JPH0359966B2 - - Google Patents
Info
- Publication number
- JPH0359966B2 JPH0359966B2 JP61262309A JP26230986A JPH0359966B2 JP H0359966 B2 JPH0359966 B2 JP H0359966B2 JP 61262309 A JP61262309 A JP 61262309A JP 26230986 A JP26230986 A JP 26230986A JP H0359966 B2 JPH0359966 B2 JP H0359966B2
- Authority
- JP
- Japan
- Prior art keywords
- tuyere
- furnace
- amount
- ore
- cooling water
- 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.)
- Expired - Lifetime
Links
- 239000000498 cooling water Substances 0.000 claims description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 20
- 229910052760 oxygen Inorganic materials 0.000 claims description 20
- 239000001301 oxygen Substances 0.000 claims description 20
- 238000000034 method Methods 0.000 claims description 19
- 229910044991 metal oxide Inorganic materials 0.000 claims description 18
- 150000004706 metal oxides Chemical class 0.000 claims description 18
- 239000002184 metal Substances 0.000 claims description 17
- 229910052751 metal Inorganic materials 0.000 claims description 17
- 230000009467 reduction Effects 0.000 claims description 17
- 238000003723 Smelting Methods 0.000 claims description 10
- 239000012255 powdered metal Substances 0.000 claims description 5
- 238000007664 blowing Methods 0.000 claims description 3
- 238000006722 reduction reaction Methods 0.000 description 17
- 239000002893 slag Substances 0.000 description 16
- 239000000571 coke Substances 0.000 description 10
- 238000002485 combustion reaction Methods 0.000 description 10
- 229910004298 SiO 2 Inorganic materials 0.000 description 8
- 238000002347 injection Methods 0.000 description 8
- 239000007924 injection Substances 0.000 description 8
- 238000002844 melting Methods 0.000 description 6
- 230000008018 melting Effects 0.000 description 6
- 239000003575 carbonaceous material Substances 0.000 description 5
- 239000000843 powder Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000009529 body temperature measurement Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 238000005303 weighing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- -1 fine ore Chemical class 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B7/00—Blast furnaces
- C21B7/24—Test rods or other checking devices
-
- 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
- C21B13/0026—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide in the flame of a burner or a hot gas stream
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
- C21B13/029—Introducing coolant gas in the shaft furnaces
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture Of Iron (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、粉状の金属酸化物を使用する溶融還
元炉の操業方法に関するもので、特に吹込量変更
時における炉内の熱レベルを適正化して操業の安
定を図るものである。[Detailed Description of the Invention] [Field of Industrial Application] The present invention relates to a method for operating a smelting reduction furnace that uses powdered metal oxides, and in particular, a method for controlling the heat level in the furnace when changing the injection amount. The aim is to stabilize operations by
通常、地下資源としての鉄鉱石などの金属酸化
物の形態としては塊状のものが少なく粉状のもの
が大半を占めており、将来、益々、粉状鉱石が増
えることが予想されることから、原料鉱石を直接
粉状のままで使用することは、昇エネルギー、製
造コストの面で有利となる。
Normally, the form of metal oxides such as iron ore as underground resources is mostly in the form of powder, with few lumps, and it is expected that the number of powdered ores will increase in the future. Using the raw material ore directly in powder form is advantageous in terms of increased energy consumption and production costs.
しかしながら、従来より、鉄鉱石など金属酸化
物還元プロセスとしては高炉還元法が主流となつ
ている。既知の如く高炉は気体と固体の向流反応
炉であるために、粉状鉱石を直接炉内へ装入した
場合、充填層内の通気性が著しく阻害され、操業
維持が非常に困難である。 However, conventionally, the blast furnace reduction method has been the mainstream method for reducing metal oxides such as iron ore. As is known, a blast furnace is a countercurrent reaction furnace for gas and solids, so if powdered ore is charged directly into the furnace, the permeability in the packed bed will be significantly inhibited, making it extremely difficult to maintain operation. .
その対策として、従来、粉状鉱石に熱源として
コークス等の炭材を添加し焼結プロセスで焼成せ
しめて粉鉱石を塊成化し、これを高炉装入物とし
て使用している。この塊成化コストの大部分は
NOx，SOxの脱硝、脱硫コスト、ハンドリング
および炭材コストであり、昇エネルギーの面で不
利である。また、焼結炉の排ガス中のNOxや
SOxの除去のために多くの費用が必要となる。そ
こで粉状鉱石を直接使用できる溶融還元製鉄法が
将来、製造コスト、立地条件などの面で有利とな
る。 As a countermeasure, conventionally, carbonaceous materials such as coke are added to powdered ore as a heat source and the powdered ore is fired in a sintering process to agglomerate the powdered ore, which is then used as blast furnace charge. Most of this agglomeration cost is
This is disadvantageous in terms of raising energy due to the cost of denitrification and desulfurization of NOx and SOx, handling and carbon material costs. In addition, NOx in the exhaust gas of the sintering furnace
A lot of money is required to remove SOx. Therefore, in the future, the smelting reduction method, which allows the direct use of powdered ore, will be advantageous in terms of production costs and location conditions.
溶融還元法は大別すると、鍋状容器内の溶融金
属に粒鉱石を投入しながら炭材と酸素を吹き込み
加熱し、溶融還元する転炉タイプと、シヤフト炉
に炭材を充填しておき、羽口から連続的に粉鉱石
を吹き込み、炭材を燃焼で溶融還元する竪型炉タ
イプとに分けられる。 The smelting reduction method can be roughly divided into the converter type, in which granular ore is poured into molten metal in a pot-shaped container, while carbonaceous material and oxygen are blown into it, heated, and melted down; It can be divided into a vertical furnace type, in which fine ore is continuously blown into the tuyere and the carbonaceous material is melted and reduced by combustion.
本出願人は後者の方法の１つとして、特公昭59
−18452を提案した。それによれば炉下部に設置
された高温空気を吹き込む上下２段の羽口のうち
少なくとも上段の羽口から粉粒状鉱石を高温空気
とともに竪型炉内に吹き込み、これを溶融還元す
ることを特徴としている。800〜900℃前後に加熱
した空気中に必要により酸素を混合して羽口より
送風し、炉内の炭材を燃焼して熱を発生するが、
炉内の熱レベル制御は操業の安定上重要である。
炉内の熱レベルは羽口覗き窓からの燃焼状態の監
視や、排出されるメタル、スラグの状態および成
分から経験的に判断されるが、粉粒体を吹き込む
場合には羽口の目視観察は難しく、一方スラグ、
メタルからの判断では数時間の遅れがあるため、
熱レベルの制御には不十分であつた。 As one of the latter methods, the applicant proposed
−18452 was proposed. According to this, granular ore is blown into the vertical furnace together with high-temperature air from at least the upper tuyere of two upper and lower tuyeres installed in the lower part of the furnace to blow high-temperature air into, and is characterized by melting and reducing the ore. There is. The air heated to around 800-900℃ is mixed with oxygen if necessary and blown through the tuyere, and the carbonaceous material in the furnace is burned to generate heat.
Heat level control inside the furnace is important for stable operation.
The heat level inside the furnace is determined empirically by monitoring the combustion status through the tuyere viewing window and by checking the condition and composition of the discharged metal and slag, but when injecting powder and granules, visual observation of the tuyere is necessary. is difficult, while slag,
According to Metal's judgment, there will be a delay of several hours, so
Control of heat levels was inadequate.
また、高炉操業においては羽口先の燃焼状態を
輝度計を用いて測定する方法もあるが、炉内の熱
レベルを定量的に測定し、制御するには不十分で
あつた。 Additionally, in blast furnace operation, there is a method of measuring the combustion state at the tip of the tuyere using a luminance meter, but this method is insufficient to quantitatively measure and control the heat level inside the furnace.
一般に粉鉱石などの金属酸化物を羽口から吹き
込む還元炉の場合、単位時間当りの吹込量に対す
る投入熱量はコークスを燃焼しうる空気量および
酸素量で決定される。 In general, in the case of a reduction furnace in which metal oxides such as fine ore are blown into the furnace through the tuyere, the amount of heat input relative to the amount of injection per unit time is determined by the amount of air and oxygen that can burn the coke.
炉内の、特に羽口先の熱レベルは炉内における
還元反応ならびにメタルスラグ成分に著しく影響
し、炉況を左右する。 The heat level inside the furnace, especially at the tip of the tuyere, significantly affects the reduction reaction inside the furnace and the metal slag components, and influences the furnace condition.
そのため、操業者は羽口の覗き窓からの燃焼状
態監視や炉から排出されるスラグの色彩度合、粘
性状態さらにはメタル中の［Si］およびスラグの
CaO／SiO2（塩基度）から炉内の熱レベルを判断
し、金属酸化物量や送風空気中に富化する酸素比
率を変更して適正な熱レベルに調整している。し
かし燃焼状態、スラグの色彩、粘性などの判断は
経験的なもので個人差があり、また、スラグ、メ
タル成分の検出は周知のとおり、数時間の遅れを
生じており、これによつて現時点の炉内における
熱レベルを推定することは難しい。 Therefore, operators must monitor the combustion status through the tuyere viewing window, monitor the color and viscosity of the slag discharged from the furnace, and monitor the [Si] and slag conditions in the metal.
The heat level inside the furnace is determined from CaO/SiO 2 (basicity), and the appropriate heat level is adjusted by changing the amount of metal oxides and the ratio of oxygen enriched in the blown air. However, judgments on combustion conditions, slag color, viscosity, etc. are based on experience and vary from person to person, and as is well known, there is a delay of several hours in detecting slag and metal components. It is difficult to estimate the heat level inside a furnace.
〔発明が解決しようとする問題点〕
金属酸化物たとえば、粉鉱石を送風羽口より吹
き込む形式をとる溶融還元炉の場合、炉内の熱的
レベルは羽口から吹き込む金属酸化物量または送
風中の酸素割合で調整している。[Problems to be solved by the invention] In the case of a smelting reduction furnace in which metal oxides, such as fine ore, are blown into the tuyere, the thermal level inside the furnace depends on the amount of metal oxide blown in through the tuyere or the amount of air being blown into the furnace. Adjusted by oxygen percentage.
本発明は炉熱レベルの変動を表示するオンライ
ン因子によつて、これらを制御し安定な操業をす
ることができる方法を提供することを目的とす
る。 It is an object of the present invention to provide a method that can control fluctuations in the furnace heat level using on-line factors that display fluctuations in the furnace heat level to achieve stable operation.
送風羽口を溶損から防止するため、常時、羽口
内部を冷却水で冷却しているが、本発明者らは酸
素割合や粉鉱石の吹込量を変更すると、冷却水の
排水温度は炉内の燃焼状態や熱的レベルにより敏
感に変化することを見出した。すなわち、羽口冷
却水の入口、出口の温度差の変化量を検知し、そ
の検出値に応じて金属酸化物の吹込や酸素割合を
変更した場合の炉内における燃焼状態および熱的
レベルをきめ細かに管理することによつて、操業
の安定化を図ることができることがわかつた。 In order to prevent the blast tuyere from being damaged by erosion, the inside of the tuyere is always cooled with cooling water, but the inventors found that by changing the oxygen ratio and the amount of fine ore injected, the cooling water drainage temperature decreased We found that it changes sensitively depending on the internal combustion state and thermal level. In other words, the amount of change in the temperature difference between the inlet and outlet of the tuyere cooling water is detected, and the combustion state and thermal level in the furnace are determined in detail when the metal oxide injection and oxygen ratio are changed according to the detected value. It was found that stable management of operations can be achieved by managing the conditions.
本発明は羽口冷却水の羽口入口および出口の温
度差を検知し、粉粒体吹込量および／または送風
空気中に添加する酸素量を制御し、炉内、特に羽
口先の熱レベルを管理することにより、メタル、
スラグ成分の変動を抑制し、操業の安定を図ろう
とするものである。 The present invention detects the temperature difference between the tuyere inlet and outlet of the tuyere cooling water, controls the amount of granular material injected and/or the amount of oxygen added to the blown air, and controls the heat level inside the furnace, especially at the tip of the tuyere. By managing metal,
The aim is to suppress fluctuations in slag components and stabilize operations.
すなわち本発明は竪型炉の羽口から粉状金属酸
化物を送風空気とともに炉内に吹き込んで溶融金
属を還元する方法において、該羽口冷却水の羽口
入口および出口の温度差を測定し、その変動に応
じて粉状金属酸化物の吹込量および／または送風
空気中の酸素添加量を制御することを特徴とする
溶融還元炉の操業方法である。
That is, the present invention measures the temperature difference between the tuyere inlet and outlet of the tuyere cooling water in a method for reducing molten metal by blowing powdered metal oxide into the furnace together with blast air from the tuyere of a vertical furnace. A method of operating a smelting reduction furnace is characterized in that the amount of blown metal oxide powder and/or the amount of oxygen added to blown air is controlled in accordance with fluctuations thereof.
メタル中の［Si］、スラグ中のSiO2を例にとる
と、SiO2から［Si］への還元は主としてＣが還
元剤となつて［Si］まで還元される。この場合、
SiO2とＣの親和力、すなわちSiO2から［Si］ま
で還元される度合は、炉内温度に最も左右され
る。このことからメタル中の［Si］の変動によつ
て高炉の熱レベルを判定している。
Taking [Si] in metal and SiO 2 in slag as an example, the reduction of SiO 2 to [Si] mainly uses C as a reducing agent and is reduced to [Si]. in this case,
The affinity between SiO 2 and C, that is, the degree of reduction of SiO 2 to [Si], is most influenced by the temperature inside the furnace. From this, the heat level of the blast furnace is determined by the fluctuation of [Si] in the metal.
また、スラグ中のSiO2の量は、還元された
［Si］がメタルに溶解するか、また還元されずに
SiO2のままでスラグ中に入るかで異つてくる。
メタル中［Si］の増加はスラグの塩基度（CaO
％）／（SiO2％）の減少につながる。塩基度の
増減はスラグの融点、粘性に影響を及ぼすので操
業の安定にも密接に関係する。それゆえ、炉内の
熱レベルを制約することは、メタル、スラグ成分
の変動を抑制でき操業の安定につながる。 In addition, the amount of SiO 2 in the slag depends on whether the reduced [Si] is dissolved in the metal or not reduced.
It depends on whether SiO 2 enters the slag as it is.
The increase in [Si] in the metal is due to the basicity of the slag (CaO
%)/(SiO 2 %). Increases and decreases in basicity affect the melting point and viscosity of slag, and are closely related to operational stability. Therefore, restricting the heat level in the furnace can suppress fluctuations in metal and slag components, leading to stable operation.
竪型炉タイプの溶融還元炉では通常の高炉と同
様に1000℃前後に加熱された空気が羽口を通じて
炉内に送られ、コークスと反応して燃焼するが、
その燃焼温度は高温となり、金属製の羽口は冷却
しないと溶損する。その対策として羽口の材質は
熱伝導性の良い銅を用いてその内部を冷却水を流
し、羽口の熱を抜熱することにより溶損を防止し
ている。 In a vertical furnace type smelting reduction furnace, air heated to around 1000℃ is sent into the furnace through the tuyeres, reacting with coke and burning it, just like in a normal blast furnace.
The combustion temperature is so high that the metal tuyeres will melt if not cooled. As a countermeasure, the tuyeres are made of copper, which has good thermal conductivity, and cooling water is run through the tuyere to remove heat from the tuyere, thereby preventing melting and damage.
羽口の熱を吸収した冷却水は温度が上昇するた
めに、冷却塔で冷却した後、再び羽口に循環さ
れ、羽口を冷却する。この冷却水は、酸素混合量
や羽口から吹き込む金属酸化物の量により羽口先
での燃焼状態ならびに羽口が受ける熱量が変化す
るので、それらの影響を受け、温度が敏感に上下
する。第１図に鉱石吹込量と富化酸素量変更時の
羽口冷却水の温度差の変化を示した。 The temperature of the cooling water that absorbs heat from the tuyeres rises, so after being cooled in the cooling tower, it is circulated back to the tuyere to cool the tuyere. The temperature of this cooling water sensitively fluctuates as the combustion state at the tip of the tuyere and the amount of heat received by the tuyere change depending on the amount of oxygen mixed and the amount of metal oxide blown in from the tuyere. Figure 1 shows the change in the temperature difference of the tuyere cooling water when the amount of ore injection and the amount of enriched oxygen are changed.
第１図に示す如く、金属酸化物吹込量の増加は
同じ富化酸素量では冷却水温度差を低下させる方
向に、また富化酸素量の増加は冷却水温度差を上
昇させる方向に作用す。従つて、２段羽口の上段
と下段で冷却水の温度差を別々に測定し、これを
利用することにより、粉体吹込や酸素量が羽口先
の熱レベルに及ぼす影響を安定的に把握すること
ができ、これを制御因子として用いることができ
る。 As shown in Figure 1, an increase in the amount of metal oxide blown in will act in the direction of lowering the cooling water temperature difference for the same amount of enriched oxygen, and an increase in the amount of enriched oxygen will act in the direction of increasing the cooling water temperature difference. . Therefore, by measuring the temperature difference of the cooling water separately in the upper and lower stages of the two-stage tuyere and using this, it is possible to stably understand the effects of powder injection and oxygen content on the heat level at the tip of the tuyere. can be used as a control factor.
第２図に溶融還元法のプロセスフローの実施例
を示す。
FIG. 2 shows an example of the process flow of the smelting reduction method.
原料ホツパ１〜３には、粉状の金属酸化物およ
び溶剤が収納され、所定の配合で同時に切り出さ
れて混合鉱石としてベルトコンベア５で重量計量
ホツパ６に装入され、ベルトコンベア７で鉱石用
バンカ１１に入り、鉱石用均排圧ホツパ１２を経
由して、金属酸化物ホツパ１３へ装入される。 Powdered metal oxide and solvent are stored in the raw material hoppers 1 to 3, and are simultaneously cut out in a predetermined proportion and charged as mixed ore by a belt conveyor 5 into a weighing hopper 6, and then by a belt conveyor 7 for ore use. It enters a bunker 11, passes through a pressure equalization hopper 12 for ore, and is charged into a metal oxide hopper 13.
コークスはコークス原料ホツパ４より単独に切
り出されベルトコンベア５で重量計量ホツパ６へ
運ばれベルトコンベア７でコークス用バンカ８に
装入され、コークス均圧ホツパ９、コークスホツ
パ１０を経由して、溶融還元炉１４に装入され
る。 Coke is individually cut out from the coke raw material hopper 4, conveyed to the weighing hopper 6 by the belt conveyor 5, charged into the coke bunker 8 by the belt conveyor 7, passed through the coke equalization hopper 9 and the coke hopper 10, and then melted and reduced. It is charged into the furnace 14.
次に金属酸化物に溶剤を加えた混合鉱石は鉱石
用ホツパ１３から鉱石供給量調節フイーダ１５、
吹込用パイプ１６を経て羽口１９より溶融還元炉
１４内へ吹き込まれる。 Next, the mixed ore containing the metal oxide and the solvent is transferred from the ore hopper 13 to the ore supply amount adjustment feeder 15,
It is blown into the melting reduction furnace 14 through the tuyere 19 through the blowing pipe 16 .
また、送風空気は送風ブロワ１７より熱交換器
１８に送られ、800〜900℃前後に加熱され、羽口
１９より熱風として炉１４内へ送風される。この
空気は同時に鉱石吹込パイプ１６から羽口１９を
通して吹き込まれる混合鉱石を溶融還元炉１４内
に搬送し、コークスの燃焼熱とその際発生する還
元ガスおよびカーボンとの接触によつて、溶融還
元せしめる。溶融メタルは出銑口２０より排出さ
れ、スラグは出滓口２１より排出される。 Further, the blown air is sent from the blower 17 to the heat exchanger 18, heated to around 800 to 900°C, and blown into the furnace 14 from the tuyere 19 as hot air. This air simultaneously conveys the mixed ore injected from the ore injection pipe 16 through the tuyere 19 into the melting reduction furnace 14, where it is melted and reduced by the combustion heat of the coke and contact with the reducing gas and carbon generated at the time. . Molten metal is discharged from the tap hole 20, and slag is discharged from the slag hole 21.
次に羽口の冷却水は羽口冷却水ライン２２を循
環し、クーリングタワー２２ａで空冷された後、
昇圧ポンプ２３で羽口に送られ、羽口の熱を抜熱
した後、クーリングタワー２２ａへ戻され再び空
冷される。そこで循環する冷却水の羽口への入口
側と羽口からの排水側にそれぞれ冷却水温度を検
知するセンサ２４，２５を取り付ける。刻々変化
する羽口冷却水の出入の温度２４，２５の温度差
は演算装置２６によつて演算され、酸素流量制御
弁２７を制御する。 Next, the tuyere cooling water circulates through the tuyere cooling water line 22, and after being air-cooled in the cooling tower 22a,
After being sent to the tuyere by the boost pump 23 and removing the heat from the tuyere, it is returned to the cooling tower 22a and air-cooled again. Therefore, sensors 24 and 25 for detecting the temperature of the cooling water are attached to the inlet side of the circulating cooling water to the tuyere and the drainage side from the tuyere, respectively. The temperature difference between the inlet and outlet temperatures 24 and 25 of the tuyere cooling water, which changes every moment, is calculated by a calculation device 26, and the oxygen flow control valve 27 is controlled.
羽口冷却水の温度差を検出し、鉱石供給量調節
フイーダ１５により鉱石供給量を制御し、酸素流
量制御弁２７により羽口送風への混入酸素量を調
節することにより、炉内、特に羽口先の熱レベル
を調節することができる。 By detecting the temperature difference in the tuyere cooling water, controlling the ore supply amount using the ore supply amount adjustment feeder 15, and adjusting the amount of oxygen mixed into the tuyere ventilation using the oxygen flow rate control valve 27, You can adjust the heat level of your mouth.
実施例として次の仕様の溶融還元炉を用いて下
記の範囲で試験操業を行つた。 As an example, a test operation was conducted in the following range using a melting reduction furnace with the following specifications.
炉内径：1.2ｍ
羽口：上段、下段各３本
送風量：1600Nm2／Ｈ
送風温度：850℃
鉱石配合比：処理鉱石66％、石灰石27％珪石
７％
鉱石吹込量：600〜800Kg／Ｈ
富化O2：50〜150Nm3／Ｈ
冷却水量：60ton／Ｈ
熱レベル制御の実施例として
富化O2：120Nm3／Ｈ
粉鉱石吹込量800Kg／Ｈ
の条件で操業を行つていた場合に、羽口温度が３
℃低下したので、熱レベルを回復させたために、
富化O2流量を120Nm3／Ｈから130Nm3／Ｈに増加
した。また、別の操業では20℃低下したので粉鉱
石吹込量を800Kg／Ｈを750Kg／Ｈに調整して熱レ
ベルを制御した。 Furnace inner diameter: 1.2m Tuyeres: 3 each for upper and lower tiers Air flow rate: 1600Nm 2 /H Airflow temperature: 850℃ Ore composition ratio: Processed ore 66%, limestone 27%, silica stone 7% Ore injection amount: 600-800Kg/H Enriched O 2 : 50-150Nm 3 /H Cooling water amount: 60ton/H As an example of heat level control Enriched O 2 : 120Nm 3 /H When operating under the conditions of fine ore injection amount 800Kg/H , the tuyere temperature is 3
As the temperature decreased, the heat level recovered.
The enriched O 2 flow rate was increased from 120 Nm 3 /H to 130 Nm 3 /H. In another operation, the temperature dropped by 20°C, so the amount of fine ore injected was adjusted from 800 kg/h to 750 kg/h to control the heat level.
本発明方法によればメタル中［Si］％変動値は
標準偏差で0.041重量％で従来法での0.089重量％
と比較して、変動が小さかつた。そして本発明で
従来より安定した操業が行えるようになつた。 According to the method of the present invention, the standard deviation of the fluctuation value of [Si]% in metal is 0.041% by weight compared to 0.089% by weight using the conventional method.
The fluctuations were small compared to The present invention has made it possible to operate more stably than before.
本発明方法により竪型還元炉のオンライン操炉
因子によつて操炉することが可能となつたので、
従来の熟練者の勘による操業を軽減することが可
能となつた。
The method of the present invention makes it possible to operate the vertical reduction furnace using online operation factors.
It has now become possible to reduce the amount of operations that previously required the intuition of experts.
第１図は金属酸化物と溶剤の混合鉱石吹込量と
富化酸素量に対する羽口冷却水排水温度の変化を
すグラフ、第２図は本発明を示す溶融還元プロセ
スフローシートである。
１，２，３，４…原料ホツパ、５…ベルトコン
ベア、６…原料計量ホツパ、７…正転、逆転可能
なベルトコンベア、８…コークス用バンカ、１４
…溶融還元炉、１５…鉱石供給量調節フイーダ、
１９…羽口、２２…羽口冷却水ライン、２３…冷
却水循環ポンプ、２４…冷却水入口温度測定セン
サ、２５…冷却水出口温度測定センサ、２６…冷
却水の出入温度差の演算装置、２７…酸素流量制
御弁。
FIG. 1 is a graph showing changes in tuyere cooling water drainage temperature with respect to the amount of mixed ore injected with metal oxide and solvent and the amount of enriched oxygen, and FIG. 2 is a flow sheet of the smelting reduction process showing the present invention. 1, 2, 3, 4... Raw material hopper, 5... Belt conveyor, 6... Raw material measuring hopper, 7... Belt conveyor capable of forward and reverse rotation, 8... Bunker for coke, 14
... Smelting reduction furnace, 15... Ore supply amount adjustment feeder,
19...Tuyere, 22...Tuyere cooling water line, 23...Cooling water circulation pump, 24...Cooling water inlet temperature measurement sensor, 25...Cooling water outlet temperature measurement sensor, 26...Calculating device for cooling water inlet/outlet temperature difference, 27 ...Oxygen flow control valve.
Claims (1)
とともに炉内に吹き込んで溶融金属を還元する方
法において、該羽口冷却水の羽口入口および出口
の温度差を測定し、その変動に応じて粉状金属酸
化物の吹込量および／または送風空気中の酸素添
加量を制御することを特徴とする溶融還元炉の操
業方法。1. In a method of reducing molten metal by blowing powdered metal oxide into the furnace together with air from the tuyere of a vertical furnace, the temperature difference between the tuyere inlet and outlet of the tuyere cooling water is measured, and its fluctuations are measured. 1. A method for operating a smelting reduction furnace, which comprises controlling the amount of powdered metal oxide blown into the air and/or the amount of oxygen added to the blown air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61262309A JPS63114911A (en) | 1986-11-04 | 1986-11-04 | Method for operation smelting/reducing furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61262309A JPS63114911A (en) | 1986-11-04 | 1986-11-04 | Method for operation smelting/reducing furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63114911A JPS63114911A (en) | 1988-05-19 |
| JPH0359966B2 true JPH0359966B2 (en) | 1991-09-12 |
Family
ID=17373992
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61262309A Granted JPS63114911A (en) | 1986-11-04 | 1986-11-04 | Method for operation smelting/reducing furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63114911A (en) |
-
1986
- 1986-11-04 JP JP61262309A patent/JPS63114911A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS63114911A (en) | 1988-05-19 |
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