JPS63241125A - Method and device for prereduction of fine ore by using exhaust gas sucked from smelting reduction furnace - Google Patents
Method and device for prereduction of fine ore by using exhaust gas sucked from smelting reduction furnaceInfo
- Publication number
- JPS63241125A JPS63241125A JP16456987A JP16456987A JPS63241125A JP S63241125 A JPS63241125 A JP S63241125A JP 16456987 A JP16456987 A JP 16456987A JP 16456987 A JP16456987 A JP 16456987A JP S63241125 A JPS63241125 A JP S63241125A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- gas
- fine ore
- flue
- solid
- 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.)
- Pending
Links
- 230000009467 reduction Effects 0.000 title claims abstract description 76
- 238000003723 Smelting Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims description 19
- 239000007789 gas Substances 0.000 claims description 136
- 239000003638 chemical reducing agent Substances 0.000 claims description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 239000000428 dust Substances 0.000 abstract description 19
- 239000000843 powder Substances 0.000 abstract description 8
- 239000010419 fine particle Substances 0.000 abstract description 3
- 238000006722 reduction reaction Methods 0.000 description 66
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 16
- 238000002844 melting Methods 0.000 description 12
- 230000008018 melting Effects 0.000 description 12
- 229910052742 iron Inorganic materials 0.000 description 8
- 239000002184 metal Substances 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 8
- 239000003245 coal Substances 0.000 description 7
- 238000007664 blowing Methods 0.000 description 6
- 238000005520 cutting process Methods 0.000 description 6
- 230000007246 mechanism Effects 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 229910000805 Pig iron Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000007654 immersion Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000009792 diffusion process Methods 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
- 230000008569 process Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910000640 Fe alloy Inorganic materials 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 230000004323 axial length Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000010406 interfacial reaction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Manufacture Of Iron (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、鉄鉱石、予備還元物等の酸化物系原料を固体
炭素等で溶融還元する際に、溶融還元炉で発生した排ガ
スを原料の予備還元・予熱に有効利用する方法及び装置
に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention uses waste gas generated in a smelting reduction furnace when smelting and reducing oxide raw materials such as iron ore and pre-reduced products with solid carbon. The present invention relates to a method and an apparatus that can be effectively utilized for preliminary reduction and preheating.
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、シャフト炉で還元した鉄鉱石原料を電気炉で溶
解する方法等が従来から採用されている。In order to reduce iron ore to produce hot metal, methods such as using a blast furnace and melting iron ore raw material reduced in a shaft furnace in an electric furnace have been adopted.
ところが、高炉を使用する方法においては、熱源及び還
元材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、炉内の通気性及び還元性を向上させる
ために、焼結鉱として高炉に装入されるのが通常である
。このため、高炉法には、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が必
要となる。したがって、多大な設備費は勿論のこと、多
くのエネルギー及び労働力を必要とし、処理コストの高
騰を招くという欠点があった。また、強粘結炭は、世界
的に賦存量が少なく且つ地域的に偏在した賦与状態とな
っているために、供給が不安定になり易いという問題も
ある。However, in the method using a blast furnace, a large amount of coke is used as a heat source and reducing agent. In addition, iron ore, which is an iron source, is usually charged into a blast furnace as sintered ore in order to improve air permeability and reducibility within the furnace. Therefore, the blast furnace method requires coke oven equipment for dry distilling highly caking coal and sintering equipment for producing sintered ore. Therefore, there is a drawback that not only a large amount of equipment costs but also a large amount of energy and labor are required, leading to a rise in processing costs. In addition, there is also the problem that the supply of highly coking coal tends to be unstable because there is only a small amount of it available worldwide and the supply is unevenly distributed in different regions.
他方、シャフト炉による鉄鉱石の還元法においては、鉄
鉱石を例えばペレット化する前処理が必要となり、また
還元材及び熱源として高価な天然ガス及び電力等を多量
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 pre-treatment, such as pelletizing the iron ore, and has the disadvantage that it consumes large amounts of expensive natural gas and electricity as a reducing agent and 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り、シャフト炉型、転炉
型、混銑炉型等がある。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 with the aim of producing molten iron alloys using smaller-scale equipment without being restricted by the raw materials used, and is of the shaft furnace type, There are converter type, mixed pig iron furnace type, etc.
これらのタイプのうち、混銑炉型の溶融還元炉は、浴面
を大きくとることができるため、溶湯と溶融スラグとの
界面反応を活発に行うことができるものとして有望視さ
れている。また、その浴面の大きさは炉の長さに応じて
適宜法められるものであるから、生産量に応じた浴面を
自由に選ぶことが可能となる。本発明者等も、このよう
な形式の炉において一定条件下でガス吹込みを行えるも
のを開発し、これを特願昭６１−８６７９４号として先
に出願した。Among these types, mixed iron furnace type smelting reduction furnaces have a large bath surface and are therefore considered promising as they can actively carry out interfacial reactions between the molten metal and molten slag. Furthermore, since the size of the bath surface is determined as appropriate depending on the length of the furnace, it is possible to freely select the bath surface according to the production volume. The inventors of the present invention also developed a furnace of this type that allows gas injection under certain conditions, and filed an application for this in Japanese Patent Application No. 86794/1983.
ところが、この種の溶融還元炉から排出される排ガスは
、粉鉱石、粉炭等の粉塵が浮遊している高温状態にある
。この排ガスをそのまま廃棄するとき大気を汚染する原
因となるため、排ガス集塵装置を必ず設置しなければな
らない。しかし、この排ガスを集塵するだけで排出した
のでは、資源の利用効率及び熱経済性からみて極めて不
合理なものとなる。また、この排ガスには多量のｃｏｔ
７．分が含まれていることから、還元能を有している。However, the exhaust gas discharged from this type of smelting reduction furnace is in a high temperature state in which dust such as fine ore and powdered coal is suspended. When this exhaust gas is disposed of as it is, it causes air pollution, so an exhaust gas dust collector must be installed. However, discharging this exhaust gas only by collecting dust would be extremely unreasonable in terms of resource utilization efficiency and thermoeconomic efficiency. In addition, this exhaust gas contains a large amount of cot.
7. It has reducing ability because it contains
この面でも、排ガスの再利用が望まれるところであるが
、今までのところ該排ガスの再利用法として適切なもの
が提案されていない。In this respect as well, it is desired to reuse the exhaust gas, but so far no suitable method for reusing the exhaust gas has been proposed.
他方、溶融還元炉に装入される鉱石原料としては、炉内
の還元反応を高めるために、予熱・予備還元されたもの
を使用することが望ましい。そこで、この溶融還元炉に
予熱装置及び予備還元装置を付設した設備設計が考えら
れている。しかし、このような付帯設備を配置するとき
、設備費の高騰を招き、本来経済的な溶融金属製造法と
して開発された溶融還元法の長所を損なうことになる。On the other hand, as the ore raw material charged into the smelting reduction furnace, it is desirable to use one that has been preheated and pre-reduced in order to enhance the reduction reaction within the furnace. Therefore, a facility design in which a preheating device and a preliminary reduction device are attached to this smelting reduction furnace is being considered. However, when arranging such ancillary equipment, the cost of the equipment increases and the advantages of the smelting reduction method, which was originally developed as an economical method for producing molten metal, are lost.
そこで、本発明は、排ガスのもつ還元能及び熱量に着目
し、この排ガスを粉鉱石の予備還元・予熱に利用するた
めに、排ガス処理装置を予熱装置や予備還元装置として
兼用することにより、極めて経済的設備とすると共に効
率的な溶融還元を行うことを目的とする。Therefore, the present invention focuses on the reducing ability and calorific value of exhaust gas, and in order to utilize this exhaust gas for preliminary reduction and preheating of fine ore, the exhaust gas treatment device is also used as a preheating device and a preliminary reduction device. The purpose is to make the equipment economical and to perform efficient melting reduction.
本発明の排ガスの処理法は、その目的を達成するために
、溶融還元炉から排出される排ガスを、煙道を介して固
気分離器を通して吸引すると共に、前記煙道の途中のガ
ス温度６００℃以上で且つＣＯ濃度が４０％以上の該排
ガス中に粉鉱石を供給し、排ガスの流れに乗せて搬送す
ると共に予備還元を行い、且つ前記固気分離器により排
ガスから分離することにより粉鉱石を回収した後、該粉
鉱石を前記溶融還元炉に加圧送給することを特徴とする
。In order to achieve the objective, the exhaust gas treatment method of the present invention sucks the exhaust gas discharged from the smelting reduction furnace through a solid-gas separator through a flue, and the gas temperature in the middle of the flue is 600. Fine ore is supplied into the exhaust gas at a temperature of 40% or higher and a CO concentration of 40% or higher, carried along with the flow of the exhaust gas, subjected to preliminary reduction, and separated from the exhaust gas by the solid-gas separator to produce fine ore. After recovering the ore powder, the ore powder is fed under pressure to the melting reduction furnace.
このとき、煙道内界囲気のｃｏｄ度が４０％未満の場合
には、その煙道内に粉炭、ＣＯ、コークス等の炭素系又
は炭化水素系還元材を吹き込むことが好ましい。At this time, if the cod degree of the surrounding air in the flue is less than 40%, it is preferable to blow a carbon-based or hydrocarbon-based reducing agent such as powdered coal, CO, or coke into the flue.
また、この方法を実施するための排ガス処理装置は、溶
融還元炉に付設した排ガスフードと固気分離器とを煙道
を介して直結し、該煙道の途中に粉鉱石供給用のノズル
を配置し、且つ固気分離器にて排ガスから分離された粉
鉱石を回収し、その後排ガスは吸引ファンにより吸引排
出されると共に、前記粉鉱石を溶融還元炉に加圧送給す
る配管を前記固気分離器と前記溶融還元炉との間に設け
たことを特徴とする。In addition, the exhaust gas treatment device for carrying out this method directly connects the exhaust gas hood attached to the smelting reduction furnace and the solid-gas separator via a flue, and a nozzle for supplying fine ore is installed in the middle of the flue. The fine ore separated from the exhaust gas by the solid-gas separator is recovered, and the exhaust gas is then sucked and discharged by a suction fan, and the pipe for supplying the fine ore under pressure to the smelting reduction furnace is connected to the solid-gas separator. It is characterized in that it is provided between the separator and the melting reduction furnace.
以下、図面に示した実施例により、本発明の特徴を具体
的に説明する。Hereinafter, features of the present invention will be specifically explained with reference to embodiments shown in the drawings.
第１図は、本実施例の排ガス処理装置の全体を示す概略
図である。FIG. 1 is a schematic diagram showing the entire exhaust gas treatment apparatus of this embodiment.
本実施例における溶融還元炉本体１は、横型いわゆる混
銑炉型の炉体をもち、その円筒型炉体の軸は水平となっ
ており、回転機構２上に載置されている。なお、この溶
融還元炉本体ｌは、混銑炉型に拘束されるものではなく
、転炉型、シャフト炉型等の他の形式のものであっても
良い。そして、たとえば転炉型の溶融還元炉を使用する
場合には、図示した回転機構２に代えてトラニオン軸に
よる傾転機構が使用される。The smelting reduction furnace main body 1 in this embodiment has a horizontal so-called mixed pig iron furnace type furnace body, the axis of the cylindrical furnace body is horizontal, and is placed on a rotating mechanism 2. Note that the smelting reduction furnace main body l is not limited to the mixed pig iron furnace type, but may be of other types such as a converter type or a shaft furnace type. For example, when a converter-type melting reduction furnace is used, a tilting mechanism using a trunnion shaft is used in place of the illustrated rotating mechanism 2.
溶融還元炉本体１の下部には、溶湯浴中にガスを吹き込
むための浸漬羽口３が、炉の長手方向に関して複数個配
列されている。これら浸漬羽口３からは、酸素、不活性
ガス等が吹き込まれる。また、それらをキャリアガスと
して、粉鉱石を吹き込むことができる。A plurality of immersion tuyeres 3 for blowing gas into the molten metal bath are arranged in the lower part of the melting reduction furnace body 1 in the longitudinal direction of the furnace. Oxygen, inert gas, etc. are blown into these immersion tuyeres 3. Moreover, fine ore can be blown into the carrier gas.
また、溶融還元炉本体１の上部には、上吹きランス４を
炉内に挿入するための開口５が設けられている。この上
吹きランス４は、混銑炉型の溶融還元炉本体１の場合に
は軸方向長さに応じて複数個配列されるものであり、そ
れに対応して開口５が炉体上部に穿設されている。また
、上吹きランス４からの吹錬酸素に随伴させて、粉鉱石
を炉内に吹き込むこともできる。Furthermore, an opening 5 for inserting the top blowing lance 4 into the furnace is provided in the upper part of the melting reduction furnace main body 1. In the case of a mixed pig iron furnace type smelting reduction furnace body 1, a plurality of these top blow lances 4 are arranged according to the axial length, and corresponding openings 5 are bored in the upper part of the furnace body. ing. Further, fine ore can also be blown into the furnace together with blowing oxygen from the top blowing lance 4.
この溶融還元炉本体１を使用して溶融還元を行うとき、
多量の排ガスが発生する。この排ガスＡは、炉内に吹き
込まれた粉鉱石、粉炭等の微粒子を伴って炉外に放出さ
れる。また、溶融還元炉本体１から排出される排ガスＡ
は、製錬条件にもよるが１６００℃〜１８００℃と極め
て高温状態にあり、Ｃ０成分を多量に含むものである。When performing melt reduction using this melt reduction furnace main body 1,
A large amount of exhaust gas is generated. This exhaust gas A is discharged to the outside of the furnace together with fine particles such as fine ore and powdered coal blown into the furnace. In addition, exhaust gas A discharged from the smelting reduction furnace main body 1
Although it depends on the smelting conditions, it is in an extremely high temperature state of 1600°C to 1800°C and contains a large amount of C0 component.
そこで、この排ガスＡを、開口５近傍に配置した排ガス
フード６で集め、煙道７−１に導く。煙道７−１は固気
分離器８に連結されているので、排ガスＡは、微粒子を
浮遊させたままで固気分離器８に送り込まれる。この固
気分離器８としては、サイクロン１．低速度除塵器等が
使用される。Therefore, this exhaust gas A is collected by an exhaust gas hood 6 disposed near the opening 5 and guided to the flue 7-1. Since the flue 7-1 is connected to the solid-gas separator 8, the exhaust gas A is sent to the solid-gas separator 8 with fine particles suspended therein. As this solid-gas separator 8, a cyclone 1. A low speed dust remover etc. is used.
この煙道７−１の途中には、粉鉱石Ｂを供給するための
粉鉱石用ノズル９が設けられている。この粉鉱石用ノズ
ル９から吸引又は吹き込まれた粉鉱石Ｂは、排ガスへの
流れに乗って固気分離器８に搬送される。この搬送の過
程で、粉鉱石Ｂは、排ガスＡと充分に接触して受熱し、
また排ガスに含まれているＣＯ成分によって予備還元さ
れる。このとき、排ガスへの温度が６００〜１８００℃
であり、ＣＯ濃度が４０〜９９％であるので、粉鉱石Ｂ
の予備還元及び予熱は充分に行われる。なお、ＣＯａ度
がこれより低いような場合、粉炭、ＣＯ等の還元材を還
元材用ノズル１０から煙道７−１内に供給し、煙道７−
１内雰囲気のＣＯ濃度を４０％以上となるように調節す
る。このため、煙道７−１内に適宜のＣＯ濃度計（図示
せず）を設け、それによる検出値に基づいて還元材用ノ
ズル１０を作動させると良い。A fine ore nozzle 9 for supplying fine ore B is provided in the middle of this flue 7-1. The fine ore B sucked or blown from the fine ore nozzle 9 is conveyed to the solid-gas separator 8 along with the flow of exhaust gas. During this transportation process, fine ore B comes into sufficient contact with exhaust gas A and receives heat.
It is also preliminarily reduced by the CO component contained in the exhaust gas. At this time, the temperature of the exhaust gas is 600 to 1800℃
Since the CO concentration is 40 to 99%, fine ore B
Preliminary reduction and preheating of is carried out sufficiently. Note that if the COa degree is lower than this, a reducing agent such as powdered coal or CO is supplied into the flue 7-1 from the reducing agent nozzle 10, and the flue 7-
Adjust the CO concentration in the atmosphere inside 1 to 40% or more. For this reason, it is preferable to provide an appropriate CO concentration meter (not shown) in the flue 7-1 and operate the reducing agent nozzle 10 based on the detected value.
このようにして予備還元・予熱された粉鉱石Ｂは、溶融
還元炉本体１から飛散した粉塵と共に、固気分離器８に
より排ガスＡから分離され、固気分離器８の下部に蓄え
られる。本実施例においては、この固気分離器は、２段
配置されている。したがって、第１０固気分離器８とし
て、煙道７−１の流路断面積が急に広がるような内容積
をもち、煙道７−１と固気分離器８との間に急激な流速
低下を生じさせ、それによって粉鉱石等が落下するよな
節屯な構造のものを使用することができる。The fine ore B prereduced and preheated in this manner is separated from the exhaust gas A by the solid-gas separator 8 together with the dust scattered from the smelting reduction furnace main body 1, and stored in the lower part of the solid-gas separator 8. In this embodiment, the solid-gas separator is arranged in two stages. Therefore, the tenth solid-gas separator 8 has an internal volume such that the flow passage cross-sectional area of the flue 7-1 suddenly expands, and a rapid flow rate between the flue 7-1 and the solid-gas separator 8. It is possible to use a structure with a narrow structure that causes a drop and thereby allows powder ore, etc. to fall.
また、煙道７−１を固気分離器８の接線方向に取り付け
ることにより、いわゆるサイクロン分離器を使用するこ
ともできる。Moreover, by attaching the flue 7-1 in the tangential direction of the solid-gas separator 8, a so-called cyclone separator can also be used.
固気分離器８を通過した排ガスＡは、煙道７−２を経て
第２の固気分離器１２に送られる。そして、第２の固気
分離器１２では、依然として排ガス八に浮遊している比
較的粒度の小さい粉鉱石等を分離する。分離された粉鉱
石等は第２の固気分離器１２の下部に溜り、他方の排ガ
スＡは、更に煙道７−３を経由して集塵器１４に送り込
まれる。The exhaust gas A that has passed through the solid-gas separator 8 is sent to the second solid-gas separator 12 via the flue 7-2. Then, in the second solid-gas separator 12, relatively small-sized powder ore and the like still floating in the exhaust gas are separated. The separated fine ore etc. accumulate in the lower part of the second solid-gas separator 12, and the other exhaust gas A is further sent to the dust collector 14 via the flue 7-3.
この排ガスフード６から第２の固気分離器１２に至る経
路で、排ガス八と粉鉱石Ｂとの接触が充分に行われ、且
つ、煙道により吸熱され、それに伴って、排ガスへの温
度が３００℃以下に低下するので、この排ガスＡは、た
とえばバグフィルタ−等の乾式集塵機により処理するこ
とが可能な状態となる。したがって、従来、冷却能力の
大きいベンチニリースクラバ等の湿式集塵装置を高温排
ガス用として多用していたが、それを使わずにすむため
設備費の削減と集塵水による二次公害を回避することが
できる。このようにして除塵された排ガスＡは、排ガス
ファン１５によって吸引され、ガスホルダー１６に蓄え
られ、また、貯蔵しないときは放散塔１７を経由して系
外に放出される。In the route from the exhaust gas hood 6 to the second solid-gas separator 12, sufficient contact between the exhaust gas 8 and the fine ore B occurs, and heat is absorbed by the flue, and the temperature of the exhaust gas decreases accordingly. Since the temperature is lowered to 300° C. or lower, the exhaust gas A is in a state where it can be treated with a dry dust collector such as a bag filter. Therefore, conventionally, wet dust collectors such as ventilary scrubbers with large cooling capacity have been frequently used for high-temperature exhaust gas, but since this is no longer necessary, equipment costs can be reduced and secondary pollution caused by collected dust water can be avoided. be able to. The exhaust gas A from which dust has been removed in this manner is sucked by an exhaust gas fan 15 and stored in a gas holder 16, and is discharged outside the system via a diffusion tower 17 when not stored.
このガスホルダー１６に蓄えられた排ガスＡは、一つの
実施例として配管１８を経由してブースター２５により
昇圧されて送り出され、固気分離器８゜１２で分離され
た粉鉱石、粉塵等を溶融還元炉本体１に向けて搬送する
キャリアガスとして使用することもできる。すなわち、
固気分離器８．１２の下部に溜まった粉鉱石、粉塵等は
、切出し装置１９−１゜１９−２を経由して落下し、エ
ジェクター２０−１．２０−２によりガスホルダー１６
から配管１８を経てブースター２５により昇圧されて送
られてくる排ガスＡに乗って、受入れタンク２６に搬送
される。そして、受入れタンク２６より切出し装置２７
を介してブロータンク２１に切り出され、このブロータ
ンク２１には、同様にガスホルダー１６よりの配管１８
が接続されており、ブロータンク２１より溶湯に浸漬さ
れた浸漬羽口３を経て溶融還元炉本体ｌ内の溶融金属浴
内に吹き込まれる。及び／又は上吹きランス４を経て上
方から溶融金属浴表面に吹き付けられる。In one embodiment, the exhaust gas A stored in the gas holder 16 is boosted in pressure by a booster 25 via a pipe 18 and sent out, melting ore powder, dust, etc. separated by a solid-gas separator 8.12. It can also be used as a carrier gas to be transported toward the reduction furnace main body 1. That is,
Powdered ore, dust, etc. accumulated at the bottom of the solid-gas separator 8.12 fall through the cutting devices 19-1 and 19-2, and are sent to the gas holder 16 by the ejector 20-1 and 20-2.
The exhaust gas A is boosted in pressure by the booster 25 and sent through the piping 18, and is transported to the receiving tank 26. Then, the cutting device 27 is removed from the receiving tank 26.
The pipe 18 from the gas holder 16 is also connected to the blow tank 21 through the gas holder 16.
is connected to the blow tank 21, and is blown into the molten metal bath in the melting reduction furnace main body l through the immersion tuyere 3 immersed in the molten metal. and/or sprayed from above onto the surface of the molten metal bath via the top blowing lance 4.
このようにして、排ガスＡの還元能及び保有熱を粉鉱石
Ｂの予備還元及び予熱に直接使用することにより、予備
還元装置や予熱装置等の付帯設備を必要とすることなく
、粉鉱石Ｂを溶融還元に好ましい状態（例えば予備還元
率１０〜６０％）に調整することができる。また、排ガ
スＡ自体も乾式集塵が可能な状態にまで降温されるので
、集塵設備が簡単となる。In this way, by directly using the reducing ability and retained heat of the exhaust gas A for preliminary reduction and preheating of fine ore B, fine ore B can be converted to fine ore B without the need for incidental equipment such as a preliminary reduction device or a preheating device. It can be adjusted to a state preferable for melt reduction (for example, preliminary reduction rate of 10 to 60%). Moreover, since the temperature of the exhaust gas A itself is lowered to a state where dry dust collection is possible, the dust collection equipment becomes simple.
なふ、溶融還元炉本体１から排出される排ガスへの熱量
は、予備処理される粉鉱石Ｂの必要装入量を大幅に上回
る場合が多い。このようなときには、煙道７−１に排熱
回収機構を設け、排ガスＡの熱を有効に回収することが
望ましい。第１図に示した例においては、この排熱回収
機構としてボイラーシステム２２を採用している。すな
わち、排ガスフード６、煙道？−１を水冷構造とし、配
管２３を介して給水し、煙道７−１よりの高温排水を配
管２４によりボイラーシステム２２に導き、排ガスＡの
熱をスチームを発生させることにより回収し、蒸気その
もの、もしくは発電用として利用することができる。こ
の構成は固気分離器８，１２及び煙道７−２．７−３等
を水冷化した場合も同様に適用できる。In many cases, the amount of heat given to the exhaust gas discharged from the smelting reduction furnace main body 1 greatly exceeds the required charging amount of fine ore B to be pretreated. In such a case, it is desirable to provide an exhaust heat recovery mechanism in the flue 7-1 to effectively recover the heat of the exhaust gas A. In the example shown in FIG. 1, a boiler system 22 is employed as this exhaust heat recovery mechanism. In other words, exhaust gas hood 6, flue? -1 has a water-cooled structure, water is supplied through piping 23, high-temperature waste water from flue 7-1 is guided to boiler system 22 through piping 24, heat of exhaust gas A is recovered by generating steam, and the steam itself is Alternatively, it can be used for power generation. This configuration can be similarly applied when the solid-gas separators 8, 12, the flue 7-2, 7-3, etc. are water-cooled.
第２図は、排ガスのＣ０１１度及び温度が粉鉱石の予備
還元に与える影響を示したグラフである。この図におい
ては、排ガスのＣＯａ度１００％で排ガス温度１２００
℃での予備還元能力を１．０として、これに対する比較
値を縦軸の予備還元率として表している。この図から明
らかなように、排ガスによる粉鉱石の予備還元は、ＣＯ
ａ度の増加と共に向上している。しかしながら、排ガス
温度が６００℃未満の比較的低温の場合には、予備還元
率の増加は僅かなものである。ところが、排ガス温度が
６００℃以上の領域になると、たとえば８００℃の線に
みられるようにＣＯ濃度４０％を境として予備還元率は
急激に大きくなる。これは、次の理由によるものと考え
られる。FIG. 2 is a graph showing the influence of exhaust gas C011 degrees and temperature on preliminary reduction of fine ore. In this figure, the COa degree of the exhaust gas is 100% and the exhaust gas temperature is 1200%.
The preliminary reduction capacity at °C is assumed to be 1.0, and the comparison value with respect to this is expressed as the preliminary reduction rate on the vertical axis. As is clear from this figure, the preliminary reduction of fine ore by exhaust gas is CO
It improves as the a degree increases. However, when the exhaust gas temperature is relatively low, below 600° C., the increase in the preliminary reduction rate is small. However, when the exhaust gas temperature reaches a region of 600° C. or higher, the preliminary reduction rate increases rapidly with the CO concentration reaching 40%, as shown by the 800° C. line, for example. This is considered to be due to the following reasons.
すなわち、６００℃以上の高温になると還元反応の速度
ならびに鉱石粒子内部の酸素の拡散が促進されるためで
ある。またＣｏａ１度が４０％以下では平衡論的な観点
からも還元反応が進みにくい。That is, this is because a high temperature of 600° C. or higher accelerates the reduction reaction rate and the diffusion of oxygen inside the ore particles. Further, when the Coa1 degree is 40% or less, the reduction reaction is difficult to proceed from an equilibrium viewpoint.
本実施例においては、この排ガスの温度及びＣＯ濃度が
粉鉱石の予備還元に与える影響を積極的に利用し、粉鉱
石の予備還元を効果的に行うものである。In this embodiment, the influence of the temperature and CO concentration of the exhaust gas on the preliminary reduction of the fine ore is actively utilized to effectively perform the preliminary reduction of the fine ore.
ただし、排ガスの温度が１６００℃を超えるようになる
と、粉鉱石のスティッキングが生じ、煙道７−１もしく
は固気分離器８．１２内で融着し、排出が極めて困難に
なる。そこで、排ガスＡの温度が過度に高い場合には、
煙道７−１内の適宜の個所に冷却用の空気取入れ口を設
け、排ガスへの温度を調節することが好ましい。However, when the temperature of the exhaust gas exceeds 1600° C., sticking of the fine ore occurs and fuses within the flue 7-1 or the solid-gas separator 8.12, making it extremely difficult to discharge. Therefore, if the temperature of exhaust gas A is excessively high,
It is preferable to provide a cooling air intake at an appropriate location within the flue 7-1 to adjust the temperature of the exhaust gas.
また、この粉鉱石を溶融還元炉本体１に装入するとき、
切出し装置１９−１．１９−２より熱間で切り出し、受
入れタンク２６で熱間で貯蔵し、ブロータンク２１より
熱間で吹き込むことが可能であり、例えばブロータンク
２１より５００ ℃以下の温度にて浸漬羽口３を介して
浴中に吹込むことにより、炉内の温度低下を来すことな
く、円滑な溶融還元が可能な極めて合理的な方法及び装
置を提供するものである。Moreover, when charging this fine ore into the smelting reduction furnace main body 1,
It is possible to cut hot from the cutting device 19-1, 19-2, store hot in the receiving tank 26, and blow hot from the blow tank 21. The present invention provides an extremely rational method and apparatus that enables smooth melting and reduction without causing a temperature drop in the furnace by blowing the melt into the bath through the immersion tuyere 3.
第３図は、本実施例の効果を更に高めた第２の実施例を
示す全体概略図である。FIG. 3 is an overall schematic diagram showing a second embodiment that further enhances the effects of this embodiment.
第２の実施例においては、第１の実施例に比較して更に
粉鉱石と排ガスの接触時間を大幅に長くすることが可能
となる構造を採用している。In the second embodiment, a structure is adopted which makes it possible to significantly lengthen the contact time between the fine ore and the exhaust gas compared to the first embodiment.
すなわち、粉鉱石Ｂは、第２の固気分離塔１２と第３の
固気分離器１３とを連結する煙道７−３に設けられた粉
鉱石用ノズル９−３から煙道７−３内に吸引されて、こ
の煙道７−３を通って第３の固気分離器１３に送られる
。固気分離器８．１２．１３は、共にサイクロン分離器
となっており、内部で旋回流となった粉鉱石Ｂは還元性
の排ガスと充分な接触時間をもって接触し、還元反応及
び予熱が充分に行われた後、下部に堆積する。第３の固
気分離器１３内に堆積した粉鉱石は、切出し装置１９−
３を経由して送鉱管１１−１を通って、第１の固気分離
器８と第２の固気分離器１２との間にある煙道７−２内
に、粉鉱石用ノズル９−２を介して吸引される。That is, the fine ore B is passed from the fine ore nozzle 9-3 provided in the flue 7-3 connecting the second solid-gas separation tower 12 and the third solid-gas separator 13 to the flue 7-3. The gas is sucked into the air and sent to the third solid-gas separator 13 through this flue 7-3. The solid-gas separators 8, 12, and 13 are all cyclone separators, and the fine ore B, which has become a swirling flow inside, comes into contact with the reducing exhaust gas for a sufficient contact time, and the reduction reaction and preheating are sufficient. After that, it is deposited at the bottom. The fine ore deposited in the third solid-gas separator 13 is removed from the cutting device 19-
A fine ore nozzle 9 is inserted into the flue 7-2 between the first solid-gas separator 8 and the second solid-gas separator 12 through the ore feed pipe 11-1 via the -2.
ここで、煙道７−２内では排気流が上昇しているため、
粉鉱石は、その気流によって搬送され、第２の固気分離
器１２の中に入る。そして、２回目の旋回流となって、
ここでも充分な還元反応及び予熱が行われる接触時間を
得ることができる。Here, since the exhaust flow is rising in the flue 7-2,
The fine ore is carried by the air flow and enters the second solid-gas separator 12. Then, there is a second swirling flow,
Here, too, a sufficient contact time for reduction reaction and preheating can be obtained.
更に、切出し装置１９−２から排出された粉鉱石は送鉱
管１１−２を通って（点線のルート）粉鉱石用ノズル９
−１に送られ、そこから煙道７−１内に吸引される。Further, the fine ore discharged from the cutting device 19-2 passes through the ore feed pipe 11-2 (route indicated by a dotted line) and is passed through the fine ore nozzle 9.
-1, and is sucked into the flue 7-1 from there.
更に、粉鉱石は、煙道７−１を通って第１の固気分離器
８に入り、そこで更に高温、高還元性の排ガスと共に旋
回流となった後、固気分離器８の下部に堆積し、切出し
装置１９−’１を介してエジェクター２０−１によって
受入れタンク２６に圧送される。Furthermore, the fine ore enters the first solid-gas separator 8 through the flue 7-1, where it becomes a swirling flow together with the high-temperature, highly reducing exhaust gas, and then flows into the lower part of the solid-gas separator 8. It is deposited and pumped into the receiving tank 26 by the ejector 20-1 via the cutting device 19-'1.
それ以降の動きは、第１の実施例と同様であるから、重
複を避けるため説明を省略する。しかし、同様の構成と
応用ができることは勿論である。Since the subsequent operations are similar to those in the first embodiment, the explanation will be omitted to avoid duplication. However, it goes without saying that similar configurations and applications can be made.
この第２の実施例によると、粉鉱石は、煙道７−１．
７−２． ７−３で排ガスに触れるだけでなく、固気分
離器１３．１２． ８を順次通過することになる。According to this second embodiment, the fine ore is transferred to the flue 7-1.
7-2. 7-3, as well as the solid-gas separator 13.12. 8 will be passed one after another.
したがって、長時間排ガスと接触することが可能になり
、充分な予備還元及び予熱が行われる。このことは、予
備還元率を高めることができるために、溶融還元炉の排
ガス処理装置を兼用しても、充分に還元能力及び予熱能
力を持たせることができる方法を提供することが可能と
なることを意味する。Therefore, it becomes possible to contact the exhaust gas for a long time, and sufficient preliminary reduction and preheating is performed. This makes it possible to increase the preliminary reduction rate, making it possible to provide a method that can provide sufficient reduction ability and preheating ability even if the exhaust gas treatment device of the smelting reduction furnace is also used. It means that.
また、本実施例は、固気分離器８．１２．１３を３基直
列に連結したものであるが、４基以上を直列に連結して
も良く、また設備の簡略化のために２基を直列に連結し
ても良いことは勿論である。たとえば、２基直列のケー
スでは、粉鉱石Ｂのノズル９は、煙道７−２に設けられ
、第３の固気分離器１３は省略され、煙道７−３は集塵
機１４の入側に直接接続されることになる。Additionally, in this embodiment, three solid-gas separators 8.12.13 are connected in series, but four or more may be connected in series, or two solid-gas separators 8.12.13 may be connected in series to simplify the equipment. Of course, they may be connected in series. For example, in the case of two units in series, the nozzle 9 for fine ore B is provided in the flue 7-2, the third solid-gas separator 13 is omitted, and the flue 7-3 is located on the inlet side of the dust collector 14. It will be directly connected.
以上に説明したように、本発明においては、溶融還元炉
から排出される排ガスを固気分離器に導く煙道内で粉鉱
石と接触させることにより、排ガスの還元能及び保有熱
を溶融還元炉に装入される粉鉱石の予備還元及び予熱に
利用している。そのため、大がかりな独立した予備還元
設備や予熱装置等の付帯設備を必要とすることなく、溶
融還元炉の排ガス処理装置を兼用して粉鉱石を溶融還元
に好適な状態とすることができ、また排ガスにより持ち
出される粉鉱石、粉炭等の有価物及び熱の回収も行われ
る。更には、粉鉱石によって排ガスの温度が下げられる
ので、排ガスに対する除塵処理が容易となる。このこと
は、バックフィルター等の乾式集塵機を使用することが
できるため、水処理等に伴う二次公害を防止する上で更
に好ましく、また、設備費も安価とすることができる。As explained above, in the present invention, by bringing the exhaust gas discharged from the smelting reduction furnace into contact with fine ore in the flue leading to the solid-gas separator, the reducing ability and retained heat of the exhaust gas is transferred to the smelting reduction furnace. It is used for preliminary reduction and preheating of fine ore to be charged. Therefore, it is possible to use the flue gas treatment equipment of the smelting reduction furnace to bring the fine ore into a state suitable for smelting reduction, without requiring large-scale independent preliminary reduction equipment or incidental equipment such as preheating equipment. Valuable materials such as fine ore and powdered coal, as well as heat, carried out by the exhaust gas are also recovered. Furthermore, since the temperature of the exhaust gas is lowered by the fine ore, the dust removal process for the exhaust gas becomes easier. This is more preferable in terms of preventing secondary pollution caused by water treatment, etc., since a dry dust collector such as a back filter can be used, and equipment costs can also be reduced.
このように、本発明によるとき、溶融還元により副生じ
た熱の有効利用が図られると共に、原料を無駄に消費す
ることのない溶融還元を簡単な設備により実施すること
が可能となる。As described above, according to the present invention, it is possible to effectively utilize the heat generated as a by-product of melting reduction, and to carry out melting reduction without wasteful consumption of raw materials using simple equipment.
第１図は本発明実施例の設備配置を概略的に示す図であ
り、第２図は排ガスによる粉鉱石の予備還元効果を示す
グラフで、排ガスのＣＯ濃度１００ ％で排ガス温度１
２００℃での予備還元能力を１．０ として比較値を示
したグラフであり、第３図は本発明の効果を更に高めた
第２の実施例を示す全体概略図である。Fig. 1 is a diagram schematically showing the equipment layout of an embodiment of the present invention, and Fig. 2 is a graph showing the preliminary reduction effect of fine ore by exhaust gas, where the CO concentration of the exhaust gas is 100% and the exhaust gas temperature is 1.
This is a graph showing comparative values assuming a preliminary reduction capacity of 1.0 at 200° C., and FIG. 3 is an overall schematic diagram showing a second embodiment in which the effects of the present invention are further enhanced.
Claims (1)
固気分離器を通して吸引すると共に、前記煙道の途中の
ガス温度６００℃以上で且つＣＯ濃度が４０％以上の該
排ガス中に粉鉱石を供給し、該吸引排ガスの流れに乗せ
て搬送すると共に予備還元を行い、且つ前記固気分離器
により排ガスから分離することにより粉鉱石を回収した
後、該粉鉱石を前記溶融還元炉に加圧送給することを特
徴とする溶融還元炉からの吸引排ガスを用いた粉鉱石の
予備還元方法。 ２、特許請求の範囲第１項記載の煙道に設けた還元材吹
込みノズルから還元材を吸引させ、煙道内雰囲気のＣＯ
濃度を４０％以上に調整することを特徴とする溶融還元
炉からの吸引排ガスを用いた粉鉱石の予備還元方法。 ３、溶融還元炉に付設した排ガスフードと固気分離器と
を煙道を介して直結し、該煙道の途中に粉鉱石供給用の
ノズルを配置し、且つ固気分離器にて排ガスから分離さ
れた粉鉱石を回収し、その後排ガスは吸引ファンにより
吸引排出されると共に、前記粉鉱石を溶融還元炉に加圧
送給する配管を前記固気分離器と前記溶融還元炉との間
に設けたことを特徴とする溶融還元炉からの吸引排ガス
を用いた粉鉱石の予備還元装置。 ４、特許請求の範囲第３項記載の煙道に、還元材吹込み
ノズルを付設したことを特徴とする溶融還元炉からの吸
引排ガスを用いた粉鉱石の予備還元装置。[Claims] 1. The exhaust gas discharged from the smelting reduction furnace is sucked through a solid-gas separator through a flue, and the gas temperature in the middle of the flue is 600°C or higher and the CO concentration is 40%. Fine ore is supplied into the above exhaust gas, carried along with the flow of the suction exhaust gas, preliminary reduction is performed, and the fine ore is recovered by being separated from the exhaust gas by the solid-gas separator. A method for preliminary reduction of fine ore using suction exhaust gas from a smelting reduction furnace, characterized in that ore is fed under pressure to the smelting reduction furnace. 2. The reducing agent is sucked through the reducing agent injection nozzle provided in the flue as described in claim 1, and the CO in the atmosphere inside the flue is reduced.
A preliminary reduction method for fine ore using suction exhaust gas from a smelting reduction furnace, characterized by adjusting the concentration to 40% or more. 3. The exhaust gas hood attached to the smelting reduction furnace and the solid-gas separator are directly connected via a flue, and a nozzle for supplying fine ore is placed in the middle of the flue, and the solid-gas separator is used to separate the flue gas from the flue gas. A pipe is provided between the solid-gas separator and the smelting-reduction furnace to recover the separated fine ore, and then exhaust gas is suctioned and discharged by a suction fan, and to feed the fine ore under pressure to the smelting-reduction furnace. A preliminary reduction device for fine ore using suction exhaust gas from a smelting reduction furnace. 4. A preliminary reduction device for fine ore using suction exhaust gas from a smelting reduction furnace, characterized in that a reducing agent injection nozzle is attached to the flue according to claim 3.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61-285014 | 1986-11-29 | ||
| JP28501486 | 1986-11-29 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63241125A true JPS63241125A (en) | 1988-10-06 |
Family
ID=17686032
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16456987A Pending JPS63241125A (en) | 1986-11-29 | 1987-06-30 | Method and device for prereduction of fine ore by using exhaust gas sucked from smelting reduction furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63241125A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63140012A (en) * | 1986-12-02 | 1988-06-11 | Nkk Corp | Smelting reduction refining device |
| JPH02209408A (en) * | 1989-02-09 | 1990-08-20 | Nkk Corp | Smelting reduction iron-making method |
| AU722258B2 (en) * | 1996-10-08 | 2000-07-27 | Pohang Iron & Steel Co., Ltd. | Process for injecting metal-oxide-containing fine particles into a reducing gas |
| KR100723223B1 (en) * | 2005-12-23 | 2007-05-29 | 주식회사 포스코 | Pre-reduction method of sintered ore |
| JP2009179820A (en) * | 2008-01-29 | 2009-08-13 | Aisin Takaoka Ltd | Apparatus for recovering vaporized zinc |
| JP2013505356A (en) * | 2009-09-17 | 2013-02-14 | ポスコ | Reduced iron manufacturing apparatus and manufacturing method thereof |
-
1987
- 1987-06-30 JP JP16456987A patent/JPS63241125A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63140012A (en) * | 1986-12-02 | 1988-06-11 | Nkk Corp | Smelting reduction refining device |
| JPH02209408A (en) * | 1989-02-09 | 1990-08-20 | Nkk Corp | Smelting reduction iron-making method |
| AU722258B2 (en) * | 1996-10-08 | 2000-07-27 | Pohang Iron & Steel Co., Ltd. | Process for injecting metal-oxide-containing fine particles into a reducing gas |
| CN1072263C (en) * | 1996-10-08 | 2001-10-03 | 沃斯特－阿尔派因工业设备制造有限公司 | Method for blowing fine particles containing metal oxide into a reducing gas |
| KR100723223B1 (en) * | 2005-12-23 | 2007-05-29 | 주식회사 포스코 | Pre-reduction method of sintered ore |
| JP2009179820A (en) * | 2008-01-29 | 2009-08-13 | Aisin Takaoka Ltd | Apparatus for recovering vaporized zinc |
| JP2013505356A (en) * | 2009-09-17 | 2013-02-14 | ポスコ | Reduced iron manufacturing apparatus and manufacturing method thereof |
| US9783862B2 (en) | 2009-09-17 | 2017-10-10 | Posco | Apparatus for manufacturing reduced iron and method for manufacturing the same |
| US10557179B2 (en) | 2009-09-17 | 2020-02-11 | Posco | Method for manufacturing reduced iron |
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