JPH0788523B2 - Operating method of circulating fluidized bed reduction equipment - Google Patents
Operating method of circulating fluidized bed reduction equipmentInfo
- Publication number
- JPH0788523B2 JPH0788523B2 JP3066849A JP6684991A JPH0788523B2 JP H0788523 B2 JPH0788523 B2 JP H0788523B2 JP 3066849 A JP3066849 A JP 3066849A JP 6684991 A JP6684991 A JP 6684991A JP H0788523 B2 JPH0788523 B2 JP H0788523B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- ore
- dust
- cyclone
- reduction
- 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
Landscapes
- Manufacture Of Iron (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、流動層を形成している
粉状の鉱石中に還元ガスを導入して還元する鉱石の還元
法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for reducing ores in which a reducing gas is introduced into a powdery ore forming a fluidized bed for reduction.
【０００２】[0002]
【従来の技術】かかる還元法の適用例として、部分還元
した鉱石を溶融還元して銑鉄を製造するに当たっての予
備還元があり、例えば、特開昭６２−２３０９１１号公
報、特開平１−１１１８０７号公報に開示されているよ
うに、流動層を形成するライザーの上部側方から平均粒
度が１ｍｍ程度の粉状鉱石を投入し、底部から流動層形
成用のキャリアガスと溶融還元炉からの排ガスを還元用
ガスとして導入し、鉱石の流動層を形成して固気反応に
よって鉱石を還元するに際して、流動層を形成した粒子
と反応気体を流動層の上方かサイクロンを経て排ガスを
除去回収すると共に、粉体はダウンカマーを下降せしめ
てライザーに戻す循環流動層法がある。2. Description of the Related Art As an application example of such a reduction method, there is a pre-reduction in producing pig iron by melting and reducing partially reduced ore, for example, JP-A-62-230911 and JP-A-1-111807. As disclosed in the publication, a powdered ore with an average particle size of about 1 mm is charged from the upper side of a riser forming a fluidized bed, and carrier gas for fluidized bed formation and exhaust gas from a smelting reduction furnace are fed from the bottom. Introduced as a reducing gas, when reducing the ore by forming a fluidized bed of ore and a solid-gas reaction, the particles forming the fluidized bed and the reaction gas are removed and recovered from the upper part of the fluidized bed or through a cyclone to remove the exhaust gas, For the powder, there is a circulating fluidized bed method in which the downcomer is lowered and returned to the riser.
【０００３】[0003]
【発明が解決しようとする課題】この流動層において
は、原料鉱石粒子同士が衝突して粉化し、２０μｍ以下
の多量の微粉状ダストが発生する。このサイクロンの捕
集能を越えて排ガス中に含まれるダストの発生は還元装
置の操業効率を低下させるばかりでなく、還元および熱
効率の低下によりエネルギー原単位を押し上げることに
なる。BRIEF Problem to be Solved] In the fluidized bed, ore grains collide with powdered, 20 [mu] m or less under
A large amount of fine powder dust is generated. The generation of dust contained in the exhaust gas beyond the collection ability of the cyclone not only lowers the operation efficiency of the reduction device, but also increases the energy consumption rate by reduction of reduction and thermal efficiency.
【０００４】本発明において解決すべき課題は、かかる
循環流動還元における原料鉱石の微粉化による問題を解
消するための手段を見出すことにある。[0004] The problem to be solved in the present invention is to find means for solving the problem caused by atomization of the raw material ore in such circulating fluidized reduction.
【０００５】[0005]
【課題を解決するための手段】本発明は、流動層におけ
る原料鉱石の微粉化の態様に対する知見を得、これを循
環流動還元における反応効率の向上に積極的に利用する
ことによってその課題を解決したもので、流動層におけ
る粉状鉱石中の微粉の構成割合を一定にすることによっ
て上記課題を解決した。Means for Solving the Problems The present invention solves the problem by obtaining knowledge about the mode of pulverization of a raw material ore in a fluidized bed and positively utilizing it for the improvement of reaction efficiency in circulating fluidized reduction. in which the solved the above problems by the composition ratio of the fine powdery ore in the flow Doso constant.
【０００６】すなわち本発明は、循環流動装置のライザ
ーの上方から排出される還元された原料鉱石をサイクロ
ンで捕集した後、サイクロンからの排ガスに含まれた２
０μｍ以下の微粉状ダストを高温集塵装置で捕集し、前
記微粉状ダストをダウンカマー下部に戻すことにより、
ライザー中の流動層鉱石に含まれる２０μｍ以下の微粉
を２〜７重量％に調整することを特徴とする循環流動層
還元装置の操業方法である。 That is, the present invention relates to a riser for a circulating fluidizer.
Cyclone of the reduced raw material ore discharged from above
2 contained in the exhaust gas from the cyclone after being collected by
Before collecting fine powder dust of 0 μm or less with a high temperature dust collector,
By returning the fine powder dust to the bottom of the downcomer,
Fine powder of 20 μm or less contained in the fluidized bed ore in the riser
Of 2 to 7% by weight for circulating fluidized bed
It is a method of operating the reduction device.
【０００７】反応流動層を形成する粉鉱石の粒度構成に
おいて、２０μｍ以下の微粉の粒度構成量は、流動層の
操業条件にもよるが、平均粒度が０．１〜０．５ｍｍの
流動鉱石において、２〜７重量％が良い。[0007] In the particle size configuration of fine ore to form a reaction fluidized bed, the particle size configuration of fines under 20μm or less, depending on the operating conditions of the fluidized bed, the average particle size of 0.1~0.5mm flow ore In, 2 to 7% by weight is preferable.
【０００８】[0008]
【作用】流動層に装入される原料粉鉱石の微粉化は、一
定の粒子構成となるまで急速に進み、その後の微粉化は
極端に遅くなる。そのため、流動層において発生した微
粉が系外に散逸すると流動層内で形成される微粉化は促
進されることになる。The fine powder of the raw powdered ore charged into the fluidized bed rapidly progresses until it has a certain particle structure, and the fine powder thereafter becomes extremely slow. Therefore, when the fine powder generated in the fluidized bed is dissipated outside the system, the pulverization formed in the fluidized bed is promoted.
【０００９】本発明は集塵装置で捕集した微粉を流動層
に戻すことによって、それ以上の微粉化は進行せず、微
粉化に伴うエネルギー原価の増大は回避できる。[0009] The present invention is by returning the dynamic layer flow of fines collected in the dust collector, further micronized does not proceed, increased energy costs associated with the micronization can be avoided.
【００１０】[0010]
【実施例】本発明を溶融還元炉の予備還元に利用した例
について説明する。EXAMPLE An example in which the present invention is used for preliminary reduction in a smelting reduction furnace will be described.
【００１１】図１は本発明を実施するための装置の配置
例を示す。FIG. 1 shows an example of the arrangement of devices for carrying out the present invention.
【００１２】同図において、１はライザーであって、ラ
イザー１の底部から導入されるキャリアガスと次工程の
溶融還元炉からの排ガスから形成される還元ガスによっ
て、その側部上方から投入される原料粉状鉱石２の流動
層を形成する。この流動層における固気反応によって部
分的に還元された原料鉱石は、排出ガスと共にライザー
１の上方から第１のサイクロン３によって捕集されてダ
ウンカマー４を通ってライザー１に戻り、予定の還元状
態になったところでダウンカマー４およびライザー１の
下方の製品注出口５から取り出される。上記の第１のサ
イクロン３から出た排ガスは、更に第２のサイクロン６
を通過し、ここで第１のサイクロン３で捕集できなかっ
たダストは回収循環路７を経由してダウンカマー４に戻
される。さらに、第２のサイクロン６を通過したガス
は、１μｍ程度の微粉の回収能力を有するセラミックス
フィルターを備えた高温集塵装置８によって回収され、
分配装置９で捕集される。通常のダストと排ガスはそれ
ぞれガス排出口１０とダスト排出口１１から排出され
る。この分配装置９に捕集された２０μｍ以下の微粉
は、流動層を形成する粉鉱石の粒度構成の変動に基づい
て、流動層に適宜に供給され、流動層を形成する粉鉱石
の微粉の構成割合を一定にする。In the figure, reference numeral 1 is a riser, which is introduced from above the side portion thereof by a carrier gas introduced from the bottom of the riser 1 and a reducing gas formed from exhaust gas from a smelting reduction furnace in the next step. A fluidized bed of the raw powdery ore 2 is formed. The raw material ore partially reduced by the gas-solid reaction in the fluidized bed is collected together with the exhaust gas from above the riser 1 by the first cyclone 3 and returned to the riser 1 through the downcomer 4 to carry out the planned reduction. When it comes to a state, it is taken out from the product pouring port 5 below the downcomer 4 and the riser 1. The exhaust gas emitted from the first cyclone 3 is further mixed with the second cyclone 6
The dust that could not be collected by the first cyclone 3 is returned to the downcomer 4 via the recovery circulation path 7. Further, the gas that has passed through the second cyclone 6 is recovered by the high temperature dust collector 8 equipped with a ceramics filter having a fine powder recovery capability of about 1 μm,
It is collected by the distributor 9. Normal dust and exhaust gas are discharged from the gas outlet 10 and the dust outlet 11, respectively. Fines of the dispensing device 9 20 [mu] m or less under trapped in, based on the variation of the particle size configuration of fine ore to form a fluidized bed, is supplied suitably to the fluidized bed, the fine powder ore forming the fluidized bed Keep the composition ratio constant.
【００１３】この図１に示す装置を用いて本発明を実施
したところ、以下のような結果を得た。When the present invention was carried out using the apparatus shown in FIG. 1, the following results were obtained.
【００１４】 （１）ライザーに供給される鉱石の粒度構成（網下積算分布；％） 粒子径（ｍｍ） 5 2 1 0.5 0.25 0.125 分布率（％） 100 86 72 51 29 14 （２）還元条件 還元温度 還元ガス組成（％） ガス原単位 製品還元率 ８９０℃ ＣＯ ＣＯ2 Ｈ2 Ｈ2 Ｏ Ｎ2 1.43 Ｎｍ3/Kg 63 ％ 64.7 5.1 24.6 2.7 2.9 （３）サイクロンで捕集された鉱石の粒度構成（網下積算分布；％） ・第１のサイクロン３で捕集された粒子 粒子径（ｍｍ） 5 2 1 0.5 0.25 0.125 0.063 0.044 分布率（％） 100 97 87 80 61 36 16 9 ・第２のサイクロン６に入る粒子 粒子径（μｍ） 200 100 50 20 10 5 2 1.5 分布率（％） 100 98 82 68 41 26 9 2 ・高温集塵装置８に入る粒子 粒子径（μｍ） 200 100 50 20 10 5 2 1.5 分布率（％） 100 97 92 48 23 （４）流動層を形成する微粉の粒度構成 粒子径（ｍｍ） 5 2 1 0.5 0.25 0.125 0.063 0.044 0.020 分布率（％） 100 98 88 81 63 39 19 12 5 （５）その他 本操業は高温集塵装置８で捕集された粒子の一定割合を
戻すことにあるが、本実施例の場合は上に述べた粒度分
布において定常状態が確保された。（高温集塵装置から
戻す量が多すぎれば微粉は系内に蓄積する。また戻す量
が少なすぎればダストとして系外に取り出す量が多くな
る。） （６）結果 系外へのダスト割合を以下で定義する。(1) Particle size composition of ore supplied to the riser (integral distribution under net;%) Particle size (mm) 5 2 1 0.5 0.25 0.125 Distribution rate (%) 100 86 72 51 29 14 (2) Reduction conditions Reduction temperature Reducing gas composition (%) Gas basic unit Product reduction rate 890 ℃ CO CO 2 H 2 H 2 O N 2 1.43 Nm 3 / Kg 63% 64.7 5.1 24.6 2.7 2.9 (3) Particle size of ore collected by cyclone Composition (cumulative distribution under net;%) ・ Particle size captured by the first cyclone 3 Particle size (mm) 5 2 1 0.5 0.25 0.125 0.063 0.044 Distribution rate (%) 100 97 87 80 61 36 16 9 ・ Second Particles entering the cyclone 6 of the particle size (μm) 200 100 50 20 10 5 2 1.5 Distribution rate (%) 100 98 82 68 41 26 9 2 ・ Particle size entering the high temperature dust collector 8 Particle size (μm) 200 100 50 20 10 5 2 1.5 Distribution rate (%) 100 97 92 48 23 (4) Particle size composition of fine powder forming the fluidized bed Particle size (mm) 5 2 1 0.5 0.25 0.125 0.063 0.044 0.02 0 Distribution rate (%) 100 98 88 81 63 39 19 12 5 (5) Others This operation is to return a certain proportion of the particles collected by the high temperature dust collector 8, but in the case of this embodiment, A steady state was ensured in the particle size distribution described in. (If the amount returned from the high-temperature dust collector is too large, the fine powder will accumulate in the system. If the amount returned is too small, the amount taken out of the system as dust will increase.) (6) Results Dust ratio outside the system Defined below.
【００１５】ダスト排出口11からのダスト排出量／（製
品注出口５からの排出量＋ダスト排出口11からのダスト
排出量） ・本実施例 ダスト割合 ２％ ダスト還元率 ６８％ ・比較例（微粉を戻さない場合） ダスト割合 ８％ ダスト還元率 ５８％Dust discharge amount from dust discharge port 11 / (discharge amount from product pouring port 5 + dust discharge amount from dust discharge port 11) -Dust ratio 2% Dust reduction rate 68% -Comparative example ( Dust ratio: 8% Dust reduction ratio: 58%
【００１６】[0016]
【発明の効果】本発明によって、以下の効果を奏する。The present invention has the following effects.
【００１７】（１）予備還元過程での微粉の発生量を少
なくでき、生産効率を上げることができる。(1) It is possible to reduce the amount of fine powder generated in the preliminary reduction process and increase the production efficiency.
【００１８】（２）製品の還元率を上げることができ
る。(2) The reduction rate of the product can be increased.
【００１９】（３）溶融還元炉の予備還元に適用するこ
とによって、エネルギー単価の低減が可能となる。(3) The energy unit price can be reduced by applying it to the preliminary reduction of the smelting reduction furnace.
【図１】本発明を溶融還元炉の予備還元装置として実施
した装置の配列の概要を示す。FIG. 1 shows an outline of the arrangement of an apparatus in which the present invention is implemented as a preliminary reduction apparatus for a smelting reduction furnace.
１ ライザー ２ 原料粉状鉱石 ３ 第１のサイクロン ４ ダウンカマー ５ 製品注出口 ６ 第２のサイクロン ７ 回収循環路 ８ 高温集塵装置 ９ 分配装置 １０ ガス排出口 １１ ダスト排出口 1 riser 2 raw material powdered ore 3 first cyclone 4 downcomer 5 product injection port 6 second cyclone 7 recovery circulation 8 high temperature dust collector 9 distribution device 10 gas outlet 11 dust outlet
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平１−111807（ＪＰ，Ａ) 特開 平３−138308（ＪＰ，Ａ) ─────────────────────────────────────────────────── ─── Continuation of the front page (56) References JP-A-1-111807 (JP, A) JP-A-3-138308 (JP, A)
Claims (1)
される還元された原料鉱石をサイクロンで捕集した後、
サイクロンからの排ガスに含まれた２０μｍ以下の微粉
状ダストを高温集塵装置で捕集し、前記微粉状ダストを
ダウンカマー下部に戻すことにより、ライザー中の流動
層鉱石に含まれる２０μｍ以下の微粉を２〜７重量％に
調整することを特徴とする循環流動層還元装置の操業方
法。1. Discharge from above a riser of a circulating fluidizer.
After collecting the reduced raw material ore by a cyclone,
Fine powder of 20 μm or less contained in exhaust gas from cyclone
The fine dust with a high temperature dust collector, and collect the fine dust.
Flow in the riser by returning to the bottom of the downcomer
2 to 7% by weight of fine powder of 20 μm or less contained in layered ore
A method for operating a circulating fluidized bed reduction apparatus, which is characterized by adjusting .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3066849A JPH0788523B2 (en) | 1991-03-29 | 1991-03-29 | Operating method of circulating fluidized bed reduction equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3066849A JPH0788523B2 (en) | 1991-03-29 | 1991-03-29 | Operating method of circulating fluidized bed reduction equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04301023A JPH04301023A (en) | 1992-10-23 |
| JPH0788523B2 true JPH0788523B2 (en) | 1995-09-27 |
Family
ID=13327709
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3066849A Expired - Lifetime JPH0788523B2 (en) | 1991-03-29 | 1991-03-29 | Operating method of circulating fluidized bed reduction equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0788523B2 (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0723491B2 (en) * | 1987-10-27 | 1995-03-15 | 新日本製鐵株式会社 | Circulating fluidized bed preliminary reduction device |
| JPH0637654B2 (en) * | 1989-10-23 | 1994-05-18 | 川崎製鉄株式会社 | Preliminary reduction method in circulating fluidized bed of powdered ore |
-
1991
- 1991-03-29 JP JP3066849A patent/JPH0788523B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH04301023A (en) | 1992-10-23 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 19960322 |