JPH0247529B2 - - Google Patents
Info
- Publication number
- JPH0247529B2 JPH0247529B2 JP23859783A JP23859783A JPH0247529B2 JP H0247529 B2 JPH0247529 B2 JP H0247529B2 JP 23859783 A JP23859783 A JP 23859783A JP 23859783 A JP23859783 A JP 23859783A JP H0247529 B2 JPH0247529 B2 JP H0247529B2
- Authority
- JP
- Japan
- Prior art keywords
- rotary kiln
- cao
- steel dust
- weight
- sio
- 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
- 239000000428 dust Substances 0.000 claims description 32
- 229910000831 Steel Inorganic materials 0.000 claims description 31
- 239000010959 steel Substances 0.000 claims description 31
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 16
- 229910052725 zinc Inorganic materials 0.000 claims description 13
- 229910052745 lead Inorganic materials 0.000 claims description 11
- 239000003638 chemical reducing agent Substances 0.000 claims description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 48
- 239000000292 calcium oxide Substances 0.000 description 24
- 235000012255 calcium oxide Nutrition 0.000 description 24
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 20
- 239000011701 zinc Substances 0.000 description 17
- 238000002844 melting Methods 0.000 description 11
- 230000008018 melting Effects 0.000 description 10
- 239000011787 zinc oxide Substances 0.000 description 10
- 239000000203 mixture Substances 0.000 description 7
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 6
- 229910052731 fluorine Inorganic materials 0.000 description 6
- 239000011737 fluorine Substances 0.000 description 6
- 230000002829 reductive effect Effects 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000010587 phase diagram Methods 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 239000008188 pellet Substances 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 229910004261 CaF 2 Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- -1 can be used Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 230000002452 interceptive effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Classifications
-
- 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
- Y02P10/20—Recycling
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Description
本発明は、鉄鋼ダスト中に含まれるZnおよび
Pbを、還元揮発させて回収さる鉄鋼ダストの還
元焙焼方法に関する。
鉄鋼業の平電炉および高炉から発生する鉄鋼ダ
ストは酸化鉄以外にZn、Pbを含有しているので、
従来からこの鉄鋼ダスト中のZnやPbを回収する
ことが行なわれているが、従来最も一般的に行な
われているのは、ウエルツキルン法に代表される
還元焙焼法であり、内熱向流型のロータリーキル
ンが使用される。鉄鋼ダストは粉粒状のまゝか、
あるいは必要に応じてペレツトに成形され、石炭
やコークス等の炭素質還元剤と共にロータリーキ
ルンに装入され、適切な温度と滞留時間を選んで
還元焙焼され、還元揮発したZn、Pbは排ガスと
共に炉外に導びかれて集塵機によつてPbを含有
する粗酸化亜鉛として回収される。このような鉄
鋼ダストの還元焙焼方法において、ZnやPbの揮
発性の向上をはかるためには、還元雰囲気を強く
し還元温度を高くするのが有効であるが、高温度
で還元すると、融点の低い成分がロータリーキル
ン内壁へ融着してリング状の付着物を生成し、こ
れを除去するために一旦操業を休止することが必
要となり、連続操業可能な期間を短かくしてしま
う。従つて、操業の稼動率を高める目的で連続操
業が可能な期間をある程度長くするためには、上
記したリング状付着物の生長を抑えるため、しば
しばロータリーキルン内の温度を下げざるを得な
くなり、従つてZn、Pbの揮発回収率は低くなら
ざるを得ない。即ち、上記した従来の鉄鋼ダスト
の還元焙焼方法は、低融点成分のロータリーキル
ン内壁への融着のために、連続操業可能な期間が
短かく、しかもZn、Pbの揮発率もあまり高くで
きないという欠点があつた。
本発明者等は、鉄鋼ダストにCaO源を添加して
ロータリーキルン装入物のCaO／SiO2重量比を
高めることによつて、ロータリーキルン内壁付着
物の生長を効果的に抑制することが可能であるこ
と、また回収された粗酸化亜鉛を亜鉛製錬工程で
処理する際、妨害成分となるフツ素等のハロゲン
元素の含有率を下げることが可能であることに着
目し、本発明に到達したものである。
従つて本発明の目的は、鉄鋼ダストの還元焙焼
方法において、ロータリーキルン内の高温領域に
おける内壁付着物の生長を抑制して長期間の連続
操業を可能とし、ZnおよびPbの揮発回収率を高
めること、および回収された粗酸化亜鉛のフツ素
含有量を下げることのできる還元焙焼方法を提供
することにある。
この目的を達成するため本発明は、含Zn、Pb
鉄鋼ダストと炭素質還元剤をロータリーキルンに
装入し、ロータリーキルンの排出側端部にバーナ
ーを設けてロータリーキルン内を加熱することに
よつてZnおよびPbを還元揮発させて回収する鉄
鋼ダストの還元焙焼方法において、鉄鋼ダストに
CaO源を添加してロータリーキルン装入物の
CaO／SiO2重量比を2.5以上とすることを特徴と
するものである。
通常、鉄鋼ダストの組成はZn20〜24重量％、
Pb2〜４重量％、Fe25〜30重量％、CaO1〜５重
量％、SiO21〜５重量％、C1〜３重量％、MgO2
〜５重量％、Al2O31〜４重量％、F1〜1.5重量％
であり、CaO／SiO2重量比は0.8〜1.2であるが、
この鉄鋼ダストに炭素質還元剤を添加し加熱還元
してZnおよびPbを高い揮発率で回収するために
は1100〜1200℃に加熱する必要がある。しかしな
がら上記組成の鉄鋼ダストは、そのままでは1100
〜1200℃で軟化溶融を起し、そのため前記したロ
ータリーキルン内壁付着物を生成し易くなる。鉄
鋼ダストが高温で還元されるとき生ずる低融点物
は、CaO−FeO−SiO2系にMgO、Al2O3等が加わ
つた多元系の物質であつて、その溶融点はCaO−
FeO−SiO2系状態図から予測される溶融点より
も低くなるが、本発明者等はCaO／SiO2重量比
の違いによる溶融点の変化の傾向をCaO−FeO−
SiO2系状態図を用いて推定した。即ち、図に
CaO−FeO−SiO2系状態図を示すが、図におい
てＡで示される領域が鉄鋼ダストをそのまゝ還元
した場合に生成する低融点物の領域であるのに対
して、この鉄鋼ダストにCaO源を添加してCaO／
SiO2重量比を2.5以上とした場合に還元過程で生
成する物質はＢで示される領域のものとなり、そ
の溶融点は200℃程度高くなることが期待できる。
このような推定に基ずいて、本発明者等は鉄鋼ダ
ストにCaOを添加してCaO／SiO2重量比を変え
た混合物をつくり、これを還元雰囲気の下で加熱
して実際の溶融点を測定した。その結果を第１表
に示す。
The present invention focuses on the Zn and steel dust contained in steel dust.
This invention relates to a method for reducing and roasting steel dust, which recovers Pb by reducing and volatilizing it. Steel dust generated from flat electric furnaces and blast furnaces in the steel industry contains Zn and Pb in addition to iron oxide.
Recovery of Zn and Pb from this steel dust has been carried out for a long time, but the most commonly used method is the reduction roasting method represented by the Wertz kiln method, which uses internal heat countercurrent. A type of rotary kiln is used. Is the steel dust still in the form of powder or granules?
Alternatively, if necessary, the pellets are formed into pellets, charged into a rotary kiln together with a carbonaceous reducing agent such as coal or coke, and reduced and roasted by selecting an appropriate temperature and residence time. It is led outside and collected by a dust collector as crude zinc oxide containing Pb. In such a reduction roasting method for steel dust, it is effective to strengthen the reducing atmosphere and raise the reduction temperature in order to improve the volatility of Zn and Pb. Components with low levels of fused to the inner wall of the rotary kiln form a ring-shaped deposit, which requires temporary suspension of operation to remove this, which shortens the period during which continuous operation is possible. Therefore, in order to extend the period during which continuous operation is possible for the purpose of increasing the operation rate, it is often necessary to lower the temperature inside the rotary kiln in order to suppress the growth of the ring-shaped deposits described above. Therefore, the volatilization recovery rate of Zn and Pb has to be low. In other words, the conventional reduction roasting method for steel dust mentioned above has a short period of continuous operation due to the fusion of low melting point components to the inner wall of the rotary kiln, and furthermore, the volatilization rate of Zn and Pb cannot be very high. There were flaws. The present inventors have found that it is possible to effectively suppress the growth of deposits on the inner wall of a rotary kiln by adding a CaO source to steel dust and increasing the CaO/SiO 2 weight ratio of the rotary kiln charge. The present invention was developed by focusing on the fact that it is possible to reduce the content of halogen elements such as fluorine, which become interfering components when treating recovered crude zinc oxide in a zinc smelting process. It is. Therefore, an object of the present invention is to suppress the growth of deposits on the inner wall in the high temperature region of a rotary kiln in a reduction roasting method for steel dust, enable long-term continuous operation, and increase the volatilization recovery rate of Zn and Pb. Another object of the present invention is to provide a reduction roasting method capable of lowering the fluorine content of recovered crude zinc oxide. In order to achieve this objective, the present invention
Reductive roasting of steel dust, in which steel dust and carbonaceous reducing agent are charged into a rotary kiln, and a burner is installed at the discharge end of the rotary kiln to heat the inside of the rotary kiln to reduce and volatilize Zn and Pb and recover them. In the method, to steel dust
Addition of CaO source to rotary kiln charge
It is characterized by having a CaO/SiO 2 weight ratio of 2.5 or more. Usually, the composition of steel dust is Zn20-24% by weight,
Pb2-4% by weight, Fe25-30% by weight, CaO1-5% by weight, SiO2 1-5% by weight, C1-3% by weight, MgO2
~5% by weight, Al2O3 1~4% by weight , F1~1.5% by weight
, and the CaO/SiO 2 weight ratio is 0.8 to 1.2,
In order to add a carbonaceous reducing agent to this steel dust and perform thermal reduction to recover Zn and Pb at a high volatility rate, it is necessary to heat the dust to 1100-1200°C. However, steel dust with the above composition is 1100
It undergoes softening and melting at ~1200°C, and therefore tends to form the aforementioned deposits on the inner walls of the rotary kiln. The low-melting point substance that is produced when steel dust is reduced at high temperatures is a multi-element substance consisting of the CaO-FeO-SiO 2 system plus MgO, Al 2 O 3 , etc., and its melting point is CaO-
Although the melting point is lower than that predicted from the phase diagram of the FeO−SiO 2 system, the present inventors have investigated the tendency of the melting point change due to the difference in the CaO/SiO 2 weight ratio.
Estimated using the SiO 2 system phase diagram. That is, in fig.
The CaO-FeO-SiO 2 system phase diagram is shown. The region indicated by A in the diagram is the region of low melting point substances that are produced when steel dust is directly reduced, whereas CaO CaO/
When the weight ratio of SiO 2 is set to 2.5 or more, the substances generated in the reduction process are in the range shown by B, and the melting point can be expected to be about 200°C higher.
Based on these estimates, the present inventors added CaO to steel dust to create mixtures with varying CaO/SiO 2 weight ratios, heated them in a reducing atmosphere, and determined the actual melting point. It was measured. The results are shown in Table 1.
【表】
第１表によれば、CaO／SiO2重量比が0.97では
溶融点は1100〜1150℃であるが、CaO／SiO2重
量比2.56で1300℃以上となり、前記した状態図に
よる予測と大略一致する傾向が確かめられた。
また、鉄鋼ダストにCaO源を添加して焙焼すれ
ば次式、
MF2＋H2O→MO＋2HF
2HF＋CaO→CaF2＋H2O
（Ｍ：鉄鋼ダスト中のPb等の金属元素）
に従つてフツ素が固定され、揮発回収される粗酸
化亜鉛中に入るフツ素が減少することが期待でき
る。
以上のような知見に基ずいて、本願発明者等は
実操業において鉄鋼ダストに石灰石等のCaO源を
添加して装入物のCaO／SiO2重量比を2.5以上と
し、これをコークス等の炭素質還元剤と共にロー
タリーキルンに連続的に装入し、ロータリーキル
ン排出側端部からロータリーキルン内をバーナー
で加熱して還元焙焼を行なつた。ロータリーキル
ン内壁への付着物の生長が効果的に抑制され、連
続操業可能な期間は従来法の30日間から60日間へ
と延長し、その間充分な高温での還元が持続でき
るようになると共に、粗酸化亜鉛に入るフツ素の
量は第２表に示すように大幅に低下した。[Table] According to Table 1, when the CaO/SiO 2 weight ratio is 0.97, the melting point is 1100 to 1150°C, but when the CaO/SiO 2 weight ratio is 2.56, it is over 1300°C, which is in line with the prediction from the phase diagram above. A roughly consistent tendency was confirmed. In addition, if a CaO source is added to steel dust and roasted, fluorine will be produced according to the following formula: MF 2 + H 2 O → MO + 2HF 2HF + CaO → CaF 2 + H 2 O (M: metallic element such as Pb in steel dust) is fixed, and it can be expected that the amount of fluorine that enters the crude zinc oxide that is volatilized and recovered will be reduced. Based on the above knowledge, the inventors added a CaO source such as limestone to steel dust in actual operation to make the CaO/SiO 2 weight ratio of the charge 2.5 or more, and used this as a source of coke, etc. It was continuously charged into a rotary kiln together with a carbonaceous reducing agent, and the inside of the rotary kiln was heated with a burner from the discharge side end of the rotary kiln to perform reduction roasting. The growth of deposits on the inner wall of the rotary kiln is effectively suppressed, and the period during which continuous operation can be performed is extended from 30 days to 60 days using the conventional method. The amount of fluorine entering the zinc oxide was significantly reduced as shown in Table 2.
【表】
なお本発明法において、装入物中のCaO／
SiO2重量比は2.5以上であれば効果があるが、あ
まり多量のCaO源を添加するとロータリーキルン
装入物の物量が増大して加熱に要するエネルギー
が大となり、装入物中のZn品位を下げて不利と
なるので、CaO／SiO2重量比の上限は3.5程度に
抑えるのが経済的である。
また、添加するCaO源としては生石灰の他に、
石灰石、消石灰等の高温でCaOを生成する物質で
あればいずれも使用可能であり、ドロマイト等を
添加しても良く、添加方法もロータリーキルン装
入前に鉄鋼ダストとあらかじめ混合したり、ペレ
ツトとして内装してもよいが、そのまゝ鉄鋼ダス
トと共に連続的に装入すればロータリーキルン炉
内で自然に混合が行なわれ、充分な効果が得られ
る。
以上詳細に説明したように、本発明の鉄鋼ダス
トの還元焙焼方法によれば、ロータリーキルン内
壁付着物の生長を抑制して長期間の連続操業が可
能となり、且つ炉内温度を高温に維持できるので
Zn、Pbの揮発回収率を高くすることができ、ま
た回収された粗酸化亜鉛中のフツ素の含有量を低
くすることができて亜鉛製錬工程で処理するのに
適した品質の良い粗酸化亜鉛を回収することがで
きるという大きな効果がある。
実施例
レンガ内径３ｍ、長さ50ｍ、勾配２％のロータ
リーキルンに、Zn23重量％、Pb3重量％、Fe30
重量％、CaO5重量％、SiO24重量％、C1重量％、
F1.5重量％の組成の鉄鋼ダストとCaO55重量％の
石灰石、およびC88重量％のコークスを、それぞ
れ8500Kg／Ｈ、1000Kg／Ｈ、1500Kg／Ｈで連続的
に装入し、装入物のCaO／SiO2重量比を2.8とな
るようにして、ロータリーキルン排出端に設けた
重油バーナーでロータリーキルン内を1200℃に加
熱して還元焙焼を行なつた。
ロータリーキルン内壁付着物の生長を効果的に
抑制して60日間の連続操業を行ない、Zn60重量
％、Pb7重量％、F0.84重量％の粗酸化亜鉛を
2960Kg／Ｈで回収し、Zn揮発率90.8％、Pb揮発
率81.2％の成績を得た。
比較例
実施例と同一のロータリーキルンに、実施例と
同一組成の鉄鋼ダストとコークスを、それぞれ
8500Kg／Ｈ、1500Kg／Ｈで連続的に装入し、CaO
源を装入することなく、重油バーナーでロータリ
ーキルン内を1200℃に加熱して還元焙焼を行なつ
た。ロータリーキルン内壁付着物の生長が著るし
く、時々加熱温度を下げざるを得ない場合が生
じ、連続操業可能な期間は30日間であつた。ま
た、Zn57重量％、Pb6.6重量％、F1.97重量％の
粗酸化亜鉛を2942Kg／Ｈで回収し、Zn揮発率85.8
％、Pb揮発率76.5％であつた。[Table] In addition, in the method of the present invention, CaO/
It is effective if the SiO 2 weight ratio is 2.5 or more, but if too much CaO source is added, the amount of the rotary kiln charge will increase, the energy required for heating will increase, and the Zn quality in the charge will decrease. Therefore, it is economical to suppress the upper limit of the CaO/SiO 2 weight ratio to about 3.5. In addition to quicklime, CaO sources to be added include
Any substance that generates CaO at high temperatures, such as limestone or slaked lime, can be used, and dolomite, etc., can also be added.Addition methods include pre-mixing with steel dust before charging into the rotary kiln, or adding it as pellets. However, if it is continuously charged as is with the steel dust, mixing will occur naturally in the rotary kiln, and a sufficient effect will be obtained. As explained in detail above, according to the method for reducing and roasting steel dust of the present invention, it is possible to suppress the growth of deposits on the inner wall of a rotary kiln, to enable continuous operation for a long period of time, and to maintain the temperature inside the furnace at a high temperature. So
It is possible to increase the volatilization recovery rate of Zn and Pb, and to reduce the fluorine content in the recovered crude zinc oxide, resulting in a high quality crude zinc oxide suitable for processing in the zinc smelting process. It has the great effect of being able to recover zinc oxide. Example: In a rotary kiln with a brick inner diameter of 3 m, a length of 50 m, and a slope of 2%, Zn23% by weight, Pb3% by weight, Fe30
wt%, CaO5 wt%, SiO2 4 wt%, C1 wt%,
Steel dust with a composition of 1.5% by weight of F, limestone with a composition of 55% by weight of CaO, and coke with a composition of 88% by weight of C were continuously charged at 8500Kg/H, 1000Kg/H, and 1500Kg/H, respectively. /SiO 2 weight ratio was 2.8, and the inside of the rotary kiln was heated to 1200°C using a heavy oil burner installed at the rotary kiln discharge end to perform reduction roasting. The rotary kiln was operated continuously for 60 days while effectively suppressing the growth of deposits on the inner walls, and crude zinc oxide containing 60% by weight of Zn, 7% by weight of Pb, and 0.84% by weight of F was produced.
It was recovered at 2960Kg/H, and the Zn volatilization rate was 90.8% and the Pb volatilization rate was 81.2%. Comparative Example Steel dust and coke with the same composition as in the example were placed in the same rotary kiln as in the example.
Continuously charged at 8500Kg/H, 1500Kg/H, CaO
Reduction roasting was performed by heating the inside of the rotary kiln to 1200°C using a heavy oil burner without charging any source. The growth of deposits on the inner walls of the rotary kiln was so significant that it was sometimes necessary to lower the heating temperature, and the period of continuous operation was only 30 days. In addition, crude zinc oxide containing 57% by weight of Zn, 6.6% by weight of Pb, and 1.97% by weight of F was recovered at 2942 kg/h, and the Zn volatile rate was 85.8.
%, and the Pb volatilization rate was 76.5%.
図はCaO−FeO−SiO2系状態図における低融
点物の生成領域を示す図である。
The figure is a diagram showing the generation region of low melting point substances in the CaO-FeO-SiO 2 system phase diagram.
Claims (1)
タリーキルンに装入し、ロータリーキルンの排出
側端部にバーナーを設けてロータリーキルン内を
加熱することによつて、ZnおよびPbを還元揮発
させて回収する鉄鋼ダストの還元焙焼方法におい
て、鉄鋼ダストにCaO源を添加してロータリーキ
ルン装入物のCaO／SiO2重量比を2.5以上とする
ことを特徴とする鉄鋼ダストの還元焙焼方法。1 Charge Zn and Pb steel dust and a carbonaceous reducing agent into a rotary kiln, install a burner at the discharge end of the rotary kiln, and heat the inside of the rotary kiln to reduce and volatilize Zn and Pb and recover them. A method for reducing and roasting steel dust, the method comprising: adding a CaO source to the steel dust so that the CaO/SiO 2 weight ratio of the rotary kiln charge is 2.5 or more.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58238597A JPS60128228A (en) | 1983-12-16 | 1983-12-16 | Reduction roasting method of iron and steel dust |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58238597A JPS60128228A (en) | 1983-12-16 | 1983-12-16 | Reduction roasting method of iron and steel dust |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60128228A JPS60128228A (en) | 1985-07-09 |
| JPH0247529B2 true JPH0247529B2 (en) | 1990-10-22 |
Family
ID=17032554
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58238597A Granted JPS60128228A (en) | 1983-12-16 | 1983-12-16 | Reduction roasting method of iron and steel dust |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60128228A (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4802919A (en) * | 1987-07-06 | 1989-02-07 | Westinghouse Electric Corp. | Method for processing oxidic materials in metallurgical waste |
| DE4339591A1 (en) * | 1993-11-20 | 1995-05-24 | Metallgesellschaft Ag | Rolling process for the processing of materials containing zinc, lead and iron oxides |
| JP4564126B2 (en) * | 2000-03-27 | 2010-10-20 | 住友重機械工業株式会社 | Method for producing molten iron using a rotary kiln |
| JP4762420B2 (en) * | 2001-02-20 | 2011-08-31 | 住友重機械工業株式会社 | Method of smelting reduction of iron oxide using a rotary kiln |
| AT414127B (en) * | 2004-04-27 | 2006-09-15 | Patco Engineering Gmbh | METHOD FOR RECOVERING METALS AND / OR METAL OXIDES FROM STEELWORDS DUST |
| JP2009127064A (en) * | 2007-11-20 | 2009-06-11 | Sumitomo Heavy Ind Ltd | Reduction treatment apparatus and reduction treatment method |
| JP5770118B2 (en) * | 2012-02-02 | 2015-08-26 | 新日鐵住金株式会社 | Method for producing reduced iron |
| JP6090080B2 (en) * | 2013-09-20 | 2017-03-08 | 住友金属鉱山株式会社 | Operation method of reduction roasting furnace |
-
1983
- 1983-12-16 JP JP58238597A patent/JPS60128228A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60128228A (en) | 1985-07-09 |
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