JPS6133042B2 - - Google Patents
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- Publication number
- JPS6133042B2 JPS6133042B2 JP5097182A JP5097182A JPS6133042B2 JP S6133042 B2 JPS6133042 B2 JP S6133042B2 JP 5097182 A JP5097182 A JP 5097182A JP 5097182 A JP5097182 A JP 5097182A JP S6133042 B2 JPS6133042 B2 JP S6133042B2
- Authority
- JP
- Japan
- Prior art keywords
- hot metal
- reaction
- tank
- reaction tank
- slag
- 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
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C1/00—Refining of pig-iron; Cast iron
- C21C1/02—Dephosphorising or desulfurising
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Refinement Of Pig-Iron, Manufacture Of Cast Iron, And Steel Manufacture Other Than In Revolving Furnaces (AREA)
Description
本発明は竪型連続溶銑予備処理装置に関するも
のである。
溶銑の不純物であるSi、Ｐ、Ｓを連続的に除去
する方法として、従来から横型−樋式連続処理と
竪型連続処理が知られている。
ところで予備処理反応である脱Si、脱Ｐ、Ｓは
The present invention relates to a vertical continuous hot metal pretreatment apparatus. As methods for continuously removing impurities such as Si, P, and S from hot metal, horizontal-type continuous processing and vertical continuous processing have been known. By the way, the pretreatment reactions, such as deSi, deP, and S, are
【表】
であり、これらはスラグ−メタル反応であるの
で、効率よい脱Si、Ｐ、Ｓを実施するには、充分
なスラグ−メタル反応接触面積を確保する事が必
要である。
しかしながらこれを横型樋式の連続処理法で確
保するには次の様な反応装置上の問題がある。
(1) スラグ−メタル接触面は、一義的には装置の
横断面によつて定まつてくる。この面積を大き
くしようとすれば、勢い精錬装置を大きくせざ
るを得ない。一般的に設備の大型化は設備費の
経済性、耐火物消費量、熱損失の点から好まし
くなく実用的でない。
(2) スラグ−メタル接触面積を拡大させる方法と
しては、溶銑、スラグを撹拌する方法が考えら
れる。しかし強い撹拌は樋内の先行溶銑、後続
溶銑の混合を来たし、連続処理の特徴が失われ
るとともに処理が困難となる。
(1)、(2)の問題点を有することから、溶銑の連続
処理は理論的に又実験的には可能であるが、実用
化には至つていないのが現状である。
一方例えば特開昭49−70812号公報において、
竪型炉による溶銑のスプレー精錬方式が提案さ
れ、竪型炉落下の溶融鉄滴をスラグ形成物質の酸
化ガスにより精錬する方法が開示されている。又
特公昭47−48767号公報は、竪型連続脱硫装置が
提案されている。
本発明は上述の従来技術とは全く異なる竪型連
続式の溶銑の予備処理装置を提起するものであ
る。
以下本発明を図面により説明する。
第１図は本発明の反応槽の模式図である。図に
おいて、反応槽２０には容器２１を設け、溶銑Ｐ
が準備される。容器２１はノズル２５が所望数設
けられて、反応槽２０に開口している。反応槽２
０の下部には、排出ノズル２６を設けた溶銑湯溜
槽２７がある。２２は精錬剤添加ノズルを示し、
ノズル２２−１が反応槽２０の下部に設けられ、
ノズル２２−２，２２−３が反応槽の胴部に設け
られる。２３は排出口で反応終了スラグが取り出
される。湯溜槽２７に補助ノズル２２−４を設け
て、精錬反応剤を添加してもよい。３５はガス抜
き孔である。
まず溶銑収納容器から溶銑が、ノズル又はスリ
ツト状耐火物を介して、細線状あるいは粒滴状、
フイルム状の形態とし、反応面積を増大させて、
反応槽上部に供給される。溶銑は溶鋼と異なり、
溶銑温度と凝固温度の差ΔＴが大きい点と、粘性
の点から極めて小さい横断面として流出する事が
容易であり、数10μにする事も可能である。
本発明における反応槽には、目的に応じた精錬
剤、即ち脱Si反応剤が槽上部に脱Ｐ、Ｓ反応剤が
槽下部に溶融状態に保持されている。
前記液状反応剤の中を、溶銑は上方から下方へ
降下して行き、その降下中にスラグ−メタル反応
を起こし、脱Si次いで脱Ｐ、Ｓが実施される。反
応槽へは溶銑を連続的に供給するので、槽内のス
ラグを新しいものと交換する必要があり、各反応
域の下方から新しい精錬剤を供給するとともに、
反応槽上部より反応終了スラグを排出する。
本発明では反応槽の中間部に精錬剤の供給孔を
設けてあり、酸素、酸化鉄等の脱Si剤を供給する
事によつて、脱Si反応槽下部から脱Ｐ、Ｓ剤を供
給することによつて、脱Ｐ、Ｓと夫々の反応効率
を向上させる事が出来る。
最後に反応槽を通過した溶銑は、最下部の溶銑
溜部にたくわえられ、必要に応じて排出される。
本発明装置においては、スラグ−メタルが向流
反応を行うものであり、反応槽に供給される溶銑
は、線状、粒滴もしくはフイルム状に形成する。
この場合線状、粒滴、フイルム状の溶銑は、液状
精錬剤と接触する表面積として、0.5cm2〜10cm2／
１ｇ−溶銑が好ましい。
10cm2/ｇ超であると、連続排出する液状スラグ
とともに溶銑が排出される恐れがあり、本発明装
置による効果が達成されないし、0.5cm2/ｇ未満に
なると、向流反応が十分に期待できない。
線状、フイルム状化はノズル、スリツト状耐火
物の形状を工夫する事によつて、容易に実施出来
る。又粒滴状化は上記ノズル下部に磁気ストツパ
ーを設置するか振動をあたえることによつて、容
易に実行出来るものである。
又本発明における反応槽への精錬剤の供給は、
脱Si、脱Ｐ、Ｓに応じて各々異なるフラツクスを
添加されるが、何れも反応槽内ではほぼ完全に溶
融状態になつていなければならない。その為あら
かじめ溶解した精錬剤を反応槽内に添加する事も
でき、また熱的観点から反応槽の一個所又は複数
個所の側壁面から、又は溶銑溜部へ直接添加する
方が好ましい。
溶銑の予備処理は、大別して二つに分けられ
る。即ちSi、Mn、Cr、Zr等の割合酸素との親和
力のある元素を酸化除去する場合には、酸素ガス
及び酸化鉄（スケール、鉄鉱石粉、焼結鉱粉等）
を主として添加するが、酸化反応を調整する意味
から、一部CaO粉等の添加により、反応槽の塩基
度を調整する事もある。
次にＰ、Ｓを除去する場合は、積極性にＰ、Ｓ
と結合する物質を添加する必要があり、CaO系と
ソーダ系に大別出来る。但し脱Ｐ反応について
は、CaO系、ソーダ系をとわず、反応槽での溶銑
のSi含有量が0.2％以上では、脱Ｐがほとんど起
こらないので、0.2％まで低減させておく必要が
ある。
又CaO系を使用する場合は、CaOの溶解を促進
すると言う点から、CaCl2、CaF2等の適量の使用
は効果がある。又CaO系、ソーダ系をとわず脱
Ｐ、又は同時脱Ｐ、Ｓ反応での脱Ｐの酸化を強化
するため、酸素ガス、酸化鉄を併せて添加する事
は有効である。
本発明の反応槽の側壁部は耐火物でもよいが、
竪型槽の特長を生かすには、降下溶銑のある乱流
域部だけ広めに側壁を大きくして、反応槽を冷却
構造とするが、熱回収機構を持たせた構造とし
て、反応槽内側に精錬剤のセルフコーデング層を
生成させることもできる。
この場合従来冶金装置が、常に耐火物問題の解
決に多くの労力を費して来た事から考えると、こ
の問題から解放される事は明白である。又、竪型
反応に回転運動をあたえることによつて、液状ス
ラグの流動を活発化し、溶銑との反応効率を向上
する事も可能である。
特に反応槽の長さの問題については、上方から
供給される溶銑の単位重量当りの表面積（cm2/g
ｒ）がいくらであるかと言う事と、反応槽で不純
物をどの程度まで除去するかと言う事によつて決
まつて来るが、たとえば一般的な溶銑（Si0.5〜
0.8％、P0.08〜0.15％、S0.2〜0.04％）のもの
を、脱Si槽でSi0.05〜0.2％までSiを除去したり、
又は脱Ｐ、Ｓ槽でP0.01〜0.02％、S0.01〜0.015
％で除去する場合は、供給溶銑径を数m/mにす
れば、数メートル〜10メートル前後で充分であ
る。
又冶金反応は除去すべき元素によつて異なる
が、温度の影響を受けやすいものであるから、反
応槽外側に誘導加熱装置を配置する事によつて、
自由に槽内温度の制御を可能にする。又、誘導撹
拌する事によつて、冶金反応を促進出来る事は当
然である。
第２図、第３図は本発明の他の実施例である。
（第１図と同一符号は同一名称につき説明を省略
した。）
第２図は脱Si槽２０−１と脱Ｐ、Ｓ槽２０−２
に分離して反応槽２０を構成し、槽２０−２の外
周に誘導コイル３０を設ける。槽２０−１と槽２
０−２との間に容器３１を設けて、脱Si溶銑を貯
めることができる。精錬剤は脱Si用として酸化
鉄、酸素ガスがArガスとともにノズル２２−２
から容器３１に供給され、脱Ｓ、Ｐ用として
CaO、CaCl2、スケールがN2ガスとともにノズル
２２−１から湯溜り部２７に供給される。
第３図は脱Si槽２０−１と脱Ｐ、Ｓ槽２０−２
を水冷反応槽２０として竪型に構成し、湯溜り部
を耐火煉瓦とした例を示す。脱Si剤はノズル２２
−２から供給されて、排出口２３−１から脱Siス
ラグとし取出され、脱Ｐ、Ｓ剤はノズル２２−１
から供給されて、排出口２３−２から脱Ｐ、Ｓス
ラグとして取出される。
又脱Si槽と脱Ｐ、Ｓ槽との中間には、脱Siスラ
グと脱Ｐ、Ｓスラグとの混合層が形成されてい
る。
以上の通り本発明は構成されているので、次の
ような効果がある。
即ち溶銑の特徴を生かして、溶銑を小さい横断
面として反応槽に入れる事によつて、脱Si、Ｐ、
Ｓ反応で、最も重要であるスラグ−メタル接触面
積を拡げることが出来る。特に横型樋式に比較し
て、103〜105倍とする事が極めて容易なため、反
応時間を樋式の1/103〜1/105に短縮可能となり、
連続処理炉が極めて小型化出来る。
次に竪型であるため溶銑は上→下、反応スラグ
は下→上と対向流となり、横型樋式で問題となつ
た先行溶銑と後続溶銑又はスラグの混合がおこり
づらく、極めて安定した連続反応、向流反応が確
保出来て反応効率を高める事が可能である。
又溶銑は上→下への線状、粒状、フイルム状の
流れとなり、その周辺部を反応スラグが覆つてい
る形とすると、反応槽の外周部分には溶銑がない
ため、反応槽は耐火物で構成する必要がなく、金
属壁又は水冷、空冷を行つている金属壁で反応槽
を構成出来、溶銑予備処理で最も問題となる耐火
物問題（一つは耐火物コスト、もう一つは耐火物
中SiO2による反応スラグの反応性の低下）から
解放される。
更に本発明では脱Siと脱Ｐ、Ｓが連続処理によ
つて、容易に達成出来る利点がある。尚、反応槽
内では精錬反応時にCOガス等のガス体が一部発
生することもあるので、反応槽上部にガス抜き孔
をもうける事は、液状精錬スラツグの連続的排出
を定形化する事になる。
以下本発明装置の使用例をのべる。
使用例 １
第２図に示す竪型連続脱Si、Ｐ、Ｓ反応槽（脱
硅槽脱Ｐ、Ｓ槽ともに耐火物製内径100cmφ）
に、最上方より２m/mφ×200個の多孔ノズルよ
り、溶銑をTon／分で脱硅槽に供給し、下部溶銑
溜からさらに２m/mφ×200個の多孔ノズルを介
して、3Ton／分で脱Ｐ、Ｓ槽に溶銑を連続供給
した。
一方脱硅反応槽下部より、酸化鉄、酸素ガス
を、Arガスで稀薄して吹込み、又脱Ｐ、Ｓ槽下
部より、CaO、CaCl2、スケールをN2ガスで吹込
んで、表−１の如く効率的に連続処理結果を得
た。[Table] Since these are slag-metal reactions, in order to efficiently remove Si, P, and S, it is necessary to ensure a sufficient slag-metal reaction contact area. However, in order to ensure this by a horizontal gutter type continuous treatment method, there are the following problems regarding the reactor. (1) The slag-metal contact surface is primarily determined by the cross section of the device. If you try to increase this area, you will have to increase the size of the momentum refining device. In general, increasing the size of equipment is undesirable and impractical from the viewpoints of economical equipment costs, consumption of refractories, and heat loss. (2) A possible method for increasing the slag-metal contact area is to stir hot metal and slag. However, strong stirring causes mixing of the preceding hot metal and the following hot metal in the gutter, which causes the continuous processing characteristics to be lost and the processing to become difficult. Due to the problems (1) and (2), continuous processing of hot metal is theoretically and experimentally possible, but it has not yet been put into practical use. On the other hand, for example, in Japanese Patent Application Laid-Open No. 49-70812,
A spray refining method of hot metal using a vertical furnace has been proposed, and a method has been disclosed in which molten iron droplets falling from the vertical furnace are refined using an oxidizing gas of a slag-forming substance. Furthermore, Japanese Patent Publication No. 47-48767 proposes a vertical continuous desulfurization apparatus. The present invention proposes a vertical continuous hot metal pretreatment apparatus that is completely different from the above-mentioned prior art. The present invention will be explained below with reference to the drawings. FIG. 1 is a schematic diagram of a reaction tank of the present invention. In the figure, a reaction tank 20 is provided with a container 21, and hot metal P
is prepared. The container 21 is provided with a desired number of nozzles 25 and opens into the reaction tank 20 . Reaction tank 2
At the bottom of 0, there is a hot metal sump 27 equipped with a discharge nozzle 26. 22 indicates a refining agent addition nozzle;
A nozzle 22-1 is provided at the bottom of the reaction tank 20,
Nozzles 22-2 and 22-3 are provided in the body of the reaction tank. 23 is a discharge port from which the reaction-completed slag is taken out. The sump tank 27 may be provided with an auxiliary nozzle 22-4 to add the refining reactant. 35 is a gas vent hole. First, hot metal is transferred from the hot metal storage container through a nozzle or slit-like refractory into fine wires or droplets.
By creating a film-like form and increasing the reaction area,
Supplied to the upper part of the reaction tank. Hot metal is different from molten steel;
Due to the large difference ΔT between the hot metal temperature and the solidification temperature and the viscosity, it is easy to flow out as an extremely small cross section, and it is possible to have a cross section of several tens of microns. In the reaction tank of the present invention, a refining agent according to the purpose, that is, a de-Si reactant is kept in the upper part of the tank for removing P, and a reactant for S is kept in a molten state in the lower part of the tank. The hot metal descends from above to below in the liquid reactant, and during the descent, a slag-metal reaction occurs, and Si removal followed by P removal and S removal are performed. Since hot metal is continuously supplied to the reaction tank, it is necessary to replace the slag in the tank with new one, and new refining agent is supplied from below each reaction zone.
The reaction completed slag is discharged from the upper part of the reaction tank. In the present invention, a refining agent supply hole is provided in the middle part of the reaction tank, and by supplying a desiliconizing agent such as oxygen and iron oxide, a dephosphorization and S agent is supplied from the bottom of the desiliconizing reaction tank. By doing so, it is possible to improve the respective reaction efficiencies of P removal and S reaction. The hot metal that has finally passed through the reaction tank is stored in the lowest hot metal reservoir and discharged as needed. In the apparatus of the present invention, the slag-metal undergoes a countercurrent reaction, and the hot metal supplied to the reaction tank is formed in the form of a line, droplet, or film.
In this case, the linear, droplet, or film-like hot metal has a surface area of 0.5 cm 2 to 10 cm 2 /
1 g of hot metal is preferred. If it exceeds 10 cm 2 /g, there is a risk that hot metal will be discharged together with the continuously discharged liquid slag, and the effect of the device of the present invention will not be achieved. If it is less than 0.5 cm 2 /g, the countercurrent reaction may not be fully expected. Can not. Linear or film-like refractories can be easily formed by modifying the shape of the nozzle and slit-like refractories. Furthermore, formation of particles into droplets can be easily carried out by installing a magnetic stopper at the bottom of the nozzle or by applying vibration. In addition, the supply of the refining agent to the reaction tank in the present invention is as follows:
Different fluxes are added depending on the removal of Si, P, and S, but each must be in an almost completely molten state in the reaction tank. Therefore, a pre-dissolved refining agent can be added into the reaction tank, and from a thermal point of view it is preferable to add it from the side wall surface of one or more places in the reaction tank or directly into the hot metal sump. Pretreatment of hot metal can be broadly divided into two types. In other words, when oxidizing and removing elements that have an affinity for oxygen, such as Si, Mn, Cr, and Zr, oxygen gas and iron oxide (scale, iron ore powder, sintered ore powder, etc.) are used.
is mainly added, but in order to adjust the oxidation reaction, the basicity of the reaction tank may be adjusted by adding some CaO powder, etc. Next, when removing P and S, P and S are added to aggressiveness.
It is necessary to add a substance that binds to the carbon, and they can be broadly classified into CaO-based and soda-based. However, regarding the deP reaction, regardless of CaO type or soda type, if the Si content of the hot metal in the reaction tank is 0.2% or more, deP will hardly occur, so it is necessary to reduce it to 0.2%. . Furthermore, when using a CaO system, it is effective to use an appropriate amount of CaCl 2 , CaF 2 , etc. in terms of promoting the dissolution of CaO. In addition, it is effective to add oxygen gas and iron oxide together in order to strengthen the oxidation of deP or simultaneous deP and S reactions, regardless of whether it is a CaO type or a soda type. The side wall of the reaction tank of the present invention may be made of refractory material, but
In order to take advantage of the features of the vertical tank, the side walls are made wider in the turbulent region where the hot metal fall is located, and the reaction tank has a cooling structure. It is also possible to generate self-coding layers of agents. In this case, it is obvious that conventional metallurgical equipment can be freed from this problem, considering that much effort has always been devoted to solving the problem of refractories. Furthermore, by applying rotational motion to the vertical reaction, it is possible to activate the flow of liquid slag and improve the reaction efficiency with hot metal. In particular, regarding the length of the reaction tank, the surface area per unit weight of hot metal supplied from above (cm 2 /g
It depends on how much r) is and how much impurities are removed in the reaction tank.
0.8%, P0.08~0.15%, S0.2~0.04%), remove Si to 0.05~0.2% in a deSi tank,
Or deP, P0.01~0.02%, S0.01~0.015 in S tank
%, if the diameter of the supplied hot metal is several m/m, it is sufficient to have a diameter of several meters to around 10 meters. In addition, metallurgical reactions vary depending on the element to be removed, but since they are easily affected by temperature, by placing an induction heating device outside the reaction tank,
Allows you to freely control the temperature inside the tank. Furthermore, it is a matter of course that the metallurgical reaction can be promoted by induction stirring. FIGS. 2 and 3 show other embodiments of the present invention.
(The same reference numerals as in Fig. 1 have the same names, so explanations are omitted.) Fig. 2 shows the Si removal tank 20-1 and the P and S removal tank 20-2.
A reaction tank 20 is constructed by separating into two, and an induction coil 30 is provided around the outer periphery of the tank 20-2. Tank 20-1 and tank 2
A container 31 can be provided between the molten pig iron 0 and 0-2 to store the Si-free hot metal. The refining agent is iron oxide for removing Si, and oxygen gas is sent to the nozzle 22-2 along with Ar gas.
is supplied to the container 31 from
CaO, CaCl2 , and scale are supplied to the sump 27 from the nozzle 22-1 along with N2 gas. Figure 3 shows the Si removal tank 20-1 and the P removal and S tank 20-2.
An example is shown in which the water-cooled reaction tank 20 is configured in a vertical shape, and the water reservoir is made of refractory bricks. The desiliconizing agent is in nozzle 22.
-2, the de-Si slag is taken out from the discharge port 23-1, and the de-P and S agent is supplied from the nozzle 22-1.
The slag is supplied from the outlet 23-2 and taken out as de-P and S slag. Further, a mixed layer of Si-free slag and P-free/S-slag is formed between the Si-removal tank and the P-removal/S-removal tank. Since the present invention is configured as described above, it has the following effects. In other words, by taking advantage of the characteristics of hot metal and introducing it into a reaction tank with a small cross section, it is possible to remove Si, P,
The S reaction can expand the most important slag-metal contact area. In particular, compared to the horizontal gutter type, it is extremely easy to increase the reaction time by 10 3 to 10 5 times, making it possible to shorten the reaction time to 1/10 3 to 1/10 5 of the gutter type.
Continuous processing furnaces can be extremely miniaturized. Secondly, because it is vertical, the hot metal flows in counter-flows from top to bottom and the reaction slag flows from bottom to top, making it difficult for the preceding hot metal to mix with the following hot metal or slag, which was a problem with horizontal gutter systems, resulting in an extremely stable continuous reaction. , it is possible to ensure a countercurrent reaction and increase the reaction efficiency. In addition, the hot metal flows from top to bottom in a linear, granular, or film-like manner, and if the periphery is covered with reaction slag, there is no hot metal on the outer periphery of the reaction tank, so the reaction tank is made of refractory material. The reaction tank can be constructed with a metal wall or a metal wall that is water-cooled or air-cooled. The reduction in reactivity of the reaction slag caused by SiO 2 in the material is eliminated. Furthermore, the present invention has the advantage that removal of Si, P, and S can be easily achieved through continuous processing. In addition, some gases such as CO gas may be generated in the reaction tank during the refining reaction, so providing a gas vent hole at the top of the reaction tank will help to regularize the continuous discharge of liquid refining slag. Become. Examples of use of the device of the present invention will be described below. Usage example 1 Vertical continuous desiliconization, P, and S reaction tank shown in Figure 2 (Both desiliconization tank and S tank are made of refractory and have an inner diameter of 100cmφ)
Then, hot metal is supplied from the top to the desiliconization tank at a rate of 2 m/mφ x 200 porous nozzles at a rate of 1 ton/min, and from the lower hot metal sump, it is further supplied to the desiliconization tank through 2 m/m φ x 200 porous nozzles at a rate of 3 ton/min. Hot metal was continuously supplied to the P removal and S tank. On the other hand, iron oxide and oxygen gas diluted with Ar gas were blown in from the bottom of the desiliconization reaction tank, and CaO, CaCl 2 and scale were blown in with N 2 gas from the bottom of the deP and S tank. Efficient continuous processing results were obtained.
【表】
使用例 ２
第３図に示す竪型連続脱Si、Ｐ、Ｓ反応槽（水
冷SUS製内径150cmφ）に、最上方より２m/mφ
×400個の多孔ノズルより、溶銑5Ton／分で脱硅
槽に供給し、脱硅槽下部と脱Ｐ、Ｓ槽の間に、混
合槽をもうけ、その下に直接脱Ｐ、Ｓ槽を直結し
た。
この様に混合層をもうける事によつて、脱硅、
脱Ｐ、Ｓ槽を上下に直結しても特に効率を下げる
事なく、連続脱Si、Ｐ、Ｓ処理が出来た。
その結果を表−２に示す。[Table] Usage example 2 In the vertical continuous deSi, P, S reaction tank (made of water-cooled SUS, inner diameter 150 cmφ) shown in Figure 3, 2 m/mφ from the top.
Hot metal is supplied to the desiliconization tank at a rate of 5 tons/min through 400 multi-hole nozzles, and a mixing tank is created between the bottom of the desiliconization tank and the desulfurization and S tanks, and the desulfurization and S tanks are directly connected below it. did. By creating a mixed layer in this way, desiliconization,
Continuous deSi, P, and S treatment was possible without any particular reduction in efficiency even when the P and S tanks were connected directly above and below. The results are shown in Table-2.
第１図は本発明の説明図、第２図、第３図は本
発明の他の実施例の説明図である。
２０：反応槽、２１：溶銑容器、２２：精錬剤
添加ノズル、２７：溶銑湯溜部。
FIG. 1 is an explanatory diagram of the present invention, and FIGS. 2 and 3 are explanatory diagrams of other embodiments of the present invention. 20: Reaction tank, 21: Hot metal container, 22: Refining agent addition nozzle, 27: Hot metal sump.
Claims (1)
下方域に脱Ｐ、Ｓゾーンを形成するノズルを設
け、該ゾーンの上方域に脱Siゾーンを形成するノ
ズルを設けて反応槽を構成し、前記脱Siゾーンの
上部にスラグ排出口を設け、底部に溶銑湯溜槽を
設けて、前記反応槽に、前記溶銑容器を竪型に配
設した竪型連続溶銑予備処理装置。 ２ 底部に所望数のノズルを設けた溶銑容器と、
脱Siゾーンを形成するノズルを設け、底部に所望
数のノズルを設けた溶銑容器からなる第１反応槽
と、脱Ｐ、Ｓゾーンを形成するノズルを設け、底
部に湯溜槽を設けた第２反応槽とを、順次竪型に
配設し、各反応槽の上部に、スラグ排出口を設け
た竪型連続溶銑予備処理装置。[Claims] 1. A hot metal container having a desired number of nozzles at the bottom;
A reaction tank is configured by providing a nozzle for forming a de-P and S zone in a lower region, a nozzle for forming a de-Si zone in an upper region of the zone, and a slag discharge port is provided in the upper part of the de-Si zone, A vertical continuous hot metal pretreatment device, comprising: a hot metal reservoir provided at the bottom; and the hot metal container vertically disposed in the reaction tank. 2. A hot metal container equipped with a desired number of nozzles at the bottom;
A first reaction tank consisting of a hot metal container equipped with a nozzle for forming a Si-removal zone and a desired number of nozzles at the bottom, and a second reaction tank consisting of a hot metal container equipped with a nozzle for forming a de-P and S zone and a sump tank at the bottom. A vertical continuous hot metal pretreatment device in which reaction tanks are sequentially arranged vertically and a slag discharge port is provided at the top of each reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5097182A JPS58171518A (en) | 1982-03-31 | 1982-03-31 | Vertical type continuous preliminary treating method of molten pig iron |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5097182A JPS58171518A (en) | 1982-03-31 | 1982-03-31 | Vertical type continuous preliminary treating method of molten pig iron |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58171518A JPS58171518A (en) | 1983-10-08 |
| JPS6133042B2 true JPS6133042B2 (en) | 1986-07-31 |
Family
ID=12873694
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5097182A Granted JPS58171518A (en) | 1982-03-31 | 1982-03-31 | Vertical type continuous preliminary treating method of molten pig iron |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58171518A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0349541U (en) * | 1989-09-19 | 1991-05-15 |
-
1982
- 1982-03-31 JP JP5097182A patent/JPS58171518A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0349541U (en) * | 1989-09-19 | 1991-05-15 |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58171518A (en) | 1983-10-08 |
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