JPS62228879A - Iron ore spare reducing device - Google Patents
Iron ore spare reducing deviceInfo
- Publication number
- JPS62228879A JPS62228879A JP7156386A JP7156386A JPS62228879A JP S62228879 A JPS62228879 A JP S62228879A JP 7156386 A JP7156386 A JP 7156386A JP 7156386 A JP7156386 A JP 7156386A JP S62228879 A JPS62228879 A JP S62228879A
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- reduction
- ore
- furnace
- reduction furnace
- 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
Links
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims description 38
- 229910052742 iron Inorganic materials 0.000 title claims description 19
- 230000001603 reducing effect Effects 0.000 title description 20
- 239000002245 particle Substances 0.000 claims description 25
- 238000000034 method Methods 0.000 claims description 23
- 238000003723 Smelting Methods 0.000 claims description 19
- 238000006722 reduction reaction Methods 0.000 description 70
- 239000007789 gas Substances 0.000 description 34
- 239000003245 coal Substances 0.000 description 15
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 13
- 239000002994 raw material Substances 0.000 description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 239000003575 carbonaceous material Substances 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 7
- 235000012255 calcium oxide Nutrition 0.000 description 6
- 239000000292 calcium oxide Substances 0.000 description 6
- 239000011362 coarse particle Substances 0.000 description 6
- 238000002844 melting Methods 0.000 description 5
- 230000008018 melting Effects 0.000 description 5
- 235000019738 Limestone Nutrition 0.000 description 4
- 238000007664 blowing Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000006028 limestone Substances 0.000 description 4
- 238000005520 cutting process Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 239000004484 Briquette Substances 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000011946 reduction process Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000007873 sieving Methods 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000911 decarboxylating effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- QVGXLLKOCUKJST-AKLPVKDBSA-N oxygen-19 atom Chemical compound [19O] QVGXLLKOCUKJST-AKLPVKDBSA-N 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Manufacture Of Iron (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、溶融還元法に使用するため、鉄鉱石を流動層
予備還元炉で還元する装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application] The present invention relates to an apparatus for reducing iron ore in a fluidized bed pre-reduction furnace for use in a smelting reduction process.
鉄鉱石を還元して溶銑を製造するために、高炉を使用す
る方法５ シャフト炉で還元した鉄鉱石を電気炉で溶解
する方法等が従来から採用されている。Method 5 of using a blast furnace to reduce iron ore and produce hot metal A method of melting iron ore reduced in a shaft furnace in an electric furnace has been adopted conventionally.
高炉を使用する方法においては、熱源及び還元剤として
多量のコークスを使用している。また、鉄源である鉄鉱
石は、炉内における通気性、還元性を向上させるために
通常焼結され、焼結鉱として高炉に装入されている。こ
のようなことから、該高炉法は、強粘結炭を乾溜するた
めのコークス炉設備及び焼結鉱を製造するための焼結設
備を必要とする。したがって、該高炉法には、多大な設
備費は勿論のこと、多くのエネルギー及び労働が必要と
なる。このため、高炉法には処理コストが高くなるとい
う欠点があった。更に、強粘結炭は世界的に賦存量が少
なく、しかもその分布が地域的に偏っているため、供給
が不安定である。In the method using a blast furnace, a large amount of coke is used as a heat source and a reducing agent. Further, iron ore, which is an iron source, is usually sintered to improve air permeability and reducibility in the furnace, and is charged into the blast furnace as sintered ore. For this reason, the blast furnace method requires coke oven equipment for dry distilling highly caking coal and sintering equipment for producing sintered ore. Therefore, the blast furnace method requires a large amount of energy and labor as well as a large amount of equipment cost. For this reason, the blast furnace method has the disadvantage of high processing costs. Furthermore, the availability of strong coking coal is small worldwide, and its distribution is regionally uneven, making its supply unstable.
一方、シャフト炉による鉄鉱石の還元法では、鉄鉱石を
ペレット化する前処理を行うことが必要となり、また還
元剤、熱源として高価な天然ガス等を多量に消費すると
いう欠点がある。On the other hand, the method of reducing iron ore using a shaft furnace requires pretreatment to pelletize the iron ore, and has the disadvantage that it consumes a large amount of reducing agent and expensive natural gas as a heat source.
このような従来の溶銑製造技術に代わるものとして、溶
融還元法が注目を浴びている。この方法で使用する溶融
還元炉は、使用する原料に制約を受けることなく、より
小規模な設備により鉄系合金の溶湯を製造することを目
的として開発されたものである。As an alternative to such conventional hot metal production techniques, the smelting reduction method is attracting attention. The smelting reduction furnace used in this method was developed for the purpose of producing molten iron-based alloys using smaller-scale equipment without being restricted by the raw materials used.
このような溶融還元法の一つとして、本発明者等は、先
に第４図に示すようなフローで構成される方法を特願昭
５９−１８４０５６号として提案した。As one such melt reduction method, the present inventors previously proposed a method consisting of the flow shown in FIG. 4 in Japanese Patent Application No. 184056/1982.
この方法によるとき、次のようにして溶銑が製造される
。すなわち、鉄鉱石１及び石灰石２は、流動層予熱炉３
内で石炭４と空気５との燃焼反応で生じた熱によって加
熱される。その結果、石灰石２（ＣａＣＯｓ）は、生石
灰（Ｃａｂ）となって流動層予備還元炉６に供給される
。According to this method, hot metal is produced as follows. That is, iron ore 1 and limestone 2 are transported to a fluidized bed preheating furnace 3.
It is heated by the heat generated by the combustion reaction between coal 4 and air 5 inside. As a result, the limestone 2 (CaCOs) becomes quicklime (Cab) and is supplied to the fluidized bed pre-reduction furnace 6.
流動層予備還元炉６内では、流動状態の予熱鉱石及び生
石灰に、石炭７及び酸素又は酸素含有ガス８が吹き込ま
れる。この石炭７は、流動層予備還元炉６内で予熱鉱石
と熱交換し、また酸素との反応による部分燃焼によって
熱分解する。これによって、石炭７は、還元性のガスを
発生すると共に、チャー９となる。In the fluidized bed pre-reduction furnace 6, coal 7 and oxygen or oxygen-containing gas 8 are blown into the preheated ore and quicklime in a fluidized state. This coal 7 exchanges heat with the preheated ore in the fluidized bed pre-reduction furnace 6 and is thermally decomposed by partial combustion due to reaction with oxygen. As a result, the coal 7 generates reducing gas and becomes char 9.
他方、溶融還元炉１０で発生したガス又はそのガスを脱
炭酸処理して得られる還元ガス１１は、流動層予備還元
炉６からの燃料ガス１２との熱交換によって７００〜９
００℃に昇温された後、流動層予備還元炉６に吹き込ま
れる。流動層予備還元炉６に吹き込まれた還元ガス１１
は、石炭７の熱分解により生成した還元ガスと混合され
、流動状態にある高温の粉粒状鉄鉱石を還元し、還元鉱
１３を生成する。On the other hand, the gas generated in the smelting reduction furnace 10 or the reducing gas 11 obtained by decarboxylating the gas is reduced to 700 to 90% by heat exchange with the fuel gas 12 from the fluidized bed preliminary reduction furnace 6.
After being heated to 00°C, it is blown into a fluidized bed pre-reduction furnace 6. Reducing gas 11 blown into the fluidized bed preliminary reduction furnace 6
is mixed with the reducing gas produced by thermal decomposition of the coal 7, reduces the hot powdery iron ore in a fluidized state, and produces the reduced ore 13.
また、流動層予熱炉３内に生成した生石灰１４は、予熱
鉱石と共に流動層予備還元炉６に装入され、流動層予備
還元炉６内にあるガスの脱硫を行う。Moreover, the quicklime 14 produced in the fluidized bed preheating furnace 3 is charged into the fluidized bed prereduction furnace 6 together with the preheated ore, and the gas in the fluidized bed prereduction furnace 6 is desulfurized.
次いで、該生石灰１４は、還元鉱１３及びチャー９と共
に流動層予備還元炉６から排出される。Next, the quicklime 14 is discharged from the fluidized bed preliminary reduction furnace 6 together with the reduced ore 13 and the char 9.
このようにして得られた還元鉱１３．チャー９及び生石
灰１４に対して、溶融還元炉１０における熱バランス上
必要な石炭、コークス等の炭材が外部から加えられ、混
練される。次いで、混合物は、ブリケットマシン等の塊
成化装置１５によってブリケット１６に成形された後、
装入装置１７によって溶融還元炉ｌＯに装入される。Reduced ore thus obtained 13. Carbon materials such as coal and coke necessary for the heat balance in the smelting reduction furnace 10 are added to the char 9 and quicklime 14 from the outside and kneaded. Next, the mixture is formed into briquettes 16 by an agglomeration device 15 such as a briquette machine, and then
The charging device 17 charges the melt into the smelting reduction furnace IO.
この溶融還元炉１０内には、上吹きランス１８から酸素
１９が浴に向かって吹き付けられると共に、底吹き羽口
２０から浴中に酸素及び炭材が吹き込まれている。そし
て、ブリケット１６に含まれている炭材、底吹き羽目２
０から酸素と共に吹き込まれている炭材、装入装置１７
から供給されたコークス２１等の炭材は、上吹きランス
１８から供給された酸素と反応し、溶融還元炉１０内に
多量の熱を発生する。In this melting reduction furnace 10, oxygen 19 is blown toward the bath from a top blowing lance 18, and oxygen and carbonaceous material are blown into the bath from a bottom blowing tuyere 20. Then, the carbonaceous material contained in the briquette 16, the bottom-blown surface 2
Carbon material being blown in with oxygen from 0, charging device 17
The carbonaceous material such as coke 21 supplied from the top blowing lance 18 reacts with the oxygen supplied from the top blowing lance 18, and generates a large amount of heat in the melting reduction furnace 10.
この発生熱によって、ブリケット１６中の還元鉱１３が
熔解し、還元が進行して溶銑２２となる。This generated heat melts the reduced ore 13 in the briquettes 16, and the reduction progresses to become hot metal 22.
一方、還元１ｔ１３中の脈石と炭材及び生石灰１４とが
反応して、スラグ２３が生成する。このスラグ２３は、
溶融還元炉１０内に貯留し、時間が経過するにつれその
量を増していく。そこで、該スラグ２３を間欠的又は連
続的に炉外に排出する。On the other hand, the gangue in the reduction 1t13, the carbonaceous material, and the quicklime 14 react to generate slag 23. This slag 23 is
It is stored in the melting reduction furnace 10, and its amount increases as time passes. Therefore, the slag 23 is discharged out of the furnace intermittently or continuously.
このような溶融還元法においては、特にその開発過程か
らしても明らかなように、使用可能な原料の範囲の拡大
、熱回収の効率化、溶融還元炉における製錬反応の促進
等を如何にして達成するかが今後の課題である。In this type of smelting reduction method, as is clear from the development process, it is important to expand the range of usable raw materials, improve the efficiency of heat recovery, and promote the smelting reaction in the smelting reduction furnace. The challenge for the future is how to achieve this goal.
しかし、一般炭、粉鉱石等の廉価な原料を使用すると、
処理過程で多量の粉塵が発生する。このため、炉内の通
気性が悪くなって多量のガスを吹き込むことができず、
生産性を上げることが困難となる。そこで、このような
粉鉱石等はブリケット或いはペレット等の塊状化を行い
、粉塵を発生しない原料に加工して使用されている。ま
た、これまでに開発されている溶融還元法においては、
流動層予備還元炉から排出される還元鉱は、必要に応じ
て熱回収した後、単に溶融還元炉に投入しているに過ぎ
ない。このような方式では、効率的な熱回収及び製錬反
応の促進を行うことに限度がある。However, if cheap raw materials such as thermal coal and fine ore are used,
A large amount of dust is generated during the processing process. As a result, the ventilation inside the furnace deteriorates, making it impossible to blow in a large amount of gas.
It becomes difficult to increase productivity. Therefore, such powdered ores are agglomerated into briquettes, pellets, etc., and processed into raw materials that do not generate dust. In addition, in the melting reduction method developed so far,
The reduced ore discharged from the fluidized bed preliminary reduction furnace is merely charged into the smelting reduction furnace after heat recovery as required. In such a system, there are limits to efficient heat recovery and promotion of smelting reactions.
そこで本発明は、溶融還元法により鉄鉱石から溶銑を得
るに際し、賦存量の多い一般炭と現在利用価値の少ない
微粉鉱石を原料として用い、資源の拡大活用及び溶銑コ
ストの低下を図ることを目的とする。Therefore, the present invention aims to expand the utilization of resources and reduce the cost of hot metal by using steam coal, which has a large amount of reserves, and fine ore, which currently has little utility value, as raw materials when obtaining hot metal from iron ore by the smelting reduction method. shall be.
本発明の鉄鉱石予備還元装置は、その目的を達成するた
めに、溶融還元法に使用する予備還元鉱石を製造する設
備において、流動層予備還元炉に外部粒子循環装置を付
設し、この外部粒子循環装置に細粒状の還元鉱を取り出
す排出部を設け、かつ前記流動層予備還元炉の底部に粗
粒状の還元鉱を取り出す排出部を設けてなることを特徴
とする。In order to achieve the object, the iron ore pre-reduction device of the present invention is provided by attaching an external particle circulation device to a fluidized bed pre-reduction furnace in equipment for producing pre-reduced ore used in the smelting reduction method. The present invention is characterized in that the circulating device is provided with a discharge section for taking out fine-grained reduced ore, and the bottom of the fluidized bed preliminary reduction furnace is provided with a discharge section for taking out coarse-grained reduced ore.
すなわち、本発明においては、流動層予熱炉から排出さ
れる排ガスと鉄鉱石５石灰石等の製鉄原料を流動層予備
還元炉に供給するとともに、粉粒状の石炭も併せて装入
し、溶融還元炉で発生したガスあるいは脱炭酸ガス処理
して得られる還元ガスを流動層予備還元炉の下部から吹
き込む。この還元ガスは、炭材を酸素と部分燃焼反応さ
せることにより生成したガスと混合される。そしてこの
ガスは、高温の鉄鉱石を流動状態にして還元し、還元鉱
を生成する。生成された還元鉱は流動層予備還元炉の下
部に設けた排出部から採取される。That is, in the present invention, the exhaust gas discharged from the fluidized bed preheating furnace and ironmaking raw materials such as iron ore and limestone are supplied to the fluidized bed prereduction furnace, and granular coal is also charged, and the smelting and reduction furnace is heated. The gas generated in the process or the reducing gas obtained through decarbonation treatment is blown into the lower part of the fluidized bed pre-reduction furnace. This reducing gas is mixed with gas generated by subjecting the carbonaceous material to a partial combustion reaction with oxygen. This gas then reduces the hot iron ore to a fluidized state, producing reduced ore. The generated reduced ore is collected from the discharge section provided at the bottom of the fluidized bed pre-reduction furnace.
還元ガスの空塔速度を大にして流動粒子とのスリップ速
度を大きくとることにより、還元反応の促進を行い生産
性を向上させることができる。このとき、装入原料粒子
の多くが流動層予備還元炉から還元ガスに同併して飛散
する。この飛散した装入原料粒子を循環供給させるため
、流動層予備還元炉出口に設けたサイクロンで粒子を捕
集して再び流動層予備還元炉内へ循環供給させるような
外部粒子循環装置を付設する。粉鉱石の循環還元により
、還元率の向上と還元性及び還元率コントロール性が向
上する。By increasing the superficial velocity of the reducing gas and increasing the slip rate with the fluidized particles, the reduction reaction can be promoted and productivity can be improved. At this time, many of the charged raw material particles are scattered together with the reducing gas from the fluidized bed pre-reduction furnace. In order to circulate and supply the scattered charging raw material particles, an external particle circulation device is installed that collects the particles with a cyclone installed at the outlet of the fluidized bed pre-reduction furnace and circulates and supplies them again into the fluidized bed pre-reduction furnace. . Circulating reduction of fine ore improves the reduction rate, reducing property, and controllability of the reduction rate.
このようにして、流動層予備還元炉下部の排出部からは
粗粒状の還元鉱を、また外部粒子循環装置からは細粒状
の還元鉱をそれぞれ採取することができる。In this way, coarse-grained reduced ore can be collected from the discharge section at the lower part of the fluidized bed pre-reduction furnace, and fine-grained reduced ore can be collected from the external particle circulation device.
以下、実施例により本発明の特徴を具体的に説明する。 Hereinafter, the features of the present invention will be specifically explained with reference to Examples.
第１図は本発明の基本的構成を示す概略図である。図に
おいて、流動層予備還元炉６には、流動層予熱炉３ （
第４図参照）から送られてきた粉鉱石５石灰石等の原料
２５が切出弁４１を介して装入される。また、この流動
層予備還元炉６内には、粉粒状の石炭７も切出弁４３を
介して併せて装入され、溶融還元炉１０（第４図参照）
で発生したガスあるいは脱炭酸ガス処理して得られる還
元ガス１１が調節弁４５を介して流動層予備還元炉６の
底部から吹き込まれる。この還元ガス１１は、切出弁４
３を介して装入された石炭７を酸素と部分燃焼反応させ
ることにより生成したガスと混合される。この還元ガス
は、高温の鉄鉱石を流動状態にして還元し、還元鉱を生
成する。還元ガスの空塔速度を大にして流動粒子とのス
リップ速度を大きく取ることにより還元反応の促進を行
い生産性を向上させる。FIG. 1 is a schematic diagram showing the basic configuration of the present invention. In the figure, the fluidized bed pre-reduction furnace 6 includes the fluidized bed preheating furnace 3 (
Raw materials 25 such as powdered ore 5 and limestone sent from a source (see FIG. 4) are charged through a cut-off valve 41. In addition, powdered coal 7 is also charged into the fluidized bed pre-reduction furnace 6 via the cut-off valve 43, and the smelting reduction furnace 10 (see FIG. 4)
The gas generated or the reducing gas 11 obtained by decarbonation treatment is blown into the bottom of the fluidized bed pre-reduction furnace 6 via the control valve 45. This reducing gas 11 is supplied to the cut-off valve 4
The coal 7 charged through the coal 3 is mixed with gas generated by a partial combustion reaction with oxygen. This reducing gas reduces the hot iron ore to a fluidized state to produce reduced ore. By increasing the superficial velocity of the reducing gas and increasing the slip velocity with the fluidized particles, the reduction reaction is promoted and productivity is improved.
このとき、装入原料粒子の多くが流動層予備還元炉６か
ら還元ガスに同伴して飛散するため、流動層予備還元炉
６の出口に設けたサイクロン３１で粒子を捕集し、この
粒子をホッパ３２に貯留し、ニューマチックフィーダ３
３を介して流動層予備還元炉６内へ循環供給させる。こ
の粒子の循環供給のための気体として、調節弁４６を介
して流量調節された還元ガス１１を用いる。粉鉱石の循
環還元により還元率の向上と均−還元性及び還元率コン
トロール性が向上する。そして流動層予備還元炉６の下
部の排出部からは粗粒状の還元鉱２６が、またニューマ
チックフィーダ３３からは細粒状の還元鉱２７がそれぞ
れ連続的に採取される。採取する還元鉱２６゜２７の量
は、切出弁４２及び４４の開度を調節することにより適
当な量に加減する。At this time, many of the charged raw material particles are scattered along with the reducing gas from the fluidized bed pre-reduction furnace 6, so the particles are collected by a cyclone 31 installed at the outlet of the fluidized bed pre-reduction furnace 6. Stored in the hopper 32 and pneumatic feeder 3
3 into the fluidized bed pre-reduction furnace 6. The reducing gas 11 whose flow rate is regulated via the regulating valve 46 is used as the gas for circulating and supplying the particles. Circulating reduction of fine ore improves reduction rate, uniformity of reduction, and controllability of reduction rate. Coarse-grained reduced ore 26 and fine-grained reduced ore 27 are continuously collected from the lower discharge part of the fluidized bed pre-reduction furnace 6 and from the pneumatic feeder 33, respectively. The amount of reduced ore 26, 27 to be collected is adjusted to an appropriate amount by adjusting the opening degrees of the cut-out valves 42 and 44.
捕集した粒子を流動層予備還元炉６内に循環供給させる
ためにニューマチックフィーダ３３を用いるのは、次の
ような理由による。すなわち、サイクロン３１．ホッパ
３２及びニューマチックフィーダ３３で構成される循環
系は、サイクロン３１の部分と流動層予備還元炉６の下
部で数百龍水柱以上の圧力差がある。このため、粒子循
環時のガスシールが難しく、さらには循環粒子が高温で
あり、耐熱、耐摩耗性のある切出装置が必要である。こ
のため粉体シールと気体輸送を組合わせたニューマチッ
クフィーダを用いるのである。これによりシール性を向
上することができ、かつ回転機械部がないため、耐熱、
耐摩耗性も良い。The reason why the pneumatic feeder 33 is used to circulate and supply the collected particles into the fluidized bed pre-reduction furnace 6 is as follows. That is, cyclone 31. In the circulation system composed of the hopper 32 and the pneumatic feeder 33, there is a pressure difference of several hundred columns of water or more between the cyclone 31 and the lower part of the fluidized bed pre-reduction furnace 6. For this reason, gas sealing during particle circulation is difficult, and furthermore, the circulating particles are at a high temperature, requiring a heat-resistant and abrasion-resistant cutting device. For this reason, a pneumatic feeder that combines powder sealing and gas transport is used. This improves sealing performance, and since there are no rotating mechanical parts, heat resistance and
It also has good wear resistance.
このように、本発明においては、流動層予備還元炉６か
らの還元鉱２７．２６の排出口を、サイクロン３１．ホ
ッパ３２及びニューマチックフィーダ３３で構成される
粒子循環系と流動層予備還元炉６の下部に設ける０粒子
循環系からは流動層予備還元炉６内の流動層を偏成した
還元鉱の細かな粒子が風ふるい効果によって比較的整粒
化されて得られる。In this way, in the present invention, the discharge port of the reduced ore 27.26 from the fluidized bed pre-reduction furnace 6 is connected to the cyclone 31. A particle circulation system consisting of a hopper 32 and a pneumatic feeder 33 and a zero-particle circulation system provided at the lower part of the fluidized bed pre-reduction furnace 6 are used to collect particles of reduced ore that have been unevenly distributed in the fluidized bed in the fluidized bed pre-reduction furnace 6. The particles are relatively sized due to the wind sieving effect.
したがって、この排出還元鉱２７は気体輸送が可能であ
り、溶融還元炉１０内にはノズル吹き込みが可能である
。一方、流動層予備還元炉６の下部には比較的粒径の粗
い還元鉱が滞留流動しており、この比較的粗い粒子の還
元鉱２６を流動層予備還元炉６の下部に設けた排出口よ
り排出する。これは気体輸送するには大き過ぎるため、
コンベヤ類で機械的に搬送処理される。Therefore, this discharged reduced ore 27 can be transported as a gas, and can be blown into the smelting reduction furnace 10 through a nozzle. On the other hand, reduced ore with relatively coarse particles is accumulated and flowing in the lower part of the fluidized bed pre-reduction furnace 6, and the reduced ore 26 with relatively coarse particles is discharged through an outlet provided at the lower part of the fluidized bed pre-reduction furnace 6. Emit more. This is too large to transport gas, so
Mechanically transported by conveyors.
装入原料の粒度分布が広く、大粒の鉄鉱石が装入される
場合、あるいは流動還元過程で焼結、造粒して大粒化す
るものがある場合、第２図に示すように流動層予備還元
炉６の炉床に設けたガス分散板６ａをすりばち状にして
中央部から粗大粒子を排出させる。また、粗大粒子の鉱
石の還元速度は微粉に比べて非常に遅いため、第３図に
示すように粗大粒子の排出管４７に粒子を一時貯留し、
調節弁４８を介して還元ガス１１を排出管４７の下端か
ら流す。このように構成することにより、排出管４７内
の粗大粒子の還元を促進させると共に、還元ガス１１の
上昇粒で微粉と大粒子の風ふるいを行わせる。When the charged raw material has a wide particle size distribution and large grains of iron ore are charged, or when some iron ore is sintered and granulated to become large grains during the fluidized reduction process, the fluidized bed reserve is used as shown in Figure 2. A gas dispersion plate 6a provided on the hearth of the reduction furnace 6 is shaped like a mortar to discharge coarse particles from the center. In addition, since the reduction rate of coarse particle ore is much slower than that of fine powder, the particles are temporarily stored in the coarse particle discharge pipe 47 as shown in FIG.
The reducing gas 11 is caused to flow from the lower end of the exhaust pipe 47 via the control valve 48 . With this configuration, the reduction of coarse particles in the discharge pipe 47 is promoted, and the rising particles of the reducing gas 11 perform wind sieving of fine particles and large particles.
排出管４７内の粒子は切出弁４２を開くことによりホッ
パ４９内に排出され、さらに切出弁５０を開くことによ
り、還元鉱２６として採取される。The particles in the discharge pipe 47 are discharged into the hopper 49 by opening the cutting valve 42, and are collected as reduced ore 26 by opening the cutting valve 50.
上述したように、本発明においては、流動層予備還元炉
で発生する微粉を捕集して流動層予備還元炉内に循環さ
せる構成とし、還元鉱を流動層予備還元炉とその循環系
とから採取するようにしている。このため、溶融還元法
においても廉価な一般炭及び粉鉱石を使用することが可
能となった。As described above, in the present invention, the fine powder generated in the fluidized bed pre-reduction furnace is collected and circulated within the fluidized bed pre-reduction furnace, and the reduced ore is removed from the fluidized bed pre-reduction furnace and its circulation system. I'm trying to collect it. For this reason, it has become possible to use inexpensive steam coal and fine ore even in the smelting reduction method.
したがって、資源利用拡大が可能となり、かっ溶銑のコ
ストダウンを図ることができる。さらに、高反応率、ガ
ス利用率向上によりコンパクトな還元設備となる。Therefore, it becomes possible to expand the use of resources and reduce the cost of hot metal. Furthermore, the high reaction rate and improved gas utilization rate result in a compact reduction facility.
第１図は本発明の基本的構成を示す概略図、第２図及び
第３図は本発明の他の構成例を示す概略図、第４図は本
発明者等が先に開発した溶融還元法のフローを示す。Fig. 1 is a schematic diagram showing the basic configuration of the present invention, Figs. 2 and 3 are schematic diagrams showing other configuration examples of the present invention, and Fig. 4 is a smelting reduction method developed earlier by the present inventors. Show the flow of law.
Claims (1)
において、 流動層予備還元炉に外部粒子循環装置を付設し、この外
部粒子循環装置に細粒状の還元鉱を取り出す排出部を設
け、かつ前記流動層予備還元炉の底部に粗粒状の還元鉱
を取り出す排出部を設けてなることを特徴とする鉄鉱石
予備還元装置。[Claims] 1. In a facility for producing pre-reduced ore used in the smelting reduction method, an external particle circulation device is attached to the fluidized bed pre-reduction furnace, and fine-grained reduced ore is taken out into the external particle circulation device. An iron ore pre-reduction apparatus, comprising: a discharge section, and a discharge section for taking out coarse-grained reduced ore at the bottom of the fluidized bed pre-reduction furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61071563A JPH0792343B2 (en) | 1986-03-28 | 1986-03-28 | Iron ore preliminary reduction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61071563A JPH0792343B2 (en) | 1986-03-28 | 1986-03-28 | Iron ore preliminary reduction device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62228879A true JPS62228879A (en) | 1987-10-07 |
| JPH0792343B2 JPH0792343B2 (en) | 1995-10-09 |
Family
ID=13464304
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61071563A Expired - Lifetime JPH0792343B2 (en) | 1986-03-28 | 1986-03-28 | Iron ore preliminary reduction device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0792343B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014513661A (en) * | 2011-03-21 | 2014-06-05 | アルケマ フランス | Carbon nanotube production method and apparatus for carrying out the method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6046354A (en) * | 1983-08-23 | 1985-03-13 | Sanpo Shindo Kogyo Kk | Method for processing aluminum bronze in order to obtain superplasticity |
-
1986
- 1986-03-28 JP JP61071563A patent/JPH0792343B2/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6046354A (en) * | 1983-08-23 | 1985-03-13 | Sanpo Shindo Kogyo Kk | Method for processing aluminum bronze in order to obtain superplasticity |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014513661A (en) * | 2011-03-21 | 2014-06-05 | アルケマ フランス | Carbon nanotube production method and apparatus for carrying out the method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0792343B2 (en) | 1995-10-09 |
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