JPS6316008B2 - - Google Patents
Info
- Publication number
- JPS6316008B2 JPS6316008B2 JP56072179A JP7217981A JPS6316008B2 JP S6316008 B2 JPS6316008 B2 JP S6316008B2 JP 56072179 A JP56072179 A JP 56072179A JP 7217981 A JP7217981 A JP 7217981A JP S6316008 B2 JPS6316008 B2 JP S6316008B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- heat
- heat medium
- temperature
- heater
- 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
Links
- 239000007789 gas Substances 0.000 claims description 95
- 238000000034 method Methods 0.000 claims description 21
- 238000010438 heat treatment Methods 0.000 claims description 17
- 238000006477 desulfuration reaction Methods 0.000 claims description 10
- 230000023556 desulfurization Effects 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 6
- 238000003303 reheating Methods 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 239000003546 flue gas Substances 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 description 15
- 230000007797 corrosion Effects 0.000 description 11
- 238000005260 corrosion Methods 0.000 description 11
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chimneys And Flues (AREA)
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】
本発明は排煙脱硫時の処理ガス温度を熱媒循環
により調整する際の改良法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an improved method for adjusting the temperature of a treated gas during flue gas desulfurization by circulating a heat medium.
湿式排煙脱硫装置にて処理後の燃焼排ガスは水
蒸気飽和の状態にあり且つ二酸化硫黄（SO2）等
の腐食成分を微量含有しているので、鋼製煙突の
腐食防止および白煙防止のため、再加熱装置にて
昇温後大気放散している。従来、再加熱方法とし
てアフターバーニング方式が採用されていたが、
エネルギーコストの急上昇により、脱硫入口高温
未処理ガスと脱硫出口低温処理ガスを熱交換して
再加熱する省エネルギータイプが実用化されてい
る。省エネルギータイプとして回転蓄熱式熱交換
器が採用されているが、この方式は波板状エレメ
ントを蓄熱板として積み上げており、その為ガス
通路が狭く、特に石炭焚ボイラー用に使用する場
合、ダストの付着およびダストの乾湿の繰返しに
よる固着化等により通路閉塞を起し、運転不能と
なる。またこの方式は高温側より低温側へ未処理
ガスの漏洩が発生するので脱硫装置が大型になる
欠点を有す。 Combustion exhaust gas after treatment in the wet flue gas desulfurization equipment is saturated with water vapor and contains small amounts of corrosive components such as sulfur dioxide (SO 2 ), so it is necessary to prevent corrosion of steel chimneys and prevent white smoke. After being heated in a reheating device, it is released into the atmosphere. Conventionally, the afterburning method was used as a reheating method, but
Due to the rapid rise in energy costs, energy-saving types have been put into practical use that reheat the high-temperature untreated gas at the desulfurization inlet and the low-temperature treated gas at the desulfurization outlet by exchanging heat. A rotary regenerative heat exchanger has been adopted as an energy-saving type, but this method uses corrugated elements stacked up as heat storage plates, so the gas passage is narrow, making it difficult to collect dust, especially when used for coal-fired boilers. Due to adhesion and solidification due to repeated drying and wetting of dust, passages become blocked and operation becomes impossible. Furthermore, this method has the disadvantage that the desulfurization equipment becomes large because untreated gas leaks from the high temperature side to the low temperature side.
このように石炭焚ボイラー用湿式排煙脱硫装置
の再加熱装置として回転蓄熱式熱交換器はダスト
による通路閉塞等により運転不能となり易く、又
未処理ガスの処理ガスへの漏洩により脱硫処理後
の処理ガス中の二酸化硫黄（SO2）の濃度上昇が
あるためこれらを解消すべく、回転蓄熱式熱交換
方法に代る方式につき研究する過程で、熱媒循環
方式密閉多管型熱交換法（以下、これに使用する
装置をガス・ガス・ヒータまたはGGHと略称す
る）を用いることが合目的であることを確認した
が、ガス・ガス・ヒータの処理ガス（脱硫を後え
たガス）の伝熱管は、吸収液ミストを含んだ水蒸
気飽和状態の処理ガスに曝されるので、その腐食
は非常に激しいものとなり、更に負荷変動による
熱媒温度の低下により、更に苛酷な状態となるこ
とを見出した。そこで本発明者らは、負荷変動が
発生しても熱媒温度を可能な限り低下させず常に
高温に保持することにより装置の耐食性を向上さ
せ、同時に再加熱システム全体のコストダウンを
計るべき熱媒循環方式密閉多管型熱交換法につき
更に鋭意検討を重ね本発明を完成するに至つた。 As described above, the rotary regenerative heat exchanger used as a reheating device in a wet flue gas desulfurization system for a coal-fired boiler is likely to become inoperable due to passage blockage caused by dust, and leakage of untreated gas into the treated gas may cause damage after desulfurization. In order to eliminate the increase in the concentration of sulfur dioxide (SO 2 ) in the processed gas, in the process of researching an alternative method to the rotary regenerative heat exchange method, we decided to develop a closed multi-tube heat exchange method using a heating medium circulation method ( It has been confirmed that it is appropriate to use a device used for this purpose (hereinafter referred to as a gas-gas heater or GGH), but the transmission of the processing gas (gas after desulfurization) from the gas-gas heater has been confirmed. Since the heat tubes are exposed to water vapor-saturated processing gas containing absorption liquid mist, the corrosion becomes extremely severe, and we found that the condition becomes even more severe as the heating medium temperature decreases due to load fluctuations. Ta. Therefore, the present inventors aimed to improve the corrosion resistance of the equipment by keeping the heating medium temperature as high as possible without lowering it even when load fluctuations occur, and at the same time reduce the cost of the entire reheating system. The present invention was completed after further intensive study on the medium circulation closed multi-tube heat exchange method.
すなわち本発明は未処理ガス冷却部と処理ガス
加熱部との間を循環する熱媒により未処理ガスを
冷却し、処理ガスを再加熱するガス・ガス・ヒー
タ方式において、未処理ガスと熱交換し加熱され
た熱媒を、蒸気等により昇温し、処理ガス側へ送
入する方法に関し、これにより負荷変動があつた
場合にも熱媒温度を低下させることなく運転で
き、したがつて最も腐食の激しい処理ガス側低温
部の伝熱管材料の耐食性が向上すると共に、低級
材料の採用が可能となるので、再加熱システム全
体のコストダウンが可能となつたものである。 That is, the present invention cools the untreated gas by a heating medium circulating between the untreated gas cooling section and the treated gas heating section, and in the gas-to-gas heater method in which the treated gas is reheated, heat exchange with the untreated gas is performed. Regarding the method of raising the temperature of the heated heating medium using steam or the like and sending it to the processing gas side, this method allows operation without lowering the heating medium temperature even when there are load fluctuations, and is therefore the most efficient. This improves the corrosion resistance of the heat exchanger tube material in the low-temperature section on the processing gas side, where corrosion is severe, and allows the use of lower-grade materials, making it possible to reduce the cost of the entire reheating system.
以下、本発明の一具体例を添付図面を参照しな
がら更に詳述する。第１図はその具体例の概略的
なフローを示し、第２図は第１図フローのガス・
ガス・ヒータの制御関係を示す説明図である。 Hereinafter, a specific example of the present invention will be described in more detail with reference to the accompanying drawings. Figure 1 shows a schematic flow of a specific example, and Figure 2 shows the gas flow of Figure 1.
FIG. 3 is an explanatory diagram showing the control relationship of the gas heater.
第１図において２８は排ガスフアン、１は熱回
収器（未処理ガス側ガス・ガス・ヒータ）、２９
は冷却塔、３０は吸収塔、３１はプレヒータ、２
は再加熱器（処理ガス側ガス・ガス・ヒータ）、
３３はスチームガスヒータ、３５はスタツク、１
２は熱回収器の伝熱管、１３は再加熱器の伝熱
管、３２はプレヒータの伝熱管、３４はスチーム
ガスヒータの伝熱管、５は熱媒ポンプ、３は熱媒
加熱器、１４，１５，１６，１７，３６，３７，
３８，３９はガスダクト、１８，２２，２３，２
５は熱媒配管を示す。 In Fig. 1, 28 is an exhaust gas fan, 1 is a heat recovery device (untreated gas side gas heater), 29
is a cooling tower, 30 is an absorption tower, 31 is a preheater, 2
is a reheater (processing gas side gas heater),
33 is a steam gas heater, 35 is a stack, 1
2 is a heat transfer tube of a heat recovery device, 13 is a heat transfer tube of a reheater, 32 is a heat transfer tube of a preheater, 34 is a heat transfer tube of a steam gas heater, 5 is a heat medium pump, 3 is a heat medium heater, 14, 15, 16, 17, 36, 37,
38, 39 are gas ducts, 18, 22, 23, 2
5 indicates a heat medium pipe.
又第２図中において１は熱回収器（未処理ガス
側ガス・ガスヒータ）、２は再加熱器（処理ガス
側ガス・ガスヒータ）、３は熱媒加熱器、４は熱
媒膨張タンク、５は熱媒ポンプ、６は熱媒流量制
御弁、７は蒸気流量制御弁、８，９は温度検出
器、１０，１１は温度調節器、１２は熱回収器の
伝熱管、１３は再加熱器の伝熱管、１４，１５，
１６，１７はガスダクト、１８，１９，２０，２
１，２２，２３，２４，２５は熱媒配管、２６，
２７は蒸気配管を示す。 In Fig. 2, 1 is a heat recovery device (untreated gas side gas/gas heater), 2 is a reheater (treated gas side gas/gas heater), 3 is a heat medium heater, 4 is a heat medium expansion tank, and 5 is a heat medium expansion tank. is a heat medium pump, 6 is a heat medium flow control valve, 7 is a steam flow control valve, 8 and 9 are temperature detectors, 10 and 11 are temperature regulators, 12 is a heat exchanger tube of a heat recovery device, and 13 is a reheater Heat exchanger tube, 14, 15,
16, 17 are gas ducts, 18, 19, 20, 2
1, 22, 23, 24, 25 are heat medium pipes, 26,
27 indicates a steam pipe.
第１図において、未処理ガスはガスダクト３９
を経て排ガスフアン２８により昇圧されガスダク
ト１４を通つて、熱回収器（未処理ガス側ガス・
ガスヒータ）１に入る。熱回収器１内において未
処理ガスは熱回収器の伝熱管１２内の熱媒ポンプ
５により送られる熱媒を加熱して温度降下してガ
スダクト１５を経て冷却塔２９に入る。冷却塔２
９において未処理ガスは散水により冷却されると
共にダストおよび可溶性ガスが一部除去され、ガ
スダクト３６を経て、吸収塔３０に入る。吸収塔
３０において未処理ガス中の二酸化硫黄は吸収液
に吸収され、ミスト除去後、ガスダクト３７を経
てプレヒータ３１に入る。プレヒータ３１内にお
いて処理ガスはプレヒータの伝熱管３２内の蒸気
により加熱され、ガスダクト１６を経て再加熱器
２に入る。再加熱器２内において、処理ガスは、
熱媒加熱器３により更に昇温され熱媒配管２３を
経て再加熱器２の伝熱管１３に導入される熱媒に
より、加熱・昇温され、ガスダクト１７を経てス
チームガスヒータ３３に入る。スチームガスヒー
タ３３内において処理ガスはスチームガスヒータ
３３の伝熱管３４内を流れるスチームにより更に
昇温され、ガスダクト３８を経て、スタツク３５
より大気に放散される。 In Figure 1, the untreated gas is transferred to the gas duct 39.
The pressure is increased by the exhaust gas fan 28 and passed through the gas duct 14 to the heat recovery device (untreated gas side gas
Gas heater) enters 1. In the heat recovery device 1, the untreated gas heats the heat medium sent by the heat medium pump 5 in the heat transfer tube 12 of the heat recovery device to lower its temperature, and enters the cooling tower 29 through the gas duct 15. cooling tower 2
At 9, the untreated gas is cooled by water spraying, dust and soluble gases are partially removed, and the untreated gas passes through the gas duct 36 and enters the absorption tower 30. In the absorption tower 30, the sulfur dioxide in the untreated gas is absorbed by the absorption liquid, and after removing the mist, it enters the preheater 31 via the gas duct 37. In the preheater 31 , the process gas is heated by steam in the heat transfer tube 32 of the preheater and enters the reheater 2 via the gas duct 16 . In the reheater 2, the processing gas is
The heat medium is further heated by the heat medium heater 3 and introduced into the heat transfer tube 13 of the reheater 2 via the heat medium piping 23, whereupon it is heated and heated, and then enters the steam gas heater 33 through the gas duct 17. In the steam gas heater 33, the processing gas is further heated by the steam flowing through the heat transfer tube 34 of the steam gas heater 33, and passes through the gas duct 38 to the stack 35.
more dissipated into the atmosphere.
第２図において、ガス・ガスヒータの作用を更
に詳細に説明するとガスダクト１４を経て、熱回
収器１に入つた未処理ガスは熱回収器１の伝熱管
１２内を流れる熱媒を加熱し、温度降下してガス
ダクト１５に到る。一方熱媒は熱媒ポンプ５によ
り送液され、熱媒配管１８，１９を経て、熱回収
器１の伝熱管１２に送入される。但しガスダクト
１５に設置してある温度検出器８により未処理ガ
スの出口温度が一定以下に下らないよう、温度調
節器１０にて熱媒配管２０に設置してある熱媒流
量制御弁６の開度を調節し、熱媒の一部バイパス
を行なう。 In FIG. 2, to explain the operation of the gas-gas heater in more detail, the untreated gas that enters the heat recovery device 1 through the gas duct 14 heats the heat medium flowing in the heat transfer tubes 12 of the heat recovery device 1, and the temperature increases. It descends and reaches the gas duct 15. On the other hand, the heat medium is sent by the heat medium pump 5 and is sent to the heat transfer tube 12 of the heat recovery device 1 via the heat medium pipes 18 and 19. However, in order to prevent the outlet temperature of the untreated gas from falling below a certain level by the temperature detector 8 installed in the gas duct 15, the opening degree of the heating medium flow rate control valve 6 installed in the heating medium piping 20 is controlled by the temperature controller 10. The heating medium is partially bypassed.
熱回収器１にて熱交換後の熱媒配管２１よりの
熱媒は、熱媒配管２０をバイパスしてきた熱媒と
混合し、更に熱媒配管２２を経て熱媒加熱器３に
入る。 The heat medium from the heat medium pipe 21 after heat exchange in the heat recovery device 1 mixes with the heat medium that has bypassed the heat medium pipe 20, and further enters the heat medium heater 3 via the heat medium pipe 22.
一方、熱媒配管２４に設置してある温度検出器
９により、熱媒配管２４内の熱媒温度が一定以下
にならないように温度調節器１１にて蒸気配管２
６に設置してある蒸気流量制御弁７の開度を調節
し、熱媒加熱器３に熱媒配管２２を経て流入する
熱媒を更に加熱、昇温する。 On the other hand, a temperature detector 9 installed in the heat medium pipe 24 detects that the temperature of the steam pipe 2 is controlled by a temperature regulator 11 so that the temperature of the heat medium in the heat medium pipe 24 does not fall below a certain level.
The opening degree of the steam flow control valve 7 installed at 6 is adjusted to further heat and raise the temperature of the heat medium flowing into the heat medium heater 3 via the heat medium pipe 22.
一方、熱媒加熱器３にて加熱・昇温された熱媒
は、熱媒配管２３を経て、再加熱器２の伝熱管１
３に入り、ガスダクト１６により導入された処理
ガスを再加熱器２内にて、所定温度まで加熱後、
自身は冷却し、熱媒配管２４を経て熱媒膨張タン
ク４に入り、熱媒配管２５を経て熱媒ポンプ５に
到る。 On the other hand, the heat medium heated and heated by the heat medium heater 3 passes through the heat medium pipe 23 and then passes through the heat transfer tube 1 of the reheater 2.
3, and after heating the processing gas introduced through the gas duct 16 to a predetermined temperature in the reheater 2,
It cools itself, enters the heat medium expansion tank 4 via the heat medium pipe 24, and reaches the heat medium pump 5 via the heat medium pipe 25.
熱媒加熱器３に蒸気配管２６を経て導入された
熱媒加熱用蒸気は熱媒加熱器３内にて熱媒を加熱
後、凝縮し、蒸気配管２７を経て排出される。 The heat medium heating steam introduced into the heat medium heater 3 through the steam pipe 26 heats the heat medium in the heat medium heater 3, condenses, and is discharged through the steam pipe 27.
本発明の効果を列記すると以下の通りである。 The effects of the present invention are listed below.
(1) 再加熱器２にて熱交換後の熱媒温度を一定以
上に常時保持することにより次の効果が生じ
る。(1) By constantly maintaining the temperature of the heat medium after heat exchange in the reheater 2 above a certain level, the following effects occur.
火力発電所のボイラーは最大燃焼負荷運転
（以下MCRと略す）から1/4負荷運転までと
かなり広い範囲で運転されるためガス流量お
よび熱交換許容量がかなり低下する。ただ
し、熱回収器１の未処理ガス出口温度は熱回
収器１の伝熱管１２の硫酸露点腐食を避ける
ため、一定以下には下げることができないた
め、熱回収器１の熱交換量は限界がある。 Boilers in thermal power plants are operated over a fairly wide range from maximum combustion load operation (hereinafter abbreviated as MCR) to 1/4 load operation, resulting in a considerable reduction in gas flow rate and heat exchange capacity. However, the untreated gas outlet temperature of the heat recovery device 1 cannot be lowered below a certain level to avoid sulfuric acid dew point corrosion of the heat exchanger tubes 12 of the heat recovery device 1, so there is a limit to the amount of heat exchanged by the heat recovery device 1. be.
また処理ガスは冷却塔２９および吸収器３０で
冷却され、水蒸気飽和の状態となつており、更に
未吸収の腐食成分も残存しているのでその腐食環
境は相当厳しい。 Furthermore, the treated gas is cooled in the cooling tower 29 and the absorber 30 and is saturated with water vapor, and furthermore, unabsorbed corrosive components remain, so the corrosive environment is quite severe.
この水蒸気飽和の状態を避けるためプレヒータ
にて処理ガスを数℃（相対湿度約90％になる様）
昇温後、再加熱器２に導入するが、吸収塔３０か
らのミスト等は除去できないので、再加熱器２の
腐食環境は未だ厳しい。特に1/4負荷運転時、熱
回収器１の熱交換量が小さく従つて再加熱器２に
はいる熱媒温度は低下し、再加熱器の伝熱管１３
は広い範囲にわたつて水蒸気飽和の処理ガスにさ
らされることになり、著しい腐食を広範囲に受け
ることになる。 In order to avoid this water vapor saturation state, the processing gas is heated to several degrees Celsius using a preheater (so that the relative humidity is approximately 90%).
After raising the temperature, it is introduced into the reheater 2, but since mist etc. from the absorption tower 30 cannot be removed, the corrosive environment of the reheater 2 is still severe. Especially during 1/4 load operation, the heat exchange amount of the heat recovery device 1 is small, so the temperature of the heat medium entering the reheater 2 decreases, and the heat exchanger tube 13 of the reheater decreases.
will be exposed to water vapor saturated process gas over a wide range, and will be subject to severe corrosion over a wide area.
又、当社の処理ガス環境下における腐食テスト
結果より、伝熱管の腐食量はその管壁温度が高い
程小さいので、負荷変動にかかわらず管壁温度を
高温に保持すれば、腐食は軽減されることが判明
している。 In addition, our corrosion test results in a processing gas environment show that the higher the tube wall temperature, the smaller the amount of corrosion in heat transfer tubes, so if the tube wall temperature is maintained at a high temperature regardless of load fluctuations, corrosion can be reduced. It turns out that.
したがつて、再加熱器２にて処理ガスと熱交換
後の熱媒（熱媒配管２４のもの）の温度を、
MCRの設定温度と同温度になるよう熱媒加熱器
３により加熱することにより、再加熱器の伝熱管
１３全体の温度分布がMCRと同一条件になるた
め、水蒸気飽和の処理ガスにさらされる範囲は非
常に狭くなり、腐食がかなり軽減され、その結
果、低級材料の伝熱管が使用可能となる。なお、
プレヒータにより加熱量を増加すれば再加熱器２
に入る処理ガス温度が上昇し、ガス・ガスヒータ
の温度差が小さくなり、従つてガス・ガスヒータ
の伝熱面積が大巾に増加するので好ましくない。 Therefore, the temperature of the heat medium (those of the heat medium pipe 24) after heat exchange with the processing gas in the reheater 2 is
By heating the heat medium heater 3 to the same temperature as the set temperature of the MCR, the temperature distribution of the entire heat exchanger tube 13 of the reheater becomes the same as that of the MCR, so the range exposed to the steam-saturated process gas is much narrower, corrosion is considerably reduced, and as a result, heat exchanger tubes of lower grade materials can be used. In addition,
If the amount of heating is increased by the preheater, the reheater 2
This is undesirable because the temperature of the processing gas entering the gas increases, the temperature difference between the gas and the gas heater becomes smaller, and the heat transfer area of the gas and the gas heater increases significantly.
第１図は本発明の一具体例の概略的なフローを
示し、第２図は第１図のガス・ガスヒータの制御
関係を示す説明図である。
FIG. 1 shows a schematic flow of a specific example of the present invention, and FIG. 2 is an explanatory diagram showing the control relationship between the gas and the gas heater shown in FIG.
Claims (1)
ガス加熱部との間を循環する熱媒により、未処理
ガスを冷却し、処理ガスを再加熱する熱媒循環方
式密閉多管型ガス・ガス熱交換法において、処理
ガスと熱交換後の熱媒温度がボイラの最大燃焼負
荷運転の設定温度以下にならないよう、処理ガス
と熱交換前の熱媒側において加熱して制御するこ
とを特徴とする、排煙脱硫における処理ガス再加
熱方法。1 In flue gas desulfurization, a heat medium circulation type sealed multi-tube gas system that cools the untreated gas and reheats the treated gas using a heating medium that circulates between the untreated gas cooling section and the treated gas heating section. The heat exchange method is characterized by heating and controlling the heat medium side before heat exchange with the process gas so that the temperature of the heat medium after heat exchange with the process gas does not fall below the set temperature of the maximum combustion load operation of the boiler. A method for reheating treated gas in flue gas desulfurization.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56072179A JPS57187523A (en) | 1981-05-15 | 1981-05-15 | Reheating method of treated gas in flue gas desulfurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56072179A JPS57187523A (en) | 1981-05-15 | 1981-05-15 | Reheating method of treated gas in flue gas desulfurization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57187523A JPS57187523A (en) | 1982-11-18 |
| JPS6316008B2 true JPS6316008B2 (en) | 1988-04-07 |
Family
ID=13481734
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56072179A Granted JPS57187523A (en) | 1981-05-15 | 1981-05-15 | Reheating method of treated gas in flue gas desulfurization |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS57187523A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03125410A (en) * | 1989-09-30 | 1991-05-28 | Dornier Medizintechnik Gmbh | Flat coil |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0424272Y2 (en) * | 1985-10-30 | 1992-06-08 | ||
| JP3544432B2 (en) * | 1996-06-07 | 2004-07-21 | バブコック日立株式会社 | Exhaust gas treatment equipment and its operation method |
| JP4919766B2 (en) * | 2006-11-07 | 2012-04-18 | 中国電力株式会社 | Heating temperature adjustment method, temperature control system |
-
1981
- 1981-05-15 JP JP56072179A patent/JPS57187523A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03125410A (en) * | 1989-09-30 | 1991-05-28 | Dornier Medizintechnik Gmbh | Flat coil |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57187523A (en) | 1982-11-18 |
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