JPS6039130A - Method for recovering latent heat of waste sintering gas - Google Patents
Method for recovering latent heat of waste sintering gasInfo
- Publication number
- JPS6039130A JPS6039130A JP58146476A JP14647683A JPS6039130A JP S6039130 A JPS6039130 A JP S6039130A JP 58146476 A JP58146476 A JP 58146476A JP 14647683 A JP14647683 A JP 14647683A JP S6039130 A JPS6039130 A JP S6039130A
- Authority
- JP
- Japan
- Prior art keywords
- heat
- exhaust gas
- sintering
- gas
- oxidation
- 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.)
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Links
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、鉄鉱石等の焼結に用いられる焼結機から排出
される焼結排ガスの潜熱回収方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for recovering latent heat from sintering exhaust gas discharged from a sintering machine used for sintering iron ore and the like.
一般に鉄鉱石の焼結に当っては、設備的にも大量生産に
適した焼結機として、第１図に示すような連続式の直線
型ドワイトロイド（ＤＬ）式が採用され稼動している。Generally, when sintering iron ore, a continuous linear Dwight Lloyd (DL) type sintering machine, as shown in Figure 1, is adopted and operated as a sintering machine suitable for mass production in terms of equipment. .
第１図において、１は原料装入口、２は点火炉、３はパ
レットであシ、焼結原料は原料装入口１よりパレット３
上に、装入され、点火炉２にて点火され、パレット上の
焼結原料はパレット３の移動に伴ない成る一定時間（焼
結時間）後焼結反応を完了し、焼結機の他端より矢印に
示す如く排出され、粉砕、冷却後製品焼結鉱として高炉
に装入される。一方パレット３からの焼結排ガスは、メ
ーンブロア−７によシダクト４、生ダクト５を経由して
集塵装置６にて除塵後煙突２１より排出される。これら
排ガスは、圧力制御器１４によって、ダンパー１３を開
閉することによシ制御される構成となっている。尚第２
図は第１図のＡ−Ａ’断面を示すものである。In Fig. 1, 1 is a raw material charging port, 2 is an ignition furnace, 3 is a pallet, and the sintering raw material is fed from the raw material charging port 1 to the pallet 3.
The raw material for sintering on the pallet is charged into the sintering furnace 2, and the sintering raw material on the pallet completes the sintering reaction after a certain period of time (sintering time) as the pallet 3 moves. It is discharged from the end as shown by the arrow, and after being crushed and cooled, it is charged into a blast furnace as a product sintered ore. On the other hand, the sintering exhaust gas from the pallet 3 is removed by a dust collector 6 via a main blower 7, a duct 4, and a raw duct 5, and then discharged from a chimney 21. These exhaust gases are controlled by the pressure controller 14 by opening and closing the damper 13. Furthermore, the second
The figure shows a cross section taken along the line AA' in FIG.
これら鉄鉱石の焼結過程における排ガス成分の変化を焼
結鋼試験結果の１例として示したものが第３図である。FIG. 3 shows changes in exhaust gas components during the sintering process of these iron ores as an example of sintered steel test results.
ｆｉｌ、ｌち焼結原料中のコークスの燃焼は、過剰空気
の存在下で行なわれているが、完全にＣＯ２まで燃焼せ
ず可成ルの濃度のＣＯが存在していることが示されてい
る。The combustion of coke in the sintering raw material is carried out in the presence of excess air, but it has been shown that CO2 is not completely combusted and a considerable concentration of CO2 is present. There is.
これらＤＬ焼結機の排ガス温度は、過剰空気ならびに、
含有水分の影善のため低く、かつ排ガス量は多く、その
排熱の利用回収は行なわれていないのが現状である。The exhaust gas temperature of these DL sintering machines is the excess air and
The amount of exhaust gas is low due to the influence of water content, and the amount of exhaust gas is large, and the current situation is that the exhaust heat is not utilized and recovered.
近時焼結排ガスの脱硝、脱硫対策として排ガス量および
ＮＯｘ、 ＳＯＸ量の低減のため排ガスのカスケード使
用が行なわれている。また特に前記脱硝設備において、
排ガス中のＣＯ酸化熱が一部利用されている。然しなか
ら、これらの方法においては、排ガス全量処理という点
から、排ガス中のＣＯを有効に利用されることは、ＣＯ
＃度が低いためＣＯ酸化による排ガスの温度上昇も小さ
く、熱回収が困難でおるという欠点を有し、かつ排ガス
聞も多いため設備規模も大きくなり、設置スペース、設
備投資も大きくなっている。Recently, as a measure for denitrification and desulfurization of sintering exhaust gas, cascade use of exhaust gas has been carried out to reduce the amount of exhaust gas and the amount of NOx and SOX. In particular, in the denitrification equipment,
Part of the CO oxidation heat in the exhaust gas is utilized. However, in these methods, from the point of view of treating the entire amount of exhaust gas, the effective use of CO in the exhaust gas means that CO
# Since the temperature is low, the temperature rise of the exhaust gas due to CO oxidation is small, making it difficult to recover heat, which is a disadvantage.In addition, since there is a large amount of exhaust gas, the scale of the equipment is large, and the installation space and capital investment are also large.
本発明は斜上の焼結排ガス中のＣＯ含有成分を有効に燃
焼せしめ回収するに当って、従来技術の問題点を解消す
ることを目的としてなされたものである。即ち本発明の
要旨とするところは、焼結排ガス中のＣＯ酸成分、触媒
によシ酸化燃焼させ、熱を回収するに際し、焼結機パレ
ットを区刺し、ＣＯ濃度０．５容量チυ上の排ガスのみ
を触媒による酸化装着に導入し酸化燃焼熱を利用するこ
とを特徴とする焼結排ガスの潜熱回収方法にある。The present invention has been made for the purpose of solving the problems of the prior art in effectively burning and recovering CO-containing components in the inclined sintering exhaust gas. That is, the gist of the present invention is to oxidize and burn the CO acid component in the sintering exhaust gas using a catalyst and recover the heat by partitioning the sintering machine pallet and increasing the CO concentration by 0.5 volume. A method for recovering latent heat from sintering exhaust gas is characterized in that only the exhaust gas is introduced into oxidation equipment using a catalyst and the heat of oxidation combustion is utilized.
次に本発明を実施態様例である図面に基いて述べる。第
４図は本発明の構成を示す模式的説明図である。尚図面
中鎖１図と同じ符号は同じ機能を示すものである。Next, the present invention will be described based on drawings which are embodiment examples. FIG. 4 is a schematic explanatory diagram showing the configuration of the present invention. In the drawings, the same reference numerals as in Figure 1 indicate the same functions.
第４図において、本発明の構成はＣＯ濃度の低いガスを
発生するパレット６をダクト４によシ区側し、これらダ
クト４の排ガスを集合ダクト１１゜ｉ２ｔ １６＊ を
通じてブロワ−１５によりパレットの７−ド１８上に集
合ダクト１７より繰返すこと、これらガスの圧力制御機
器としての１４−１．１４−２ならびにダンパー１３−
２．１３−３． 稀薄ＣＯガスとＣＯ濃度リッチなガス
との仕切シ弁１９゜１９−１．２０．２１． 更に集塵
装置６、メーンブロワ−７、熱交換器８、ＣＯ酸化装置
８、熱回収装置９、及び煙突２１からなる。In FIG. 4, the configuration of the present invention is such that pallets 6 that generate gas with a low CO concentration are separated by ducts 4, and the exhaust gas from these ducts 4 is passed through a collection duct 11゜i2t 16* and used by a blower 15 to remove the pallets from the pallets. 7- repeat from the collective duct 17 on the door 18, 14-1, 14-2 as pressure control equipment for these gases and the damper 13-
2.13-3. Partition valve between dilute CO gas and CO-rich gas 19°19-1.20.21. It further includes a dust collector 6, a main blower 7, a heat exchanger 8, a CO oxidizer 8, a heat recovery device 9, and a chimney 21.
排ガスの流れをより詳しく述べると、まずＣＯ濃度、例
えばＣＯ濃度１．２容ｆｉ（乾ガス基準）チ以下の低い
給鉱部及び排鉱部のガスをブロワ−１５によりパレット
３上のＣＯ濃度リッチ部分に操返す。即ち給鉱部では、
ダクト４→集合ダクト１１→プロワ−１５→集合ダクト
１６→集合ダクト１７→フード１８に、排鉱部では、ダ
クト４→集合ダクト５−１→集合ダクト１２→ブロワ−
１５→集合ダクト１６→集合ダクト１７→フード１８の
ルートを経由しパレット６に燃焼用酸化空気と共に供給
される。ブロワ−１５以降は給鉱部及び排鉱部排ガスは
同一ルートとなる。斯くしてＣＯ濃度の低い排ガスは焼
結焼成のための燃焼空気用として利用され、パレット下
部から排出される排ガス中のＣＯ濃度は高くなる。ＣＯ
濃度の高くなつよ排ガスは各ダクト４−１から生ダクト
５に集められ集塵装置６へ導かれ集塵処理され、次にメ
ーンブロワ−７で昇圧され熱交換器８に導入され熱交換
される。次でＣＯ酸化装着９で排ガス中のＣＯはある割
合で触媒的に接触酸化され、熱回収装置１０に入り熱回
収が行なわれる。熱回収装置１０からの排出ガスには未
だＣＯが残留しておシＣＯ酸化装置９を通し酸化させ熱
交換器８で低温排ガスと熱交換して煙突２１から排出さ
れる。To explain the flow of exhaust gas in more detail, first, the gas from the ore feeding section and the ore discharge section where the CO concentration is low, for example, 1.2 volume fi (dry gas standard) or less, is removed by the blower 15 to reduce the CO concentration on the pallet 3. Return to the rich part. In other words, in the ore supply department,
duct 4 → collection duct 11 → blower 15 → collection duct 16 → collection duct 17 → hood 18; in the ore discharge section, duct 4 → collection duct 5-1 → collection duct 12 → blower
The oxidizing air is supplied to the pallet 6 along with the combustion oxidizing air via the route 15 → collection duct 16 → collection duct 17 → hood 18. After blower 15, the exhaust gas from the ore supply section and the ore discharge section is the same route. In this way, the exhaust gas with a low CO concentration is used as combustion air for sintering, and the CO concentration in the exhaust gas discharged from the lower part of the pallet increases. C.O.
The highly concentrated exhaust gas is collected from each duct 4-1 into a raw duct 5, guided to a dust collector 6, where it is collected, and then pressurized by a main blower 7 and introduced into a heat exchanger 8 for heat exchange. Next, CO in the exhaust gas is catalytically oxidized at a certain rate in a CO oxidation installation 9, and then enters a heat recovery device 10 for heat recovery. The exhaust gas from the heat recovery device 10 still contains CO, which is passed through the CO oxidizer 9 to be oxidized, exchanged heat with the low-temperature exhaust gas in the heat exchanger 8, and then discharged from the chimney 21.
以上のようにＣＯ濃度の低い排ガスをパレット上へ導き
カスケード使用すると焼結排ガス量の削減が図られると
同時にＣＯ濃度も高くな夛、ＣＯリッチな排ガスを接触
酸化することによシ排ガス温度が高められ熱回収率の向
上が図られる。As mentioned above, by guiding the exhaust gas with low CO concentration onto the pallet and using it in a cascade, the amount of sintering exhaust gas can be reduced. This increases the heat recovery rate.
ＣＯの接触酸化は高温排ガスの方が反応が早く実用的で
あるため、スタートするときは予熱炉２２で燃料を焚き
所定温度まで排ガスを予熱する。ＣＯ酸化反応が安定す
れば予熱炉２２は消火する。In the catalytic oxidation of CO, high-temperature exhaust gas reacts faster and is more practical, so when starting, fuel is fired in the preheating furnace 22 to preheat the exhaust gas to a predetermined temperature. When the CO oxidation reaction becomes stable, the preheating furnace 22 is extinguished.
排ガスの圧力コントロールについては焼結焼成過程で焼
結原料層の通過風量はある一定量が必要なため吸引圧力
を一定に制御する必要がある。そのためにはます給鉱側
について集合ダクト１１上の点２６の圧力検出を行ない
圧力制御機器１４−１によってダンパー１３−２の開閉
を行ない吸引量を調節する。また排鉱側についても同様
にダクト１２上の点２４について検出を行ない圧力制御
機器１４−２によってダンパー１６−６の開閉を行ガい
吸引量を調節する。仕切多弁１９．２１は常時閉とし、
仕切弁１９−１．２０は常時開としＣＯ濃度低い排ガス
を集合ダクト１１及び１２に導通可能とする。Regarding the pressure control of the exhaust gas, since a certain amount of air passing through the sintering raw material layer is required during the sintering and firing process, it is necessary to control the suction pressure to a constant value. For this purpose, the pressure at a point 26 on the collecting duct 11 is detected on the ore supply side, and the damper 13-2 is opened and closed by the pressure control device 14-1 to adjust the suction amount. Similarly, on the ore discharge side, the point 24 on the duct 12 is detected, and the pressure control device 14-2 opens and closes the damper 16-6 to adjust the suction amount. Partition valves 19 and 21 are always closed,
The gate valves 19-1 and 20 are always open to allow exhaust gas with a low CO concentration to flow into the collecting ducts 11 and 12.
次にＣＯ濃度例えば０，５容量チ（乾ガス基準）以上の
高い部分の排ガスを分離し熱回収する場合について第５
図に基いて説明する。Next, Section 5 describes the case where exhaust gas with a high CO concentration, for example, 0.5% by volume or more (dry gas standard) is separated and heat recovered.
This will be explained based on the diagram.
パレット中間部のＣＯ濃度が０．５容量−以上ある排ガ
スをダクト４−１に集合し集合ダクト５−２を経由し集
塵装＃６−１に導き除塵稜熱交換器８にて熱交換し酸化
装置９にて触媒により酸化しＣＯガスを燃焼せしめ排熱
回収装置１０にて熱回収する。熱回収後の排ガス中残留
ＣＯガスを酸化袋＃９を通すことにより酸化せしめ熱交
換器８を通し熱交換後ＣＯ濃度の低い排ガスと共に煙突
２１より排気する。尚ＣＯ濃度の高いガスの外圧用とし
てブロワ−１７−１によ勺ガスを導通せしめ、これらガ
スの圧力制御はダクト５−２上の点２５の圧力を検出し
圧力制御器１４−６によりダンパー１３−４を調節し制
御する。Exhaust gas with a CO concentration of 0.5 volume or more in the middle of the pallet is collected in the duct 4-1 and guided to the dust collector #6-1 via the collecting duct 5-2 for heat exchange in the dust removal ridge heat exchanger 8. The CO gas is oxidized by a catalyst in an oxidizer 9, and the CO gas is combusted, and the heat is recovered in an exhaust heat recovery device 10. The remaining CO gas in the exhaust gas after heat recovery is passed through an oxidizing bag #9 to be oxidized, and after heat exchange is passed through the heat exchanger 8 and exhausted from the chimney 21 together with the exhaust gas having a low CO concentration. In addition, a blower 17-1 is used to conduct the external pressure of the gas having a high CO concentration, and the pressure of these gases is controlled by detecting the pressure at a point 25 on the duct 5-2 and controlling the damper by the pressure controller 14-6. 13-4.
ｃｏ酸化において高温即ち４ＤＯ℃以上で反応せしめる
と、その接触酸化反応は迅速に又安定して反応するため
常時酸化製病を常時高温に維持することが必要である。In co-oxidation, when the reaction is carried out at a high temperature, that is, 4DOC or higher, the catalytic oxidation reaction occurs quickly and stably, so it is necessary to maintain the oxidation reaction at a high temperature at all times.
このためＣＯ酸化反応熱の一部をリサイクルして使用す
るために熱交換器か必要である。本発明の熱回収システ
ムの特徴１ｄ、これら機器の配列にあり、第４図及び第
５図に示が本願発明の目的を達成するために好ましい。Therefore, a heat exchanger is required to recycle and use a portion of the CO oxidation reaction heat. The feature 1d of the heat recovery system of the present invention lies in the arrangement of these devices, and the arrangement shown in FIGS. 4 and 5 is preferable for achieving the object of the present invention.
この場合の排ガスの流れはメーンブロワー→貼交換器→
ＣＯ酸化装置→排熱回収装瞳→ＣＯ酸化装置→熱交換器
と々る。この時メーンブロワーは熱交換器と酸化装置の
間、酸化装置と熱回収装置の間或は熱回収装置又は熱交
換器の後に設置してもよい。In this case, the flow of exhaust gas is from main blower → pasting exchanger →
CO oxidizer → exhaust heat recovery pupil → CO oxidizer → heat exchanger. At this time, the main blower may be installed between the heat exchanger and the oxidizer, between the oxidizer and the heat recovery device, or after the heat recovery device or the heat exchanger.
次に実施例について述べる。Next, examples will be described.
実施例
第４図の如き機器配列にてドワイトロイド焼結機の排ガ
ス中のＣＯ酸化熱回収するに当り排熱回収装置として排
熱ボイラーを用い得られた蒸気にて蒸気タービンによる
発電を行なった。その場合の操業成績を次の第１表に示
す。Example: With the equipment arrangement shown in Figure 4, an exhaust heat boiler was used as an exhaust heat recovery device to recover CO oxidation heat from the exhaust gas of the Dwight Lloyd sintering machine, and the resulting steam was used to generate electricity using a steam turbine. . The operational results in that case are shown in Table 1 below.
第１表 操業成績表
第１表に示す如く排ガス量はン２にｃｏ濃度は２％に濃
縮され、ＣＯ酸化装置による燃焼熱によシ有効な熱エネ
ルギーが発電々力として回収された。Table 1: Operational Results As shown in Table 1, the amount of exhaust gas was reduced to 2%, the CO concentration was concentrated to 2%, and effective thermal energy was recovered as power generation power from the combustion heat generated by the CO oxidizer.
第１図は従来のドワイトロイド焼結機の排ガス系統図、
第２図は第１図のＡ−Ａ’断面図、第３図は焼結過程に
おける排ガス成分の変化を示す同第４図は本発明の実施
態様例を示す模式図、第５図は本発明の別な態様を示す
模式図である。
６・・・パレット ４．４−１・・・ダクト、５．５−
１゜５−２ｔ １１，１２，１６，１７・・・集合ダク
ト、６・・・集塵装置、７．１５・・・送風機、 ８・
・・熱交換器９・・・酸化装置、１０・・・熱回収装置
、１３−１゜１３−２．１３−３． 制御弁、１４−１
．１４−２゜１４−３．１４−４、圧力制御装置 １８
１９．フード代理人 弁理士 木 村 三 朗
（り・）’ｇｔｆ乙ａ渾Figure 1 is an exhaust gas system diagram of a conventional Dwight Lloyd sintering machine.
Fig. 2 is a sectional view taken along the line AA' in Fig. 1, Fig. 3 is a schematic diagram showing changes in exhaust gas components during the sintering process, and Fig. 4 is a schematic diagram showing an embodiment of the present invention. FIG. 3 is a schematic diagram showing another embodiment of the invention. 6...Pallet 4.4-1...Duct, 5.5-
1゜5-2t 11, 12, 16, 17... Collection duct, 6... Dust collector, 7.15... Blower, 8.
...Heat exchanger 9...Oxidizer, 10...Heat recovery device, 13-1゜13-2.13-3. Control valve, 14-1
．． 14-2゜14-3.14-4, Pressure control device 18
19. Food Agent Patent Attorney Sanro Kimura (Ri・)'gtf Ota Jun
Claims (3)
させ、熱を回収するに際し、焼結機パレットを区劃し）
ＣＯ濃度０．５容１′−９上の排ガスのみを触媒による
酸化装置に導入し酸化燃焼熱を利用することを特徴とす
る焼結排ガスの潜熱回収方法。(1) When the CO acid component in the sintering exhaust gas is oxidized and burned by a catalyst and the heat is recovered, the sintering machine pallet is separated)
A method for recovering latent heat from sintering exhaust gas, characterized in that only exhaust gas with a CO concentration of 0.5 volume 1'-9 is introduced into an oxidation device using a catalyst and the heat of oxidation combustion is utilized.
、ＣＯ濃度の高いガスを排出するパレット上に繰返し、
焼結燃焼用９気として利用しＣｏ誤贋を高めた後前記酸
化装置に導入することを特徴とする特許請求の範囲第１
項記載の焼結排ガスの潜熱帥１収方法。(2) Repeating pallet exhaust gas that discharges gas with a low CO8 degree onto a pallet that discharges gas with a high CO concentration,
Claim 1, characterized in that Co is introduced into the oxidizer after being used as 9 gas for sintering and combustion to increase Co error.
1. Method for recovering latent heat from sintering exhaust gas as described in Section 1.
より、熱交換器、ＣＯ酸化装置、熱回収装置の順に導通
せしめ、酸化熱を熱回収稜、該熱回収装置の排ガスを前
記ＣＯ酸化装置ならびに前記熱交換器を経由し熱交換後
、煙突よシ排出することを特徴とする特許請求の範囲第
１項記載の焼結排ガスの潜熱回収方法。(3) The exhaust gas charged to the oxidizer is passed through the heat exchanger, the CO oxidizer, and the heat recovery device in this order by a blower, and the oxidation heat is transferred to the heat recovery ridge, and the exhaust gas from the heat recovery device is transferred to the CO oxidizer. 2. The method for recovering latent heat from sintering exhaust gas according to claim 1, further comprising expelling the sintered exhaust gas through a chimney after exchanging heat through the heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58146476A JPS6039130A (en) | 1983-08-12 | 1983-08-12 | Method for recovering latent heat of waste sintering gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58146476A JPS6039130A (en) | 1983-08-12 | 1983-08-12 | Method for recovering latent heat of waste sintering gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6039130A true JPS6039130A (en) | 1985-02-28 |
| JPS6248736B2 JPS6248736B2 (en) | 1987-10-15 |
Family
ID=15408499
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58146476A Granted JPS6039130A (en) | 1983-08-12 | 1983-08-12 | Method for recovering latent heat of waste sintering gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6039130A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0895049A1 (en) * | 1997-07-24 | 1999-02-03 | Siemens Aktiengesellschaft | Sintering installation |
| LU90439B1 (en) * | 1999-09-13 | 2001-03-14 | Wurth Paul Sa | Process for treating gases from a sintering plant |
| JP2020012574A (en) * | 2018-07-17 | 2020-01-23 | 日本製鉄株式会社 | Sintering machine and operation method thereof |
-
1983
- 1983-08-12 JP JP58146476A patent/JPS6039130A/en active Granted
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0895049A1 (en) * | 1997-07-24 | 1999-02-03 | Siemens Aktiengesellschaft | Sintering installation |
| US5971752A (en) * | 1997-07-24 | 1999-10-26 | Siemens Aktiengesellschaft | Sintering plant |
| LU90439B1 (en) * | 1999-09-13 | 2001-03-14 | Wurth Paul Sa | Process for treating gases from a sintering plant |
| WO2001019497A1 (en) * | 1999-09-13 | 2001-03-22 | Paul Wurth S.A. | Method of treating gases issued from a sintering plant |
| US6749822B2 (en) | 1999-09-13 | 2004-06-15 | Paul Wurth S.A. | Process for treatment of gases from a sintering plant |
| JP2020012574A (en) * | 2018-07-17 | 2020-01-23 | 日本製鉄株式会社 | Sintering machine and operation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6248736B2 (en) | 1987-10-15 |
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