JP3699520B2 - Waste heat recovery device - Google Patents
Waste heat recovery device Download PDFInfo
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- JP3699520B2 JP3699520B2 JP04183996A JP4183996A JP3699520B2 JP 3699520 B2 JP3699520 B2 JP 3699520B2 JP 04183996 A JP04183996 A JP 04183996A JP 4183996 A JP4183996 A JP 4183996A JP 3699520 B2 JP3699520 B2 JP 3699520B2
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- Prior art keywords
- water
- waste heat
- gas
- deaerator
- heat boiler
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Description
【０００１】
【発明の属する技術分野】
本発明は、燃焼排ガス冷却設備における廃熱ボイラー設備後の腐食性ガスを含む低温排ガスの熱回収装置に関する。
【０００２】
【従来の技術】
ごみ処理施設の燃焼排ガス冷却設備における排熱回収装置は、高温の燃焼排ガスを冷却し蒸気を発生させるための廃熱ボイラー、さらにその排ガスを冷却し廃熱ボイラーへの給水を予熱するための節炭器よりなる。
図２を用いて従来の実施例を説明すると、燃焼排ガスは廃熱ボイラー（１）の入口で約８５０℃であり、これが廃熱ボイラー（１）の仕切壁（１−１）上下部でガス流れが３回反転しながら冷却され約３００℃となり排ガスは節炭器（２）へ上から流入し約２００℃に冷却された後、節炭器下部に設置された、ろ過式集塵器（５）の入口温度を調整する水噴射式ガス冷却塔（４）へ導かれる。
【０００３】
一方、ボイラー用水は脱気器給水ポンプ（６）により脱気器（７）に供給される。ここで蒸気だめ（１０）からの蒸気を吹き込んで約１４０℃まで加熱し、ボイラー用水中の溶存酸素を放出し、加熱脱気されたボイラー用水はボイラー給水ポンプ（８）で昇圧され節炭器（２）へ給水される。節炭器ではガス流れに対し、図３に示す（１２）の向流式で熱交換を行い、給水を予熱し廃熱ボイラー（１）へ給水される。廃熱ボイラーで発生した蒸気は大半がタービンへ送気され、一部が脱気器（７）の加熱蒸気として使用される。
【０００４】
【発明が解決しようとする課題】
従来のような方式では次のような課題を抱えている。
第一に、通常、節炭器（２）への通水は器内で温水になるため下から上へと自然な方向に流し、排ガスは上から下へと流す図３に示す（１２）の向流型熱交換としているが、設置空間等の制約から廃熱ボイラー（１）内でのガス流れの反転数が偶数となり、節炭器への排ガスを下から流さざるを得ない場合も出てくる。このような場合、節炭器での熱交換が図３に示す（１３）の並流型熱交換となり節炭器内の水は熱交換した分のΔｔ1 昇温するため、出口ガス温度と接近し所定のガス温度まで下げられず、その結果、必要な熱回収ができなくなることである。
【０００５】
第二に、上向きガス流れ式の水噴射式ガス冷却塔（４）の下部がダクト（１１）のみで構成されている場合、負荷によってはドレンが滴下しダストがダクト壁面に付着する心配がある。
第三に、立ち上げ初期には節炭器内の水は常温であり、廃熱ボイラーから蒸気が発生するまでの相当な時間は節炭器出口ガス温度が低く、低温腐食防止上、後流のろ過式集塵機（５）への通ガスは待機せざるを得ないことである。
【０００６】
【課題を解決するための手段】
燃焼排ガスを冷却し蒸気を発生させる廃熱ボイラー設備と、その後流にろ過式集塵機の入口温度を調整する上向きガス流れ式の水噴射式ガス冷却塔を備えた燃焼排ガス冷却設備において、水噴射式ガス冷却塔の下部に低圧蒸発冷却器を設け、これに廃熱ボイラー給水用の脱気器器内水を循環させる水路を形成したことを特徴とする排熱回収装置を提供するものである。
【０００７】
図１を用いて説明すると、節炭器（２）出口で約２６０℃の排ガスは、低圧蒸発冷却器（３）での熱交換によって約２００℃まで低下し、一方、脱気器（７）からの循環水は約１４０℃の飽和水のものが一部飽和蒸気となり脱気器へ導かれ、脱気器ではさらに従来より少な目の蒸気を蒸気だめ（１０）から追加的に供給して約１４０℃まで昇温する。
【０００８】
すなわち、本発明の特色は図３の並流型熱交換（１３）に示すように低圧蒸発冷却器出入口の水の温度差がほとんどないことを利用して排ガスとの温度差Δｔ2 を高め、また、いずれの排ガス流れにも適用でき、必要な低温の熱回収ができるという点である。
また、設備的にみても、小容量の循環水ポンプ（９）を設けることにより脱気器器内水を循環させるだけで、制御装置も必要なく容易に設備に適用でき運転取扱も簡単である。
【０００９】
【発明の実施の形態】
図１を基にして、本発明の実施例について説明する。
図にあって、（１）は廃熱ボイラーで内部には仕切り壁（１−１）が設けられ、排ガスはボイラー内の下部及び上部で反転しながら熱交換部（ボイラー）で熱交換し、その後段に設けられている節炭器（２）にて排ガスは冷却、即ち、給水を予熱する如くなしている。
次に、上記廃熱ボイラーはダクト（１１）を介し、水噴射式ガス冷却塔（４）に接続され、ろ過式集塵機（５）に導入される排ガス温度を調整する如くなしている。
【００１０】
今、本発明にあっては、前記水噴射式ガス冷却塔（４）の下部のダクト（１１）内に低圧蒸発冷却器（３）が設けられており、該低圧蒸発冷却器への給水は、廃熱ボイラーへの給水とは独立させて、脱気器器内水を脱気器循環水ポンプ（９）で循環供給し、ここで燃焼排ガスの持つ廃熱を回収し、一部飽和蒸気の水として脱気器（７）に戻すようになしている。
【００１１】
このような構成になる本発明の排ガス及び冷却水の流れを説明すると、燃焼排ガスは廃熱ボイラー（１）の入口で約８５０℃であり、これが廃熱ボイラーの仕切壁（１−１）上下部でガス流れが２回反転しながら冷却され約３００℃となり、排ガスは後段の節炭器（２）で約２６０℃に冷却された後上側に反転し、ろ過式集塵機５の入口温度を調整する上向きガス流れ式の水噴射式ガス冷却塔（４）の下部に設置された低圧蒸発冷却器（３）へ導かれ、約２００℃に冷却される。
【００１２】
一方、ボイラー用水は脱気器給水ポンプ（６）により脱気器（７）に供給される。ここで蒸気だめ（１０）からの蒸気を吹き込んで約１４０℃まで加熱し、ボイラー用水中の溶存酸素を放出し、加熱脱気されたボイラー用水はボイラー給水ポンプ（８）で昇圧され節炭器（２）へ給水される。節炭器で向流式の熱交換を行い、給水を予熱し廃熱ボイラー（１）へ給水される。廃熱ボイラーで発生した蒸気は大半がタービンヘ送気され、一部が脱気器の加熱蒸気として使用される。
【００１３】
【発明の効果】
以上説明したように、本発明によれば次の如き優れた効果を発揮する。
（１）ダクトでガス流れを反転させることなく、上向きガス流れに対する並流型熱交換で、必要な熱回収ができる。
（２）節炭器方式と比較して、ガスとの温度差が大きくとれ伝熱面積が低減できる。
（３）上向流式の水噴射式ガス冷却塔の下部に低圧蒸発冷却器を設けることによって、滴下ドレンを蒸発させることができる。
（４）常時約１４０℃の脱気器器内水を循環できるため、立ち上げ時、後流のろ過式集塵機への通ガスを早めることができる。
【図面の簡単な説明】
【図１】本発明装置を組み込んだ排熱回収装置の例を示す図、
【図２】従来の排熱回収装置の例を示す図、
【図３】一般の熱交換型式を示す図である。
【符号の説明】
1 廃熱ボイラー
2 節炭器
3 低圧蒸発冷却器
4 水噴射式ガス冷却塔
5 ろ過式集塵機
6 脱気器給水ポンプ
7 脱気器
8 ボイラー給水ポンプ
9 脱気器循環水ポンプ
1 0 蒸気だめ
1 1 ダクト
1 2 向流型熱交換
1 3 並流型熱交換[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a heat recovery apparatus for low-temperature exhaust gas containing corrosive gas after waste heat boiler equipment in combustion exhaust gas cooling equipment.
[0002]
[Prior art]
The exhaust heat recovery device in the flue gas cooling facility of the waste treatment facility is a waste heat boiler that cools the high temperature flue gas and generates steam, and a section that cools the exhaust gas and preheats the feed water to the waste heat boiler. It consists of charcoal.
The conventional example will be described with reference to FIG. 2. The combustion exhaust gas is about 850 ° C. at the inlet of the waste heat boiler (1), and this is gas at the upper and lower parts of the partition wall (1-1) of the waste heat boiler (1). After the flow is reversed three times, it is cooled to about 300 ° C, and the exhaust gas flows into the economizer (2) from above and is cooled to about 200 ° C, and then is installed in the lower part of the economizer. It is led to a water injection type gas cooling tower (4) for adjusting the inlet temperature of 5).
[0003]
On the other hand, the boiler water is supplied to the deaerator (7) by the deaerator water supply pump (6). Here, steam from the steam sump (10) is blown and heated to about 140 ° C. to release dissolved oxygen in the boiler water, and the heated and degassed boiler water is pressurized by the boiler feed pump (8) to save the economizer. Water is supplied to (2). In the economizer, heat exchange is performed on the gas flow by the countercurrent type (12) shown in FIG. 3 to preheat the feed water and feed it to the waste heat boiler (1). Most of the steam generated in the waste heat boiler is sent to the turbine, and part of it is used as heating steam for the deaerator (7).
[0004]
[Problems to be solved by the invention]
The conventional method has the following problems.
First, the water flow to the economizer (2) is usually warm water in the vessel, so it flows in a natural direction from bottom to top, and the exhaust gas flows from top to bottom as shown in FIG. 3 (12) However, there are cases where the reversal of the gas flow in the waste heat boiler (1) is an even number due to restrictions on the installation space, etc., and the exhaust gas to the economizer is forced to flow from below. Come out. In such a case, the heat exchange in the economizer becomes a co-current type heat exchange (13) shown in FIG. 3 and the water in the economizer is heated up by Δt 1 corresponding to the heat exchange. It approaches and cannot be lowered to a predetermined gas temperature, and as a result, the necessary heat recovery cannot be performed.
[0005]
Secondly, when the lower part of the upward gas flow type water jet type gas cooling tower (4) is composed of only the duct (11), depending on the load, there is a concern that drain may drip and dust may adhere to the duct wall surface. .
Third, the water in the economizer is at room temperature at the beginning of startup, and the gas saver outlet gas temperature is low for a considerable amount of time until steam is generated from the waste heat boiler. The gas flow to the filtration type dust collector (5) must be on standby.
[0006]
[Means for Solving the Problems]
In a combustion exhaust gas cooling facility equipped with a waste heat boiler facility that cools combustion exhaust gas and generates steam, and an upward gas flow type water injection type gas cooling tower that adjusts the inlet temperature of the filtration dust collector in the downstream, water injection type A low-pressure evaporative cooler is provided at the lower part of a gas cooling tower, and a water passage for circulating water in a deaerator for waste heat boiler feed water is formed therein.
[0007]
Referring to FIG. 1, the exhaust gas at about 260 ° C. at the outlet of the economizer (2) is lowered to about 200 ° C. by heat exchange in the low pressure evaporative cooler (3), while the deaerator (7). Circulating water from the saturated water at about 140 ° C. is partially saturated steam and is led to the deaerator. The deaerator further supplies a smaller amount of steam from the conventional steam sump (10) to reduce the steam. The temperature is raised to 140 ° C.
[0008]
That is, the feature of the present invention is to increase the temperature difference Δt 2 with the exhaust gas by utilizing the fact that there is almost no temperature difference between the water at the inlet and outlet of the low-pressure evaporative cooler as shown in the parallel flow heat exchange (13) in FIG. In addition, it can be applied to any exhaust gas flow, and the necessary low-temperature heat recovery can be performed.
Also, from the viewpoint of equipment, by providing a small-capacity circulating water pump (9), only the water in the deaerator is circulated, and a control device is not necessary and can be easily applied to the equipment and the operation handling is simple. .
[0009]
DETAILED DESCRIPTION OF THE INVENTION
An embodiment of the present invention will be described with reference to FIG.
In the figure, (1) is a waste heat boiler, and a partition wall (1-1) is provided inside, and the exhaust gas is heat-exchanged at the heat exchanging part (boiler) while being inverted at the lower and upper parts in the boiler, The exhaust gas is cooled in the economizer (2) provided in the subsequent stage, that is, the feed water is preheated.
Next, the waste heat boiler is connected to the water jet type gas cooling tower (4) through the duct (11) so as to adjust the exhaust gas temperature introduced into the filtration type dust collector (5).
[0010]
In the present invention, a low-pressure evaporative cooler (3) is provided in a duct (11) below the water-injection gas cooling tower (4), and water supply to the low-pressure evaporative cooler is as follows. Independently from the water supply to the waste heat boiler, the deaerator water is circulated and supplied by the deaerator circulating water pump (9), where the waste heat of the combustion exhaust gas is recovered and partially saturated steam. The water is returned to the deaerator (7).
[0011]
Explaining the flow of the exhaust gas and cooling water of the present invention having such a configuration, the combustion exhaust gas is about 850 ° C. at the inlet of the waste heat boiler (1), which is above and below the partition wall (1-1) of the waste heat boiler. The gas flow is cooled at about 300 ° C while reversing the gas flow twice, and the exhaust gas is cooled to about 260 ° C in the latter stage economizer (2) and then turned upside down to adjust the inlet temperature of the
[0012]
On the other hand, the boiler water is supplied to the deaerator (7) by the deaerator water supply pump (6). Here, steam from the steam sump (10) is blown and heated to about 140 ° C. to release dissolved oxygen in the boiler water, and the heated and degassed boiler water is pressurized by the boiler feed pump (8) to save the economizer. Water is supplied to (2). Countercurrent heat exchange is performed in the economizer to preheat the feed water and feed it to the waste heat boiler (1). Most of the steam generated in the waste heat boiler is sent to the turbine, and part of it is used as heating steam for the deaerator.
[0013]
【The invention's effect】
As described above, according to the present invention, the following excellent effects are exhibited.
(1) Necessary heat recovery can be achieved by cocurrent flow heat exchange with the upward gas flow without reversing the gas flow in the duct.
(2) Compared with the economizer system, the temperature difference with the gas is large and the heat transfer area can be reduced.
(3) By providing a low-pressure evaporative cooler at the lower part of the upward flow type water jet type gas cooling tower, the dripped drain can be evaporated.
(4) Since the water in the deaerator at about 140 ° C. can be circulated at all times, it is possible to expedite the gas flow to the downstream filtration dust collector at startup.
[Brief description of the drawings]
FIG. 1 is a view showing an example of an exhaust heat recovery apparatus incorporating the apparatus of the present invention;
FIG. 2 is a view showing an example of a conventional exhaust heat recovery device;
FIG. 3 is a diagram showing a general heat exchange type.
[Explanation of symbols]
1 Waste heat boiler
2 economizer
3 Low pressure evaporative cooler
4 Water injection type gas cooling tower
5 Filtration dust collector
6 Deaerator water pump
7 Deaerator
8 Boiler feed pump
9 Deaerator circulating water pump
1 0 Steam
1 1 Duct
1 2 Counterflow heat exchange
1 3 Cocurrent heat exchange
Claims (1)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP04183996A JP3699520B2 (en) | 1996-02-28 | 1996-02-28 | Waste heat recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP04183996A JP3699520B2 (en) | 1996-02-28 | 1996-02-28 | Waste heat recovery device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH09236206A JPH09236206A (en) | 1997-09-09 |
| JP3699520B2 true JP3699520B2 (en) | 2005-09-28 |
Family
ID=12619436
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP04183996A Expired - Fee Related JP3699520B2 (en) | 1996-02-28 | 1996-02-28 | Waste heat recovery device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3699520B2 (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57122923A (en) * | 1981-01-21 | 1982-07-31 | Miura Co Ltd | Waste heat recovery and desulfurization apparatus |
| JPS6073202A (en) * | 1983-09-30 | 1985-04-25 | 株式会社笹倉機械製作所 | Energy conserving deaerator |
| JPS6391407A (en) * | 1986-10-03 | 1988-04-22 | 三菱重工業株式会社 | Corrosion protection method of exhaust-gas boiler deaerator generating tube |
| JPH0933024A (en) * | 1995-07-14 | 1997-02-07 | Kubota Corp | Heat recovering method in exhaust gas treatment |
-
1996
- 1996-02-28 JP JP04183996A patent/JP3699520B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH09236206A (en) | 1997-09-09 |
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