c, and from this top, a 7th conduit 306 extends to the cyclone 300.
  • the cyclone 300 separates the extremely fine iron ore particles from the exhaust gas of the second fluidized bed furnace 200, the exhaust gas being introduced through the 7th conduit 306 into the inlet 301. These separated particles are circulated back into the lower portion of the furnace 200.
  • a 6th conduit 305 is connected into a hole 302.
  • a gas discharging hole 303 which is connected to a discharge pipe 304 to discharge the exhaust 87 _
  • the height of the first fluidized bed furnace 100 above the distributor 102 should be preferably 10 - 15 times as large as its inner diameter.
  • the reason is as follows. That is, if its height is less than 10 times as large as its inner diameter, the fluidizing of the iron ore within the furnace cannot be smoothly carried out, with the result that even medium/coarse iron particles are flown to be sent to the second fluidized furnace. On the other hand, if its height is more than 15 times as large as its inner diameter, then the elutriation loss of the fine iron ore is very large.
  • the height of the narrow portion 200a above the distributor 202 should be preferably 5 - 10 times as large as its inner diameter, so that a sufficient fluidizing space can be secured, and that the elutriation loss of the fine iron ore can be lowered.
  • the height of the expanded portion 200c should be preferably 2 - 4 times as large as its inner diameter, so that the gas velocity can be reduced within the furnace while lowering the elutriation loss of the fine iron ore.
  • the first fluidized bed furnace 100 should be installed within the freeboard zone of the second fluidized bed furnace 200. Further, the bottom of the first furnace 100 should be preferably placed at a position higher than the third iron ore discharging hole 203.
  • the reducing gas which is supplied into the first fluidized bed furnace 100 is maintained at a gas velocity 7687
  • the raw fine iron ore which is supplied into the first fluidized bed furnace 100 is separated into coarse iron ore particles and medium/fine iron ore particles.
  • the coarse iron ore particles are remained within the first fluidized bed furnace 100, so that they will be reduced while forming a bubbling or turbulent fluidized bed.
  • the medium/fine particles are carried through the first conduit 106 into the lower portion of the second fluidized bed furnace 200. These particles are reduced by a reducing gas (which is supplied through the second gas supplying hole 201), while forming a bubbling fluidized bed. Then the reduced iron ores are discharged through the first discharge hole 103 and the third discharge hole 203 respectively.
  • the extremely fine iron ore particles which are loaded in the exhaust gas of the second fluidized bed furnace 200 are supplied through the 7th conduit 306 into the cyclone 300.
  • the cyclone 300 separates the extremely fine particles from the exhaust gas to circulate the extremely fine particles back to the second fluidized bed furnace 200.
  • the gas velocity within the first fluidized bed furnace 100 should be preferably 1.2 - 2.5 times as fast as the minimum fluidization velocity of the iron ore particles staying within the furnace, considering the fluidizing and elutriation.
  • the gas velocity within the second fluidized bed type furnace 200 should be preferably 1.2 - 1.8 times as fast as the minimum fluidization velocity of the iron ore particles.
  • Second furnace ID of narrow portion 0.5 m
  • the average gas utilization degree and the gas consumption rate were evaluated.
  • the result showed that the gas utilization degree was about 30 - 35%, and the gas consumption rate was 1200 - 1300 Nm 3 /ton-ore.
  • the reduced iron ores which were discharged through the first discharging hole 103 and the third discharging hole 203 showed a reduction degree of 88 - 95%.
  • the fine iron ore particles showed somewhat higher reduction degree.
  • the reduced iron ore could be discharged within 60 minutes after the feeding of the raw iron ore from the hopper, thus it was seen that the production rate was excellent.
  • the internal temperature of the reaction chambers could be maintained at 850°C without any additional heat from the outside.
  • the reduction of the fine iron ore is carried out after segregation the particle sizes. Therefore, the gas consumption rate can be reduced like in the conventional method, but unlike in the conventional method, the heat loss can be reduced, and a sufficient heat can be secured without any external heat, because the first fluidized bed furnace is installed within the second fluidized bed furnace.
  • the conventional problems can be solved, while the installation space can be decreased.
  • an uniform reduction degree can be obtained regardless of the particle sizes, and the reduced fine iron ores of different particle size classes can be obtained. Therefore, when they are fed into a melting furnace, they can be fed through different feeding devices.
  • the amount and particle sizes of the reduced iron ores which are discharged through each discharging hole can be controlled by the adjustment of the height of the second discharging hole and gas velocity. Further, the residence time of the iron ore can be controlled, and therefore, the reduction degree can be controlled for the different particle sizes.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Dispersion Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture Of Iron (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Furnace Details (AREA)

Abstract

L'invention concerne un appareil du type à lit fluidisé complexe, à utiliser pour la réduction de minerai de fer fin et un procédé associé, dans lesquels la réactivité des particules de minerai de fer fin, et le gaz et son débit sont utilisés de la manière la plus efficace possible, de sorte qu'un minerai de fer fin présentant une dimension granulométrique élevée soit réduit de manière optimale. Ledit appareil comporte des premier (100) et deuxième fours à lit fluidisé et un cyclone (300), un distributeur de gaz étant installé dans la partie inférieure de chaque four (102, 202). Le minerai de fer fin est séparé en particules de minerai de fer grossières et moyennes/fines, dans le premier four à lit fluidisé (100) qui est installé dans une zone de revanche prévue dans le deuxième four à lit fluidisé (200). Un deuxième orifice de décharge (105) de minerai de fer communique par un conduit avec une partie inférieure du deuxième four à lit fluidisé (200). Le cyclone (300) communique par sa partie inférieure, grâce à un conduit (305), avec la partie inférieure du deuxième four à lit fluidisé (200).
PCT/KR1998/000451 1998-12-22 1998-12-22 Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe Ceased WO2000037687A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
PCT/KR1998/000451 WO2000037687A1 (fr) 1998-12-22 1998-12-22 Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe
EP98961657A EP1060273A1 (fr) 1998-12-22 1998-12-22 Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe
JP2000589740A JP2002533642A (ja) 1998-12-22 1998-12-22 複合流動層型微粉鉄鉱石還元装置、及びそのための方法
BR9815681-0A BR9815681A (pt) 1998-12-22 1998-12-22 Aparelho para redução de minério de ferro fino do tipo leito fluidificado complexo e seu método
CA002322130A CA2322130A1 (fr) 1998-12-22 1998-12-22 Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe
AU16934/99A AU1693499A (en) 1998-12-22 1998-12-22 Complex fluidized bed type fine iron ore reducing apparatus, and method therefor

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/KR1998/000451 WO2000037687A1 (fr) 1998-12-22 1998-12-22 Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe

Publications (1)

Publication Number Publication Date
WO2000037687A1 true WO2000037687A1 (fr) 2000-06-29

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PCT/KR1998/000451 Ceased WO2000037687A1 (fr) 1998-12-22 1998-12-22 Appareil et procede de reduction de minerai de fer fin, du type a lit fluidise complexe

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EP (1) EP1060273A1 (fr)
JP (1) JP2002533642A (fr)
AU (1) AU1693499A (fr)
CA (1) CA2322130A1 (fr)
WO (1) WO2000037687A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102699339A (zh) * 2012-06-29 2012-10-03 武汉钢铁(集团)公司 一种利用铁红制备超细铁粉的装置
WO2024149076A1 (fr) * 2023-01-09 2024-07-18 中国石油化工股份有限公司 Système de conversion catalytique fluidisé et son utilisation

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0585190A1 (fr) * 1992-08-25 1994-03-02 Sollac S.A. Installation de réduction du minerai de fer utilisant un lit fluidisé circulant
WO1997023655A1 (fr) * 1995-12-26 1997-07-03 Pohang Iron & Steel Co., Ltd. Four a lit fluidise a deux etages pour la prereduction de fines de fer et procede associe

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0585190A1 (fr) * 1992-08-25 1994-03-02 Sollac S.A. Installation de réduction du minerai de fer utilisant un lit fluidisé circulant
WO1997023655A1 (fr) * 1995-12-26 1997-07-03 Pohang Iron & Steel Co., Ltd. Four a lit fluidise a deux etages pour la prereduction de fines de fer et procede associe

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102699339A (zh) * 2012-06-29 2012-10-03 武汉钢铁(集团)公司 一种利用铁红制备超细铁粉的装置
WO2024149076A1 (fr) * 2023-01-09 2024-07-18 中国石油化工股份有限公司 Système de conversion catalytique fluidisé et son utilisation

Also Published As

Publication number Publication date
AU1693499A (en) 2000-07-12
EP1060273A1 (fr) 2000-12-20
CA2322130A1 (fr) 2000-06-29
JP2002533642A (ja) 2002-10-08

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