JPH07180976A - Thermal recovering facility and thermal recovering method for cooler for high temperature particle block material - Google Patents
Thermal recovering facility and thermal recovering method for cooler for high temperature particle block materialInfo
- Publication number
- JPH07180976A JPH07180976A JP32371393A JP32371393A JPH07180976A JP H07180976 A JPH07180976 A JP H07180976A JP 32371393 A JP32371393 A JP 32371393A JP 32371393 A JP32371393 A JP 32371393A JP H07180976 A JPH07180976 A JP H07180976A
- Authority
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- Japan
- Prior art keywords
- pressure steam
- hot water
- cooler
- heat
- low
- 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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- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】この発明は焼結鉱等の高温粒塊物
の熱回収設備及びその熱回収方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a heat recovery facility for high temperature agglomerates such as sinter and a heat recovery method therefor.
【０００２】[0002]
【従来の技術】焼結鉱のような高温粒塊物を連続的に冷
却するクーラで発生する排風の顕熱利用として、排風
を直接に使用すること、排風を熱交換し蒸気、温水、
電力等に交換回収することに大別される。の代表例と
しては、焼結設備へ直接排風を循環して点火炉の燃焼用
空気、原料乾燥、保熱用熱源として利用する。2. Description of the Related Art As sensible heat utilization of exhaust air generated by a cooler for continuously cooling high temperature agglomerates such as sinter, direct use of exhaust air, heat exchange of exhaust air and steam, Warm water,
It is broadly divided into the exchange and recovery of electricity. As a typical example, the exhaust air is circulated directly to the sintering equipment to be used as the combustion air for the ignition furnace, the raw material drying, and the heat retaining heat source.
【０００３】しかし、実操業においては、熱回収装置
として排熱ボイラを用いた熱交換による排風の顕熱利用
の場合が多い。又、の排風の直接利用と、の排風の
熱交換利用を組合わせる場合もある。更にはクーラーの
高温側排風と、焼結機終段のウインドボックスからの排
風を抱合わせて熱回収の効率を図ったものがある（特公
昭５８−１５７０９号、特公昭６１−２５０７７号公
報）。However, in actual operation, sensible heat of exhaust air is often used by heat exchange using an exhaust heat boiler as a heat recovery device. Further, there is a case where the direct use of the exhaust air is used in combination with the heat exchange use of the exhaust air. Further, there is a system in which the high temperature side exhaust air of the cooler and the exhaust air from the wind box at the final stage of the sintering machine are combined to achieve the efficiency of heat recovery (Japanese Patent Publication No. 58-15709 and Japanese Patent Publication No. 61-25077). Gazette).
【０００４】その一例として、特公昭５８−１５７０９
号公報には、クーラーの高温側排風（排ガス）を導入す
る排熱ボイラーと焼結機終段のウインドボックスからの
排ガスを導入する過熱器とを設け、排熱ボイラーと過熱
器とを連結し、排熱ボイラーでクーラー排熱を回収し、
続いて過熱器で焼結機排熱を回収する焼結設備の排熱回
収装置が記載されている。As an example, Japanese Patent Publication No. 58-15709.
In the gazette, an exhaust heat boiler for introducing exhaust air (exhaust gas) on the high temperature side of the cooler and a superheater for introducing exhaust gas from the windbox at the final stage of the sintering machine are provided, and the exhaust heat boiler and the superheater are connected. And recover the cooler waste heat with the waste heat boiler,
Subsequently, an exhaust heat recovery device of a sintering facility that recovers exhaust heat of a sintering machine with a superheater is described.
【０００５】[0005]
【発明が解決しようとする課題】クーラで発生する排風
を排熱ボイラを用いて熱交換し、排風の顕熱を利用する
場合、例えば、焼結鉱クーラの排熱の顕熱回収として、
排熱ボイラで蒸気を製造している場合、まず、蒸気の条
件（温度、圧力）を設定し、伝熱面積（伝熱面積構成比
率も含む）が決められる。これによって排熱側の回収可
能範囲が制限される。しかし排風の温度は前工程での焼
結操業条件の影響が大きく、又、クーラの高温側入口と
低温側出口での排風の温度差が２００℃程度もあり、そ
れらの混合排風では安定した排風の温度を得ることが困
難である。そのため、必要な蒸気を必要な時機に十分に
回収出来ないと云う問題がある。When the exhaust air generated in the cooler is heat-exchanged using the exhaust heat boiler and the sensible heat of the exhaust air is utilized, for example, as a sensible heat recovery of the exhaust heat of the sinter cooler. ,
When steam is produced in the exhaust heat boiler, first, the steam conditions (temperature, pressure) are set, and the heat transfer area (including the heat transfer area composition ratio) is determined. This limits the recoverable range on the exhaust heat side. However, the temperature of the exhaust air is greatly influenced by the sintering operation conditions in the previous process, and the temperature difference between the high temperature inlet and the low temperature outlet of the cooler is about 200 ° C. It is difficult to obtain a stable exhaust air temperature. Therefore, there is a problem that necessary steam cannot be sufficiently recovered at a necessary time.
【０００６】そのために、一般には焼結鉱クーラの高温
側の排風の顕熱回収を行い、低温側の排風は直接利用
し、又は利用されないで廃棄される場合がある。特公昭
５８−１５７０９号公報に示されているような排熱回収
装置も低温側の排風の利用については記載されていな
い。Therefore, in general, sensible heat of the exhaust air on the high temperature side of the sinter cooler is recovered, and the exhaust air on the low temperature side may be directly used or may be discarded without being used. The exhaust heat recovery device as disclosed in Japanese Patent Publication No. 58-15709 does not describe the use of exhaust air on the low temperature side.
【０００７】しかしながら、焼結鉱クーラでは、クーラ
の入側で発生する排風の温度は４００℃程度で、出側で
発生する排風の温度は２００℃程度であり、低温側で発
生する排ガス量も多く、低温側の排風が十分に利用され
ないのは工場にとって大きな損失である。However, in the sinter ore cooler, the temperature of the exhaust air generated on the inlet side of the cooler is about 400 ° C., the temperature of the exhaust air generated on the outlet side is about 200 ° C., and the exhaust gas generated on the low temperature side is exhausted. It is a large loss for factories that the amount of air is large and the exhaust air on the low temperature side is not fully utilized.
【０００８】一方、工場内での、一連の排熱回収による
利用は、まちまちであるが、一般に工場では焼結鉱クー
ラの高温側の熱交換によって発生する中圧蒸気を利用す
る場合が多い。中圧蒸気はその系統に減圧装置を設ける
ことによって、使用時に低圧蒸気にすることが出来る。On the other hand, the use of a series of exhaust heat recovery in the factory varies, but in general, the factory often uses medium-pressure steam generated by heat exchange on the high temperature side of the sinter cooler. Medium pressure steam can be converted into low pressure steam at the time of use by providing a pressure reducing device in the system.
【０００９】この場合も、一般には中圧蒸気としての利
用が優先で、低圧蒸気を必要とする場所に十分に行渡ら
ない場合がある。上記のような場合は中圧蒸気、低圧蒸
気の有効利用が十分でなく、その都度余剰を生じたり、
不足を生じたりしていた。In this case as well, the use as medium-pressure steam is generally prioritized, and there is a case where low-pressure steam cannot be sufficiently distributed to a place where it is necessary. In the above cases, the effective use of medium-pressure steam and low-pressure steam is not sufficient, and each time there is a surplus,
There was a shortage.
【００１０】本発明では上記のような問題点を解決する
ものであり、クーラの排風の熱交換で生じる蒸気を、中
圧蒸気、低圧蒸気として、その使用量に応じて、無駄な
く利用出来るクーラの熱回収設備及び熱回収方法を提供
することを目的とする。The present invention solves the above-mentioned problems, and steam generated by heat exchange of exhaust air from a cooler can be used as medium pressure steam or low pressure steam without waste depending on the amount used. An object of the present invention is to provide a heat recovery facility and a heat recovery method for a cooler.
【００１１】[0011]
【課題を解決するための手段】上記目的を達成するため
に、本発明は高温粒塊物を連続的に冷却するクーラに、
クーラの排風を熱交換する中圧蒸気回収装置と、熱水お
よび低圧蒸気回収装置を付設して、前記中圧蒸気回収装
置の節炭器と、熱水および低圧蒸気回収装置の熱水循環
配管との間に切換機構を設けて連結させたことを特徴と
する高温粒塊物のクーラの熱回収設備とするものであ
る。In order to achieve the above object, the present invention provides a cooler for continuously cooling high-temperature agglomerates.
A medium pressure steam recovery device for exchanging the exhaust air of the cooler, a hot water and low pressure steam recovery device are attached, and a economizer for the medium pressure steam recovery device and hot water circulation for the hot water and low pressure steam recovery device. A heat recovery equipment for a cooler for high-temperature agglomerates, which is characterized in that a switching mechanism is provided and connected to the pipe.
【００１２】又、上記の回収設備を用いて、高温粒塊物
を連続的に冷却するクーラの排風と熱交換して中圧蒸
気、熱水と低圧蒸気を回収するにあたり、前記熱水と低
圧蒸気の使用量に余剰を生じた場合、その熱水の一部を
中圧蒸気に、また、熱水と低圧蒸気の使用量に不足を生
じた場合、中圧蒸気の供給熱水の一部を低圧蒸気にする
ことを特徴とする高温粒塊物のクーラの熱回収方法とす
るものである。Further, in recovering the medium pressure steam, the hot water and the low pressure steam by exchanging heat with the exhaust air of the cooler for continuously cooling the high temperature agglomerates using the above-mentioned recovery equipment, If the amount of low-pressure steam used is surplus, part of the hot water is used as medium-pressure steam, and if the amount of hot water and low-pressure steam used is insufficient, it becomes This is a method for recovering heat from a cooler of high-temperature agglomerates, which is characterized in that low-pressure steam is used for the part.
【００１３】[0013]
【作用】本発明において、（１）高温粒塊物を連続的に
冷却するクーラとは、焼結機の後にクラッシャを介して
接続されている焼結クーラのようなクーラである。ここ
では連続的にクーラ内に挿入される粒塊焼結鉱を冷却出
来るように、下側に複数個の風箱がラインに沿って配設
されており、エンドレスの台車上に載置された粒塊焼結
鉱が台車本体の孔から挿入された強制風によって冷却さ
れながらクーラ内を移動する。クーラにはダクトがライ
ンに沿って複数本配設されている。このダクトによっ
て、高温側の排風と、低温側の排風を区分する。高温粒
塊物とは焼結機を出てクラッシャで破砕された粒塊の焼
結鉱等を云う。In the present invention, (1) the cooler for continuously cooling the high temperature agglomerates is a cooler such as a sintering cooler connected after the sintering machine via a crusher. Here, in order to cool the agglomerate sinter that is continuously inserted into the cooler, a plurality of wind boxes are arranged along the line on the lower side and placed on an endless truck. The agglomerate sinter moves in the cooler while being cooled by the forced air inserted from the holes of the trolley body. A plurality of ducts are arranged along the line in the cooler. This duct separates the high temperature side exhaust air and the low temperature side exhaust air. A high-temperature agglomerate refers to a sinter or the like of an agglomerate that has left the sintering machine and crushed by a crusher.
【００１４】（２）クーラの排風を熱交換する中圧蒸気
回収装置と、熱水および低圧蒸気回収装置を付設したの
は、中圧蒸気回収装置は高温側の排風の熱交換に対応さ
せ、熱水と低圧蒸気の回収装置は低温側の排風の熱交換
に対応させることによる。ここにおいて、中圧蒸気回収
装置は節炭器（エコノマイザ）、エバボレータ、スーパ
ーヒータ、ドラムを具備したものである。一方、熱水お
よび低圧蒸気回収装置は熱水熱交換器と低圧蒸気フラッ
シュタンクを具備し、熱水熱交換器と低圧蒸気フラッシ
ュタンクとは熱水循環配管によって接続されている。(2) The medium pressure steam recovery device for exchanging heat from the exhaust air of the cooler and the hot water and low pressure steam recovery device are attached to the medium pressure steam recovery device for heat exchange of the exhaust air on the high temperature side. This is because the hot water and low-pressure steam recovery device supports heat exchange of the low temperature side exhaust air. Here, the medium-pressure vapor recovery device is equipped with a economizer, an evaporator, a super heater, and a drum. On the other hand, the hot water and low pressure steam recovery device includes a hot water heat exchanger and a low pressure steam flash tank, and the hot water heat exchanger and the low pressure steam flash tank are connected by a hot water circulation pipe.
【００１５】本発明の主要な特徴は中圧蒸気回収装置の
節炭器と、熱水および低圧蒸気回収装置の熱水循環配管
との間に切換機構を設けて連結させたことである。本発
明によれば、低圧蒸気の使用量が減少し、中圧蒸気の需
要が増加した時は、低圧蒸気回収装置のフラッシュ蒸気
弁を必要量に応じて絞り込み、熱水循環配管から中圧蒸
気回収装置の節炭器出口ヘッダ管に接続する分岐管に設
けた切換機構の弁を開き、加圧熱水を中圧蒸気回収装置
のエバボレータ側に供給する。節炭器出口にて合流増量
した熱水はエバボレータ、スーパーヒータを通り、過熱
蒸気になる。The main feature of the present invention is that a switching mechanism is provided and connected between the economizer of the medium pressure steam recovery device and the hot water circulation pipe of the hot water and low pressure steam recovery device. According to the present invention, when the use amount of low-pressure steam is reduced and the demand for medium-pressure steam is increased, the flash steam valve of the low-pressure steam recovery device is narrowed down according to the required amount, and the medium-pressure steam is supplied from the hot water circulation pipe. The valve of the switching mechanism provided in the branch pipe connected to the outlet pipe of the economizer of the recovery device is opened to supply pressurized hot water to the evaporator side of the intermediate pressure steam recovery device. The hot water merged and increased at the outlet of the economizer passes through the evaporator and super heater to become superheated steam.
【００１６】一方、低圧蒸気の需要が増加した時（低圧
蒸気回収の優先度が高い時）低圧蒸気増加量に見合う熱
水を中圧蒸気回収装置の節炭器で増加製造し、分岐管の
切換機構の弁を開き、分岐管を経由し、低圧蒸気回収装
置の熱水循環配管に戻し、フラッシュタンクに導き、熱
水量を増加させ、低圧蒸気を増加発生させる。On the other hand, when the demand for low-pressure steam increases (when the priority of low-pressure steam recovery is high), hot water commensurate with the increased amount of low-pressure steam is additionally manufactured by the economizer of the medium-pressure steam recovery device, and the branch pipe The valve of the switching mechanism is opened, returned to the hot water circulation pipe of the low pressure steam recovery device via the branch pipe, and led to the flash tank to increase the amount of hot water and increase the generation of low pressure steam.
【００１７】即ち、本発明によれば、異なるポテンシャ
ルレベルの排熱回収装置（ボイラ等）により、エネルギ
ー需給バランスの変動が節炭器と熱水循環配管との間に
設けた切換機構を操作して連結することで吸収され、供
給不足に伴う設備トラブル、稼働率低下や、供給過多バ
ランスの回収エネルギーの大気放散等の損失を削減す
る。That is, according to the present invention, the exhaust heat recovery device (boiler or the like) having different potential levels operates the switching mechanism provided between the economizer and the hot water circulation pipe when the fluctuation of the energy supply and demand balance. It will be absorbed by connecting the two to reduce losses such as equipment troubles due to supply shortages, lowering of operating rates, and atmospheric emission of recovered energy due to excessive supply balance.
【００１８】[0018]
【実施例】本発明の実施例を図面を用いて説明する。図
１は本発明の一実施例として、焼結設備のクーラの熱回
収設備を示す図である。ここではクーラを焼結クーラと
して説明する。図において、１は中圧蒸気回収装置、２
は低圧蒸気回収装置、３は節炭器、４は熱水循環配管で
ある。Embodiments of the present invention will be described with reference to the drawings. FIG. 1 is a view showing heat recovery equipment of a cooler of a sintering equipment as one embodiment of the present invention. Here, the cooler will be described as a sintered cooler. In the figure, 1 is a medium pressure vapor recovery device, 2
Is a low pressure steam recovery device, 3 is a economizer, and 4 is a hot water circulation pipe.
【００１９】本発明の焼結クーラ６の熱回収設備は、ク
ラッシャで破砕された高温の粒塊焼結鉱を連続的に焼結
クーラ６に、焼結クーラの排風を熱交換する中圧蒸気回
収装置１と、熱水および低圧蒸気回収装置２を付設し
て、中圧蒸気回収装置１の節炭器３と、熱水および低圧
蒸気回収装置２の熱水循環配管５との間に設けた切換弁
７によって切換え可能に連結させたものである。排熱の
有効利用の構成として、焼結クーラ６の高温排風側Ａの
ダクト８に中圧蒸気回収装置１を付設し、低温排風側Ｂ
のダクト９に、熱水および低圧蒸気回収装置２を付設し
ている。The heat recovery equipment of the sinter cooler 6 of the present invention is a medium pressure sinter that continuously exchanges the high temperature agglomerate sinter crushed by a crusher into the sinter cooler 6 and the exhaust air of the sinter cooler. A steam recovery device 1 and a hot water / low pressure steam recovery device 2 are attached, and a space between the economizer 3 of the medium pressure steam recovery device 1 and the hot water circulation pipe 5 of the hot water / low pressure steam recovery device 2 is provided. The changeover valve 7 is provided so as to be switchable. As a configuration for effectively utilizing the exhaust heat, the medium pressure steam recovery device 1 is attached to the duct 8 on the high temperature exhaust side A of the sintering cooler 6, and the low temperature exhaust side B is attached.
The hot water and low-pressure steam recovery device 2 is attached to the duct 9 of FIG.
【００２０】ここでは中圧蒸気回収装置１は節炭器４、
エバボレータ１０、スーパーヒータ１１、ドラム１２を
具備したものである。一方、熱水および低圧蒸気回収装
置２は熱水熱交換器１３と低圧蒸気フラッシュタンク１
４を具備し、熱水熱交換器１３と低圧蒸気フラッシュタ
ンク１４とは熱水循環配管４によって接続されている。
５は蒸気を需要する工場の総称である。Here, the medium-pressure steam recovery device 1 includes a economizer 4,
An evaporator 10, a super heater 11, and a drum 12 are provided. On the other hand, the hot water and low pressure steam recovery device 2 includes a hot water heat exchanger 13 and a low pressure steam flash tank 1
4, the hot water heat exchanger 13 and the low-pressure steam flash tank 14 are connected by a hot water circulation pipe 4.
5 is a general term for factories that demand steam.
【００２１】本発明では低圧蒸気の使用量が減少し、中
圧蒸気の需要が増加した時は、低圧蒸気回収装置２のフ
ラッシュ蒸気弁１５を必要量に応じて絞り込み、熱水循
環配管４から中圧蒸気回収装置１の節炭器４出口ヘッダ
管１６に接続する分岐管の切換弁７を開き、加圧熱水を
中圧蒸気回収装置１のエバボレータ側に供給する。節炭
器４の出口で合流増量した熱水はエバボレータ１０、ス
ーパーヒータ１１を通り、過熱蒸気になる。In the present invention, when the amount of low-pressure steam used decreases and the demand for medium-pressure steam increases, the flash steam valve 15 of the low-pressure steam recovery device 2 is narrowed down according to the required amount, and the hot water circulation pipe 4 is used. The switching valve 7 of the branch pipe connected to the header pipe 16 of the economizer 4 of the medium-pressure steam recovery device 1 is opened to supply pressurized hot water to the evaporator side of the medium-pressure steam recovery device 1. The hot water combined and increased at the outlet of the economizer 4 passes through the evaporator 10 and the super heater 11, and becomes superheated steam.
【００２２】一方、低圧蒸気の需要が増加した時（低圧
蒸気回収の優先度が高い時）低圧蒸気増加量に見合う熱
水を中圧蒸気回収装置１の節炭器４で増加製造し、分岐
管の切換弁７を開き、分岐管を経由し、低圧蒸気回収装
置２の熱水循環配管４に戻し、フラッシュタンク１４に
導き、熱水量を増加させ、低圧蒸気を増加発生させる。
これらの操作は工場データを制御機構１８に入力して、
自動的に行われる。ここでは比較的温度が低い２００〜
２５０℃の排風は熱交換器１３に導かれ、１２ｋｇ／ｃ
ｍ2 約１２０〜１３０℃の加圧熱水と熱交換する。On the other hand, when the demand for low-pressure steam increases (when the priority of low-pressure steam recovery is high), hot water commensurate with the increased amount of low-pressure steam is increased in the economizer 4 of the medium-pressure steam recovery device 1 and branched. The pipe switching valve 7 is opened and returned to the hot water circulation pipe 4 of the low pressure steam recovery device 2 via the branch pipe and led to the flash tank 14 to increase the amount of hot water and increase the generation of low pressure steam.
These operations input factory data to the control mechanism 18,
It is done automatically. Here, the temperature is relatively low
Exhaust air at 250 ° C is introduced to the heat exchanger 13 and 12 kg / c
m 2 Heat is exchanged with pressurized hot water of about 120 to 130 ° C.
【００２３】熱交換によって得られた熱水は約１９０℃
に昇温され、フラッシュタンク１４または中圧蒸気回収
装置１の節炭器４の出口ヘッダ管１６へ供給される。フ
ラッシュタンク１４へ供給された熱水は減圧（フラッシ
ュ）し、４．５ｋｇ／ｃｍ2 飽和蒸気で１９Ｔ／ｈｒ発
生し、低圧蒸気使用プロセスに送気される。The hot water obtained by heat exchange is about 190 ° C.
And is supplied to the outlet header pipe 16 of the economizer 4 of the flash tank 14 or the intermediate pressure steam recovery device 1. The hot water supplied to the flash tank 14 is decompressed (flushed), generates 19 T / hr with 4.5 kg / cm 2 saturated steam, and is sent to the low pressure steam using process.
【００２４】又、中圧蒸気回収装置１に供給された熱水
は節炭器４の出口で中圧蒸気回収装置１の給水と混合さ
れ、排ガスで昇熱され、エバボレータ１０、スーパーヒ
ータ１１を通り、過熱蒸気（１４ｋｇ／ｃｍ2 、２７０
℃）となる。本発明では約４８Ｔ／ｈｒの蒸気回収増が
期待出来る。Further, the hot water supplied to the medium pressure steam recovery device 1 is mixed with the water supply of the medium pressure steam recovery device 1 at the outlet of the economizer 4, and is heated by the exhaust gas to drive the evaporator 10 and the super heater 11. Street, superheated steam (14 kg / cm 2 , 270
℃). In the present invention, a vapor recovery increase of about 48 T / hr can be expected.
【００２５】上記のような熱回収設備を用いて、熱回収
を行った場合の実施例を具体的に説明する。 本発明による場合：低圧蒸気回収装置併設 回収熱量 １６×１０6 Ｋcal/ｈｒ １５Kg/cm2 熱水（循環） １９０℃ ２５０T/ｈｒ 即ち フラッシュ蒸気製造（4.5 Kg /cm2 の場
合) １９T/hr （回収熱１2 ×１０6 Ｋcal/ｈｒ） 排熱ボイラ回収蒸気量アップ ４〜８T/hr( 最
大) （回収熱 ４×１０6 Ｋcal/ｈｒ） 従来 排熱ボイラ( ベース) 回収熱 29 ×１０6 Ｋca
l/ｈｒ ４５〜５０T/hr（１4 Kg/cm2 ２７０℃) 増加回収エネルギー 16 ×１０6 Ｋcal/ｈｒ (２６
％アップ） 以上のように、本発明によれば次のような効果をあげる
ことが出来る。A specific example of heat recovery using the above heat recovery equipment will be described. According to the present invention: (for 4.5 Kg / cm 2) low pressure steam recovery system features heat collection amount 16 × 10 6 Kcal / hr 15Kg / cm 2 hydrothermal (circulation) 190 ℃ 250T / hr i.e. flush steam production 19T / hr ( Recovered heat 12 × 10 6 Kcal / hr) Exhaust heat boiler Recovered steam amount up 4-8 T / hr (maximum) (Recovered heat 4 × 10 6 Kcal / hr) Conventional exhaust heat boiler (base) Recovered heat 29 × 10 6 Kca
l / hr 45 to 50 T / hr (14 Kg / cm 2 270 ° C.) Increased recovery energy 16 × 10 6 Kcal / hr (26
% Increase) As described above, according to the present invention, the following effects can be obtained.
【００２６】（１）中圧蒸気、低圧蒸気の需給バランス
が変動しても、熱水循環系統と連結しているので、相互
に形態を変えて、損失を軽減して回収出来る。 （２）排熱源のポテンシャルに応じ、排熱源側、及び利
用側の変動に対し、適正な熱回収が出来る。即ち、 排熱回収装置は中圧蒸気回収用と、熱水および低圧
蒸気回収用の２段設置であるので、熱水および低圧蒸気
回収装置は変動吸収を目的とし多機能化出来る。多機能
化とは熱交換媒体を低圧蒸気、熱水、温水（１００℃以
下の水）の３形態としてとり得るものであり、エネルギ
ー需要バランスの変動に対し、形態変更、相互運用など
により、排熱の利用率の向上を図ることが出来る。 ポテンシャルの異なる排熱を複数の回収装置で、形
態、温度、圧力条件の異なったエネルギーに変換回収す
ることが出来るので、排熱発生源及び回収エネルギー使
用側のバランスを調節出来る。(1) Even if the supply and demand balance of the medium-pressure steam and the low-pressure steam fluctuates, since they are connected to the hot water circulation system, the forms can be changed mutually and the loss can be reduced and recovered. (2) Depending on the potential of the exhaust heat source, appropriate heat recovery can be performed against fluctuations on the exhaust heat source side and the use side. That is, since the exhaust heat recovery device is installed in two stages, one for medium pressure steam recovery and the other for hot water and low pressure steam recovery, the hot water and low pressure steam recovery device can be made multi-functional for the purpose of absorbing fluctuations. Multifunctionalization means that the heat exchange medium can take three forms: low-pressure steam, hot water, and hot water (water at 100 ° C or lower). It is possible to improve the heat utilization rate. Exhaust heat having different potentials can be converted and recovered by a plurality of recovery devices into energy having different forms, temperatures, and pressure conditions, so that the balance between the exhaust heat generation source and the recovery energy use side can be adjusted.
【００２７】[0027]
【発明の効果】本発明は次の効果を得ることが出来る。 排熱回収領域が中低温領域まで拡大し、回収熱量が増
加する。 中圧、低圧蒸気の需要バランスが変動しても、熱水循
環系統を連結しているので、相互に形態を変えて損失を
軽減して回収できる。According to the present invention, the following effects can be obtained. The exhaust heat recovery area expands to the mid-low temperature area, and the amount of recovered heat increases. Even if the demand balance of medium-pressure and low-pressure steam fluctuates, the hot water circulation system is connected, so the forms can be changed mutually and the loss can be reduced and recovered.
【図１】本発明の一実施例を示す図である。FIG. 1 is a diagram showing an embodiment of the present invention.
１ 中圧蒸気回収装置 ２ 熱水および低圧蒸気回収装置 ３ 節炭器 ４ 熱水循環配管 ５ 蒸気を需要する工場の総称 ６ 焼結クーラ ７ 切換弁 ８ 高温排風側のダクト ９ 低温排風側のダクト １０ エバポレータ １１ スーパーヒータ １２ ドラム １３ 熱水熱交換器 １４ 低圧蒸気フラッシュタンク １５ フラッシュ蒸気弁 １６ ヘッダ管 １７ 分岐管 １８ 制御機構 1 Medium-pressure steam recovery device 2 Hot water and low-pressure steam recovery device 3 Coal economizer 4 Hot water circulation pipe 5 Generic term for a factory that demands steam 6 Sintering cooler 7 Switching valve 8 High temperature exhaust side duct 9 Low temperature exhaust side Duct 10 Evaporator 11 Super heater 12 Drum 13 Hot water heat exchanger 14 Low pressure steam flash tank 15 Flash steam valve 16 Header pipe 17 Branch pipe 18 Control mechanism
【手続補正書】[Procedure amendment]
【提出日】平成６年２月１５日[Submission date] February 15, 1994
【手続補正１】[Procedure Amendment 1]
【補正対象書類名】明細書[Document name to be amended] Statement
【補正対象項目名】全文[Correction target item name] Full text
【補正方法】変更[Correction method] Change
【補正内容】[Correction content]
【書類名】 明細書[Document name] Statement
【発明の名称】 高温粒塊物のクーラの熱回収設備及び
その熱回収方法Title: Heat recovery equipment for high temperature agglomerate cooler and heat recovery method thereof
【特許請求の範囲】[Claims]
【発明の詳細な説明】Detailed Description of the Invention
【０００１】[0001]
【産業上の利用分野】この発明は焼結鉱等の高温粒塊物
の熱回収設備及びその熱回収方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a heat recovery facility for high temperature agglomerates such as sinter and a heat recovery method therefor.
【０００２】[0002]
【従来の技術】焼結鉱のような高温粒塊物を連続的に気
体で冷却するクーラで発生する排風の顕熱利用方法は、
排風を直接に使用する方法、排風を熱交換し蒸気、
温水、電力等に交換回収する方法に大別される。の代
表例としては、焼結設備へ直接排風を循環して点火炉の
燃焼用空気、原料乾燥、保熱用熱源として利用するもの
がある。しかし、実操業においては、熱回収装置とし
て排熱ボイラを用いた熱交換による排風の顕熱利用の場
合が多い。2. Description of the Related Art A method for utilizing sensible heat of exhaust air generated by a cooler that continuously cools high-temperature agglomerates such as sinter with a gas is as follows.
Method of using exhaust air directly, heat exchange of exhaust air, steam,
It is roughly divided into methods of collecting and collecting hot water, electric power, etc. As a typical example, there is one in which exhaust air is directly circulated to a sintering facility to be used as combustion air for an ignition furnace, raw material drying, and heat source for heat retention. However, in actual operation, sensible heat of exhaust air is often used by heat exchange using an exhaust heat boiler as a heat recovery device.
【０００３】[0003]
【発明が解決しようとする課題】焼結鉱クーラの排熱の
顕熱回収として、排熱ボイラで蒸気を製造している場
合、まず、蒸気の条件（温度、圧力）を設定し、伝熱面
積（伝熱面積構成比率も含む）が決められる。しかし排
風の温度は前工程での焼結操業条件の影響が大きく、
又、クーラの高温側入口と低温側出口での排風の温度差
が２００℃程度もあり、それらの混合排風では安定した
排風の温度を得ることが困難である。そのため、必要な
蒸気を必要な時機に十分に回収出来ないと云う問題があ
る。As a sensible heat recovery of the exhaust heat of the sinter cooler, when steam is produced in the exhaust heat boiler, first, the steam conditions (temperature and pressure) are set and heat transfer is performed. Area (including heat transfer area composition ratio) is determined. However, the temperature of exhaust air is greatly affected by the sintering operation conditions in the previous process,
Further, the temperature difference between the exhaust air at the high temperature side inlet and the low temperature side outlet of the cooler is about 200 ° C., and it is difficult to obtain a stable exhaust air temperature with the mixed exhaust air. Therefore, there is a problem that necessary steam cannot be sufficiently recovered at a necessary time.
【０００４】本発明は上記のような問題点を解決するも
のであり、クーラの排風の熱交換で生じる蒸気を、中圧
蒸気、低圧蒸気として、その使用量に応じて、無駄なく
利用出来るクーラの熱回収設備及び熱回収方法を提供す
ることを目的とする。The present invention solves the above problems, and steam generated by heat exchange of exhaust air of a cooler can be used as medium pressure steam or low pressure steam without waste depending on the amount used. An object of the present invention is to provide a heat recovery facility and a heat recovery method for a cooler.
【０００５】[0005]
【課題を解決するための手段】上記目的は、高温粒塊物
を連続的に気体で冷却するクーラの排風との熱交換によ
り中圧蒸気を発生する中圧蒸気回収装置に加えて、前記
クーラの排風との熱交換により熱水および低圧蒸気を発
生する熱水および低圧蒸気回収装置が設けられ、前記中
圧蒸気回収装置は節炭器と蒸発器を、前記熱水および低
圧蒸気回収装置は熱水循環配管をそれぞれ有してなり、
前記節炭器と前記熱水循環配管との間が切替機構を介し
て連結されていることを特徴とする高温粒塊物のクーラ
の熱回収設備、及び、高温粒塊物を連続的に気体で冷却
するクーラの排風との熱交換により中圧蒸気に加えて、
熱水および低圧蒸気を回収するにあたり、前記熱水と低
圧蒸気の使用量に余剰を生じた場合、その熱水の一部を
中圧蒸気に、また、熱水と低圧蒸気の使用量に不足を生
じた場合、中圧蒸気の供給熱水の一部を低圧蒸気にする
ことを特徴とする高温粒塊物のクーラの熱回収方法によ
り達成される。The above-mentioned object is to provide an intermediate-pressure steam recovery device that generates intermediate-pressure steam by heat exchange with the exhaust air of a cooler that continuously cools high-temperature agglomerates with a gas. A hot water and low pressure steam recovery device that generates hot water and low pressure steam by heat exchange with the exhaust air of the cooler is provided, and the medium pressure steam recovery device includes a economizer and an evaporator, and the hot water and low pressure steam recovery device. The device has hot water circulation piping,
A heat recovery equipment for a cooler of high temperature agglomerates, characterized in that the economizer and the hot water circulation pipe are connected through a switching mechanism, and a gas for the high temperature agglomerates continuously. In addition to the medium pressure steam by heat exchange with the exhaust air of the cooler cooled by
If excess hot water and low pressure steam are used to recover hot water and low pressure steam, some of the hot water will be insufficient for medium pressure steam and hot water and low pressure steam will be insufficient. In the case of occurrence of, the heat recovery method of the cooler for high temperature agglomerates is characterized in that a part of the hot water supplied to the medium pressure steam is converted to low pressure steam.
【０００６】[0006]
【作用】クーラにおいて高温粒塊物を連続的に冷却した
気体は、高温となって中圧蒸気回収装置に入り、蒸発器
及び節炭器を介して熱交換されて冷却される。節炭器で
は高温の水が作られ、蒸発器では中圧蒸気が生成され
る。一方、高温の気体の一部は、熱水および低圧蒸気回
収装置に導かれ、熱交換により熱水および低圧蒸気を発
生させる。中圧蒸気回収装置の節炭器と熱水および低圧
蒸気回収装置の熱水循環配管とが、切替機構を介して結
合されているので、熱水と低圧蒸気の使用量に余剰を生
じた場合には、その余剰部分を、切替機構を介して節炭
器側に回して中圧蒸気の発生を増加させることができ
る。反対に、熱水と低圧蒸気の使用量に不足を生じた場
合には、節炭器の熱水を切替機構を介して、熱水および
低圧蒸気回収装置の熱水循環配管に回すことにより、熱
水と低圧蒸気の発生を増加させることができる。The gas obtained by continuously cooling the high-temperature agglomerates in the cooler reaches a high temperature, enters the medium-pressure steam recovery device, and is heat-exchanged and cooled through the evaporator and the economizer. Hot water is produced in the economizer and medium pressure steam is produced in the evaporator. On the other hand, a part of the high-temperature gas is guided to the hot water and low-pressure steam recovery device and heat-exchanges to generate hot water and low-pressure steam. When the economizer of the medium-pressure steam recovery device and the hot water and low-temperature steam recovery device hot-water circulation piping are connected via a switching mechanism, if there is an excess in the amount of hot-water and low-pressure steam used. In addition, the surplus portion can be turned to the economizer side through the switching mechanism to increase the generation of medium-pressure steam. On the other hand, when the amount of hot water and low-pressure steam used is insufficient, by turning the hot water of the economizer through the switching mechanism into the hot water and low-pressure steam recovery device hot water circulation pipe, The generation of hot water and low pressure steam can be increased.
【０００７】[0007]
【実施例】本発明の実施例を図面を用いて説明する。図
１は本発明の一実施例として、焼結設備のクーラの熱回
収設備を示す図である。ここではクーラを焼結クーラと
して説明する。図において、１は中圧蒸気回収装置、２
は低圧蒸気回収装置、３は節炭器、４は熱水循環配管で
ある。Embodiments of the present invention will be described with reference to the drawings. FIG. 1 is a view showing heat recovery equipment of a cooler of a sintering equipment as one embodiment of the present invention. Here, the cooler will be described as a sintered cooler. In the figure, 1 is a medium pressure vapor recovery device, 2
Is a low pressure steam recovery device, 3 is a economizer, and 4 is a hot water circulation pipe.
【０００８】本発明の焼結クーラ６の熱回収設備は、ク
ラッシャで破砕された高温の粒塊焼結鉱を連続的に焼結
クーラ６に、焼結クーラの排風を熱交換する中圧蒸気回
収装置１と、熱水および低圧蒸気回収装置２を付設し
て、中圧蒸気回収装置１の節炭器３と、熱水および低圧
蒸気回収装置２の熱水循環配管５との間に設けた切換弁
７によって切換え可能に連結させたものである。排熱の
有効利用の構成として、焼結クーラ６の高温排風側Ａの
ダクト８に中圧蒸気回収装置１を付設し、低温排風側Ｂ
のダクト９に、熱水および低圧蒸気回収装置２を付設し
ている。The heat recovery equipment for the sinter cooler 6 of the present invention is a medium pressure sinter that continuously exchanges the exhaust air of the sinter cooler with the high temperature agglomerate sinter crushed by a crusher. A steam recovery device 1 and a hot water / low pressure steam recovery device 2 are attached, and a space between the economizer 3 of the medium pressure steam recovery device 1 and the hot water circulation pipe 5 of the hot water / low pressure steam recovery device 2 is provided. The changeover valve 7 is provided so as to be switchable. As a configuration for effectively utilizing the exhaust heat, the medium pressure steam recovery device 1 is attached to the duct 8 on the high temperature exhaust side A of the sintering cooler 6, and the low temperature exhaust side B is attached.
The hot water and low-pressure steam recovery device 2 is attached to the duct 9 of FIG.
【０００９】ここでは中圧蒸気回収装置１は節炭器４、
エバボレータ１０、スーパーヒータ１１、ドラム１２を
具備したものである。一方、熱水および低圧蒸気回収装
置２は熱水熱交換器１３と低圧蒸気フラッシュタンク１
４を具備し、熱水熱交換器１３と低圧蒸気フラッシュタ
ンク１４とは熱水循環配管４によって接続されている。
５は蒸気を需要する工場の総称である。Here, the medium-pressure steam recovery device 1 includes a economizer 4,
An evaporator 10, a super heater 11, and a drum 12 are provided. On the other hand, the hot water and low pressure steam recovery device 2 includes a hot water heat exchanger 13 and a low pressure steam flash tank 1
4, the hot water heat exchanger 13 and the low-pressure steam flash tank 14 are connected by a hot water circulation pipe 4.
5 is a general term for factories that demand steam.
【００１０】本発明では低圧蒸気の使用量が減少し、中
圧蒸気の需要が増加した時は、低圧蒸気回収装置２のフ
ラッシュ蒸気弁１５を必要量に応じて絞り込み、熱水循
環配管４から中圧蒸気回収装置１の節炭器４出口ヘッダ
管１６に接続する分岐管の切換弁７を開き、加圧熱水を
中圧蒸気回収装置１のエバボレータ側に供給する。節炭
器４の出口で合流増量した熱水はエバボレータ１０、ス
ーパーヒータ１１を通り、過熱蒸気になる。In the present invention, when the amount of low-pressure steam used decreases and the demand for medium-pressure steam increases, the flash steam valve 15 of the low-pressure steam recovery device 2 is narrowed down according to the required amount, and the hot water circulation pipe 4 is used. The switching valve 7 of the branch pipe connected to the header pipe 16 of the economizer 4 of the medium-pressure steam recovery device 1 is opened to supply pressurized hot water to the evaporator side of the medium-pressure steam recovery device 1. The hot water combined and increased at the outlet of the economizer 4 passes through the evaporator 10 and the super heater 11, and becomes superheated steam.
【００１１】一方、低圧蒸気の需要が増加した時（低圧
蒸気回収の優先度が高い時）低圧蒸気増加量に見合う熱
水を中圧蒸気回収装置１の節炭器４で増加製造し、分岐
管の切換弁７を開き、分岐管を経由し、低圧蒸気回収装
置２の熱水循環配管４に戻し、フラッシュタンク１４に
導き、熱水量を増加させ、低圧蒸気を増加発生させる。
これらの操作は工場データを制御機構１８に入力して、
自動的に行われる。ここでは比較的温度が低い２００〜
２５０℃の排風は熱交換器１３に導かれ、１２ｋｇ／ｃ
ｍ2 約１２０〜１３０℃の加圧熱水と熱交換する。On the other hand, when the demand for low-pressure steam increases (when the priority of low-pressure steam recovery is high), hot water commensurate with the increased amount of low-pressure steam is increased in the economizer 4 of the medium-pressure steam recovery device 1 and branched. The pipe switching valve 7 is opened and returned to the hot water circulation pipe 4 of the low pressure steam recovery device 2 via the branch pipe and led to the flash tank 14 to increase the amount of hot water and increase the generation of low pressure steam.
These operations input factory data to the control mechanism 18,
It is done automatically. Here, the temperature is relatively low
Exhaust air at 250 ° C is introduced to the heat exchanger 13 and 12 kg / c
m 2 Heat is exchanged with pressurized hot water of about 120 to 130 ° C.
【００１２】熱交換によって得られた熱水は約１９０℃
に昇温され、フラッシュタンク１４または中圧蒸気回収
装置１の節炭器４の出口ヘッダ管１６へ供給される。フ
ラッシュタンク１４へ供給された熱水は減圧（フラッシ
ュ）し、４．５ｋｇ／ｃｍ2 飽和蒸気で１９Ｔ／ｈｒ発
生し、低圧蒸気使用プロセスに送気される。The hot water obtained by heat exchange is about 190 ° C.
And is supplied to the outlet header pipe 16 of the economizer 4 of the flash tank 14 or the intermediate pressure steam recovery device 1. The hot water supplied to the flash tank 14 is decompressed (flushed), generates 19 T / hr with 4.5 kg / cm 2 saturated steam, and is sent to the low pressure steam using process.
【００１３】又、中圧蒸気回収装置１に供給された熱水
は節炭器４の出口で中圧蒸気回収装置１の給水と混合さ
れ、排ガスで昇熱され、エバボレータ１０、スーパーヒ
ータ１１を通り、過熱蒸気（１４ｋｇ／ｃｍ2 、２７０
℃）となる。本発明では約４８Ｔ／ｈｒの蒸気回収増が
期待出来る。Further, the hot water supplied to the medium pressure steam recovery device 1 is mixed with the feed water of the medium pressure steam recovery device 1 at the outlet of the economizer 4, and is heated by the exhaust gas to drive the evaporator 10 and the super heater 11. Street, superheated steam (14 kg / cm 2 , 270
℃). In the present invention, a vapor recovery increase of about 48 T / hr can be expected.
【００１４】上記のような熱回収設備を用いて、熱回収
を行った場合の実施例を具体的に説明する。 本発明による場合：低圧蒸気回収装置併設 回収熱量 １６×１０6 Ｋcal/ｈｒ １５Kg/cm2 熱水（循環） １９０℃ ２５０T/ｈｒ 即ち フラッシュ蒸気製造（4.5 Kg /cm2 の場
合) １９T/hr （回収熱１2 ×１０6 Ｋcal/ｈｒ） 排熱ボイラ回収蒸気量アップ ４〜８T/hr( 最
大) （回収熱 ４×１０6 Ｋcal/ｈｒ） 従来 排熱ボイラ( ベース) 回収熱 29 ×１０6 Ｋca
l/ｈｒ ４５〜５０T/hr（１4 Kg/cm2 ２７０℃) 増加回収エネルギー 16 ×１０6 Ｋcal/ｈｒ (２６
％アップ） 以上のように、本発明によれば次のような効果をあげる
ことが出来る。An example of heat recovery using the heat recovery equipment as described above will be specifically described. According to the present invention: (for 4.5 Kg / cm 2) low pressure steam recovery system features heat collection amount 16 × 10 6 Kcal / hr 15Kg / cm 2 hydrothermal (circulation) 190 ℃ 250T / hr i.e. flush steam production 19T / hr ( Recovered heat 12 × 10 6 Kcal / hr) Exhaust heat boiler Recovered steam amount up 4-8 T / hr (maximum) (Recovered heat 4 × 10 6 Kcal / hr) Conventional exhaust heat boiler (base) Recovered heat 29 × 10 6 Kca
l / hr 45 to 50 T / hr (14 Kg / cm 2 270 ° C.) Increased recovery energy 16 × 10 6 Kcal / hr (26
% Increase) As described above, according to the present invention, the following effects can be obtained.
【００１５】（１）中圧蒸気、低圧蒸気の需給バランス
が変動しても、熱水循環系統と連結しているので、相互
に形態を変えて、損失を軽減して回収出来る。 （２）排熱源のポテンシャルに応じ、排熱源側、及び利
用側の変動に対し、適正な熱回収が出来る。即ち、 排熱回収装置は中圧蒸気回収用と、熱水および低圧
蒸気回収用の２段設置であるので、熱水および低圧蒸気
回収装置は変動吸収を目的とし多機能化出来る。多機能
化とは熱交換媒体を低圧蒸気、熱水、温水（１００℃以
下の水）の３形態としてとり得るものであり、エネルギ
ー需要バランスの変動に対し、形態変更、相互運用など
により、排熱の利用率の向上を図ることが出来る。 ポテンシャルの異なる排熱を複数の回収装置で、形
態、温度、圧力条件の異なったエネルギーに変換回収す
ることが出来るので、排熱発生源及び回収エネルギー使
用側のバランスを調節出来る。(1) Even if the supply and demand balance of medium-pressure steam and low-pressure steam fluctuates, since they are connected to the hot water circulation system, the forms can be changed mutually and loss can be reduced and recovered. (2) Depending on the potential of the exhaust heat source, appropriate heat recovery can be performed against fluctuations on the exhaust heat source side and the use side. That is, since the exhaust heat recovery device is installed in two stages, one for medium pressure steam recovery and the other for hot water and low pressure steam recovery, the hot water and low pressure steam recovery device can be made multi-functional for the purpose of absorbing fluctuations. Multifunctionalization means that the heat exchange medium can take three forms: low-pressure steam, hot water, and hot water (water at 100 ° C or lower). It is possible to improve the heat utilization rate. Exhaust heat having different potentials can be converted and recovered by a plurality of recovery devices into energy having different forms, temperatures, and pressure conditions, so that the balance between the exhaust heat generation source and the recovery energy use side can be adjusted.
【００１６】[0016]
【発明の効果】本発明は次の効果を得ることが出来る。 排熱回収領域が中低温領域まで拡大し、回収熱量が増
加する。 中圧、低圧蒸気の需要バランスが変動しても、熱水循
環系統を連結しているので、相互に形態を変えて損失を
軽減して回収できる。According to the present invention, the following effects can be obtained. The exhaust heat recovery area expands to the mid-low temperature area, and the amount of recovered heat increases. Even if the demand balance of medium-pressure and low-pressure steam fluctuates, the hot water circulation system is connected, so the forms can be changed mutually and the loss can be reduced and recovered.
【図面の簡単な説明】[Brief description of drawings]
【図１】本発明の一実施例を示す図である。FIG. 1 is a diagram showing an embodiment of the present invention.
【符号の説明】 １ 中圧蒸気回収装置 ２ 熱水および低圧蒸気回収装置 ３ 節炭器 ４ 熱水循環配管 ５ 蒸気を需要する工場の総称 ６ 焼結クーラ ７ 切換弁 ８ 高温排風側のダクト ９ 低温排風側のダクト １０ エバポレータ １１ スーパーヒータ １２ ドラム １３ 熱水熱交換器 １４ 低圧蒸気フラッシュタンク １５ フラッシュ蒸気弁 １６ ヘッダ管 １７ 分岐管 １８ 制御機構[Explanation of symbols] 1 Medium pressure steam recovery device 2 Hot water and low pressure steam recovery device 3 Coal economizer 4 Hot water circulation pipe 5 Generic name of a factory that demands steam 6 Sintering cooler 7 Switching valve 8 High temperature exhaust side duct 9 Low temperature exhaust side duct 10 Evaporator 11 Super heater 12 Drum 13 Hot water heat exchanger 14 Low pressure steam flash tank 15 Flash steam valve 16 Header pipe 17 Branch pipe 18 Control mechanism
───────────────────────────────────────────────────── フロントページの続き (72)発明者 田崎 重吉 東京都千代田区丸の内一丁目１番２号 日 本鋼管株式会社内 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Shigeyoshi Tasaki 1-2-1, Marunouchi, Chiyoda-ku, Tokyo Nihon Steel Pipe Co., Ltd.
Claims (2)
に、クーラの排風を熱交換する中圧蒸気回収装置と、熱
水および低圧蒸気回収装置を付設して、前記中圧蒸気回
収装置の節炭器と、熱水および低圧蒸気回収装置の熱水
循環配管との間に切換機構を設けて連結させたことを特
徴とする高温粒塊物のクーラの熱回収設備。1. A medium-pressure steam recovery device for heat-exchanging the exhaust air of the cooler and a hot water and low-pressure steam recovery device are attached to a cooler for continuously cooling high-temperature agglomerates, and the medium-pressure steam recovery device is provided. A heat recovery equipment for a cooler of high-temperature agglomerates, characterized in that a switching mechanism is provided and connected between the economizer of the device and the hot water circulation pipe of the hot water and low pressure steam recovery device.
排風と熱交換して中圧蒸気と、熱水および低圧蒸気を回
収するにあたり、前記熱水と低圧蒸気の使用量に余剰を
生じた場合、その熱水の一部を中圧蒸気に、また、熱水
と低圧蒸気の使用量に不足を生じた場合、中圧蒸気の供
給熱水の一部を低圧蒸気にすることを特徴とする高温粒
塊物のクーラの熱回収設備及びその熱回収方法。2. When recovering medium-pressure steam, hot water and low-pressure steam by exchanging heat with exhaust air of a cooler for continuously cooling high-temperature agglomerates, excess amount of hot water and low-pressure steam is used. If some of the hot water is used as medium pressure steam, and if the amount of hot water and low pressure steam used is insufficient, some of the hot water supplied as medium pressure steam is used as low pressure steam. And a heat recovery equipment for a cooler of high-temperature agglomerates characterized by the above.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP32371393A JP2842186B2 (en) | 1993-12-22 | 1993-12-22 | Heat recovery equipment for cooler for hot granular mass and heat recovery method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP32371393A JP2842186B2 (en) | 1993-12-22 | 1993-12-22 | Heat recovery equipment for cooler for hot granular mass and heat recovery method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07180976A true JPH07180976A (en) | 1995-07-18 |
| JP2842186B2 JP2842186B2 (en) | 1998-12-24 |
Family
ID=18157775
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP32371393A Expired - Fee Related JP2842186B2 (en) | 1993-12-22 | 1993-12-22 | Heat recovery equipment for cooler for hot granular mass and heat recovery method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2842186B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008256309A (en) * | 2007-04-06 | 2008-10-23 | Nippon Steel Corp | Sintered material pellet drying installation and sintered material pellet drying method |
| CN104792186A (en) * | 2015-03-31 | 2015-07-22 | 孙慕文 | Sintering flue gas energy-saving type denitrification system |
-
1993
- 1993-12-22 JP JP32371393A patent/JP2842186B2/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008256309A (en) * | 2007-04-06 | 2008-10-23 | Nippon Steel Corp | Sintered material pellet drying installation and sintered material pellet drying method |
| CN104792186A (en) * | 2015-03-31 | 2015-07-22 | 孙慕文 | Sintering flue gas energy-saving type denitrification system |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2842186B2 (en) | 1998-12-24 |
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